Technical Note
ORP/TAD-76-2
Determination of Radium Removal Efficiencies in Illinois Water Supply
Treatment Processes
by
Dorothy L. Bennett
Charles R. Bell
Ira M. Markwood
Illinois Environmental Protection Agency
Division of Public Water Supplies
2200 Churchill Road
Springfield, Illinois 62706
May, 1976
Contract No. 68-03-2088
Project Officer
William L. Brinck
Radiochemistry and Nuclear Engineering Branch
U. S. Environmental Protection Agency
Cincinnati, Ohio 45268
OFFICE OF RADIATION PROGRAMS
U. S. Environmental Protection Agency
Washington, D. C. 20460
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DISCLAIMER
This report has been reviewed by the Office of Radiation
Programs, U.S. Environmental Protection Agency, and approved for
publication. Approval does not signify that the contents necessarily
reflect the views and policies of the U.S. Environmental Protection
Agency, nor does mention of trade names or commercial products
constitute endorsement or recommendation for use.
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PREFACE
The Office of Radiation Programs of the U.S. Environmental
Protection Agency carries out a national program designed to evaluate
population exposure to ionizing and non-ionizing radiation, and to
promote development of controls necessary to protect the public health
and safety. This report was prepared in order to determine the natural
radioactivity source terms associated with radium in water supplies
and the radium removal efficiencies in water treatment processes.
Readers of this report are encouraged to inform the Office of Radiation
Programs of any omissions or errors. Comments or requests for further
information are also invited.
David S. Smith
Director
Technology Assessment Division (AW-459)
Office of Radiation Programs
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ABSTRACT
Numerous public water supply wells contain significant amounts of naturally
occurring radium 226. Because of the possible deleterious effects of
ingesting radioactive substances, methods of removing natural radium must be
considered.
A study was undertaken to determine the efficiency of radium removal using
conventional water softening methods. Five water supplies which were known
to have radium 226 in the raw water (ranging from 3.3 to 14.7 pCi/1) and which
have existing water softening equipment were chosen for the study. To
compare the relative efficiency of various methods of softening, plants using
ion exchange and lime softening were investigated.
At the plants using ion exchange softening, samples of raw, aerated, and
softened water were collected, analyzed for radium 226 and mineral content,
and the radium removal efficiency was calculated. Where applicable, samples
of filtered water were also included. At the plants using lime softening,
samples of raw and filtered water were analyzed. All plants were operated in
a normal manner during sampling.
In general, the ion exchange softening removed the radium 226 more efficiently
with 70.2 to 98.2% being removed as compared to 70 to 92% for lime softening.
Although the removal efficiency was somewhat lower using lime softening, it
was more consistent since the problem of breakthrough at the end of a softener
run was not experienced and little or no blend water is required to produce
a stable product.
Waste water, resin, and lime sludge were also analyzed to determine the radio-
activity concentration in the waste. Radioactivity in brine from the ion
exchange plants peaked at levels as high as 300 pCi/1 of radium 226. Samples
of the resins also indicated significant buildups. At the lime softening
plants it appears that most of the radium was precipitated in the sludge.
Satisfactory methods for the ultimate disposal of the wastes should be
determined.
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TABLE OF CONTENTS
Disclaimer ii
Preface iii
Abstract iv
Table of Contents v
Table of Contents - Appendices vi
List of Tables - Appendices vii
List of Figures - Appendices viii
Conclusions 1
Recommendations 2
1.0 SUMMARY OF OVERALL PROGRAM
1.1 Introduction 3
1.2 Objectives 3
1.3 Description of Facilities 3
1.4 Sampling and Analytical Procedures 5
1.5 Results and Conclusions 9
2.0 DWIGHT CORRECTIONAL CENTER
2.1 Introduction 14
2.2 Description 14
2.3 Sampling and Analysis 14
2.4 Radium Removal 15
2.5 Miscellaneous Chemical Data 18
2.6 Cost Data 18
3.0 PERU
3.1 Introduction 20
3.2 Description 20
3.3 Sampling and Analysis 20
3.4 Radium Removal 22
3.5 Miscellaneous Chemical Data 23
3.6 Cost Data 23
4.0 HERSCHER
4.1 Introduction 26
4.2 Description 26
4.3 Sampling and Analysis 26
4.4 Radium Removal 26
4.5 Miscellaneous Chemical Results 31
4.6 Cost Data 31
5.0 ELGIN
5.1 Introduction 33
5.2 Description 33
5.3 Sampling and Analysis 34
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5.4 Radium Removal 34
5.5 Miscellaneous Chemical Results 35
5.6 Cost Information 35
6.0 LYNWOOD
6.1 Introduction 38
6.2 Description 38
6.3 Sampling and Analysis . 38
6.4 Radium Removal 38
6.5 Miscellaneous Chemical Results- 40
6.6 Cost Information 40
APPENDIX A—Correctional 41
APPENDIX B--Peru 51
APPENDIX C--Herscher 68
APPENDIX D—Elgin 79
APPENDIX E--Lynwood 98
VI
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LIST OF TABLES
TABLE I Radium 226 Removal Efficiency of Plants Utilizing
Ion-Exchange Softening 11
TABLE II Radium 226 Removal Efficiency of Plants Utilizing
Lime Softening 11
TABLE III Reduction of Radium and Hardness--Dwight Correctional
Center 17
TABLE IV Reduction of Radium and Hardness--Peru 24
TABLE V Reduction of Radium and Hardness--Herscher 27
TABLE VI Reduction of Radium and Hardness—Elgin 34
TABLE VII Radium Reduction--Lynwood 39
APPENDICES
TABLE A-l Chemical Analysis Data--Dwight Correctional Center 49
TABLE B-l Chemical Analysis Data—Peru 66
TABLE C-l Chemical Analysis Data--Herscher 76
TABLE D-l Chemical Analysis Data—Elgin 96
TABLE E-l Chemical Analysis Data--Lynwood 106
Vll
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LIST OF FIGURES
FIGURE 1 Study Locations and Distribution of Sandstone Formation .... 4
FIGURE 2 Comparison of Wells Used for Radium Removal Efficiency Study . 6
FIGURE 3 Grain Sampler Used for Collecting Resin and Filter
Media Samples 7
FIGURE 4 Sampling Devices - Pumps Used for Collecting Waste Water
Samples 8
FIGURE 5 Exposure Rate Profile, Dwight Correctional Center,
Dwight, Illinois 16
FIGURE 6 Well Locations in Peru, Illinois 21
FIGURE 7 Exposure Rate Profiles, Herscher, Illinois 29
FIGURE 8 Concentration of Radium 226 - in Softeners Regeneration
Water, Herscher, Illinois 4/8/75 30
FIGURE 9 Radium 226 Level and Total Radium 226 vs. Regeneration
Water Used, Herscher, Illinois 4/8/75 32
FIGURE 10 Exposure Rate Profile, Lynwood, Illinois 41
APPENDICES
FIGURE A-l Scenes at Dwight Correctional Center Water Treatment Plant. . . 43
FIGURE A-2 Well Log-Well #2 - Dwight Correctional Center 45
FIGURE A-3 Dwight Flow Schematic 46
FIGURE B-l Scenes at Peru Water Treatment Plant 52
FIGURE B-2 Well Log-Well #5 - Peru 54
FIGURE B-3 Well Log-Well #6 - Peru 55
FIGURE B-4 Well Log-Well #7 - Peru 56
FIGURE B-5 Peru Flow Schematic 57
FIGURE C-l Scenes at Herscher Water Treatment Plant 69
FIGURE C-2 Well Log-Well #5 - Herscher 71
FIGURE C-3 Herscher Flow Schematic 72
FIGURE D-l Scenes at Elgin Water Treatment Plant 80
FIGURE D-2 Well Log-Well #1 - Elgin 82
FIGURE D-3 Well Log-Well #2 - Elgin 83
FIGURE D-4 Well Log-Well #4 - Elgin 84
FIGURE D-5 Well Log-Well #5 - Elgin 85
FIGURE D-6 Well Log-Well #6 - Elgin 86
FIGURE D-7 Elgin Flow Schematic 87
FIGURE E-l Scenes at Lynwood Water Treatment Plant 99
FIGURE E-2 Well Log-Well #2 - Lynwood 101
FIGURE E-3 Lynwood Flow Schematic 102
Vlll
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CONCLUSIONS
The main purpose, determining the radium removal efficiency of various
softening methods at both small and large water treatment facilities, was
achieved.
A study undertaken to determine the efficiency of radium removal by conven-
tional water softening methods indicated that both lime and ion exchange
softening were effective in removing the major portion of the radium from the
water. Lime softening gives more consistent removal since it is not subject
to the cycle of the ion exchange softener. Also, in lime softening the hard-
ness is not reduced to as low a level as in ion exchange softening. Conse-
quently, less unsoftened water is required to produce a satisfactory hard-
ness in the finished water.
Ion exchange softening, which is more practical for small communities, can
be used successfully if the plant is operated properly. Breakthrough of
the radium occurs at approximately the same time as the calcium. Therefore,
breakthrough can be detected by monitoring for hardness without the expense
of elaborate equipment for monitoring radium. In some cases it will be
possible to obtain blend water from a shallower aquifier, reducing the amount
of radium entering the distribution system.
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RECOMMENDATIONS
During the course of the investigation several questions were raised.
Further investigation as to the geologic formations which contribute radium
to the water would be helpful. If the radium is leaching from higher levels
than the sandstone, selective casing of the well might reduce or, in some
cases, eliminate the contaminant.
Disposal of waste from both ion exchange and lime softening plants should be
studies. Significant amounts of radium are being concentrated in both the
brine rinse and the lime sludges. These in turn are discharged into sewers,
directly into watercourses, or disposed of on land. Study of the uptake of
radium by growing plants would give an insight into the quantity of radium
which enters the food chain via this route.
An investigation into the economic feasibility of recovering minerals such as
radium, barium, and possibly magnesium from water plant waste, may lead to a
means of utilizing a waste product and eliminating a disposal problem. This
would apply not only to lime softening plants, but also to brine waste from
the regeneration of zeolite. From our limited information it appears that
the major portion of the radium is released from a zeolite softener over a
relatively short period of time. With information on the characteristic
curve of the release of the radium in the waste discharge, it appears that
the major portion of the radium could be collected from a relatively small
volume of waste.
Initial investigation indicates that exposure levels in water treatment
plants were not significant to employee safety. However, further investiga-
tion of the exposure level during cleaning of filters or changing of anthra-
filt and zeolite should be observed and investigated. The levels of radio-
activity to which employees are exposed under these circumstances should be
investigated to determine whether or not a hazard exists. Disposal of the
spent material is also a problem.
Water filtered through an anthrafilt iron filter showed significant reduction
in radium levels. Backwash water from this filter indicated that most of
the radium was removed from the filter. Further investigation is needed to
determine the form of the radium as it is pumped from the well and the
chemical changes which occur during preliminary water treatment.
The gross alpha data, in all cases, were considerably higher than can be
accounted for by the radium data. Further investigation to determine what
isotopes are present and their health significance would be helpful in
evaluating the effect on the consumer.
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1.0 SUMMARY OF THE OVERALL PROGRAM
1.1 INTRODUCTION
Naturally occurring radium 226 is found in numerous public water supply deep
wells serving Illinois communities in quantities above the levels recommended
by the 1962 Public Health Service Drinking Water Standards. Since radium
may be detrimental to the health of the population exposed, much concern
exists regarding the use of these wells for drinking purposes. In many
cases, these wells are the most suitable source for supplying water to the
community. Therefore, considerable interest in methods of radium removal
exists.
1.2 OBJECTIVES
The Illinois Environmental Protection Agency, under contract with the
United States Environmental Protection Agency, conducted a study on the
efficiency of radium removal using conventional water softening methods.
It was desired that as many softening methods as possible be studies. Where
possible, cost information on both capital investment and operating costs
were included.
1.3 DESCRIPTION OF FACILITIES
Five Illinois communities were selected for the study on the following basis:
1. Previous analyses of the water indicated either high gross alpha
activity or high radium 226 concentration.(1)
2. The water supply had existing water softening facilities.
3. Both small and large population groups should be represented.
The supplies selected were those serving the Dwight Correctional Center,
Herscher, Lynwood, Peru and Elgin. Of these, the supplies at Peru and Elgin
utilize the lime softening process and those at the Dwight Correctional
Center, Lynwood and Herscher use ion exchange softening. The Lynwood and
Herscher supplies use styrene-based zeolite while the unit sampled at the
Correctional Center uses natural green sand. The Peru and Elgin supplies
serve populations greater than 10,000. The other supplies serve much
smaller population groups, ranging from 250 to 4,000.
All of the water supplies studied lie in an area of the State in which the
sandstond formations (see Fig. 1) are sufficiently close to the surface to
(1) Lucas, Henry F., and Ilcewicz, F. H., "Natural Radium 226 Content of
Illinois Water Supplies," Journal AWWA 50:1523 (November 1958)
-3-
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LYNWOOD
OWIGHT CORRECTIONAL CENTER
The shaded section indicates
the area of the State in which
the sandstone formations are pene-
trated by deep wells. Frequently
these wells have elevated radiation
levels from naturally occurring
radium 226. \SLC*> Z~\ "^
Figure 1 STUDY LOCATIONS AND DISTRIBUTION OF SANDSTONE FORMATION
- 4 -
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be penetrated by wells. These aquifers provide an abundant supply of water
and are utilized by many communities. Work done by Grover H. Emrich
(Illinois State Geological Survey) and Henry F. Lucas, Jr., (Argonne National
Laboratories) indicates that the Glenwood-St. Peter sandstone contributes
significantly to the concentration of radium found in the water with the
radium content being low at the area of recharge and increasing down the
hydraulic gradient.T^) All of the supplies included in this study have wells
which are open to the St. Peter sandstone formation (see Fig. 2).
More recent investigations indicate that the radium may not be in the sand-
stone itself, but may be in the overlying shale. It is theorized that water
passing slowly through this less permeable layer, leaches the radioactive
material from the shale and carries it to the underlying sandstone aquifer.
1.4 SAMPLING AND ANALYTICAL PROCEDURES
Samples were collected from each location on three separate occasions at
approximately one-week intervals. The plants were operated in a normal
manner during this time. Samples of raw, aerated, filtered, and softened
water were collected so that any changes in the radium 226 content of the
raw water could be observed and the removal efficiency calculated. Diffi-
culties in collecting the softened water were experienced at both Peru and
Lynwood. At Lynwood, blending of softened water and raw water is done auto-
matically to maintain a predetermined level of hardness. This blending
occurs at the bottom of the softening unit, and no tap is available for
obtaining samples of the softened water only. Sampling devices are shown
in Figures 3 and 4.
Sampling of waste water presented a number of problems. In the lime
softening plants, an attempt was made to obtain a composite sample using
small pumps during backwashing of the filters. Frequent clogging occurred
because of the heavy solids in the water. Because of this, it was necessary
to go to a manual method which made it difficult to get a representative
sample during the entire backwash cycle. At the zeolite plants, some means
of determining the exact time when the radium is released from the softener
is important. It was learned through a special sampling program at Herscher,
that radium levels peak during brine rinse and then drop off rapidly.
Unless samples are collected at the same point in the cycle it is impossible
to make a meaningful comparison of radium being removed by the ion exchange
softener during each cycle. A curve developed from numerous samplings
taken during regeneration would be necessary to determine the actual amount
(2) Emrich, Grover H., Lucas, Henry F., "1968 Geologic Occurrence of Natural
Radium 226 in Ground Waters in Illinois," International Association of
Scientific Hydrology-VIIIe Annee No. 31963, pp. 5-19.
-5-
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+300 ELGIN ELGIN ELGIN ELGIN ELGIN HERSHEJt DWIGBT LYBWOOD PERU PERU PERJ
WELL 01 WELL 0 2 WELL 03 WELL 05 BELL 0 f. WELL 05 WELL 02 WELL III WELL 05 BELL K BELL 07
+200
177 1-"
+100
0
-100
-200
-300
L 177.7
Limestone
- 55.2
St. Peter
- 11.9
Limestone
- -42.4
Sandstone
- -63.7
- -94.2
Sandstone
- -170.4
.imestone
- -185.6
Sandstone
~ -210.0
.imestone
- -255.7
Sandstone
- -277.1
Potsdam
Sandstone
- -322.8
'otsdam
Sandstone
- -347.2
*- -367.0 1
Potsdam /
— 226.5 -
- 178.3-
Limestone
- 55.2
- 11.9
,imestone
- -42.4
iandstone
- -63.7
--94.2
Sandstone
- -170.4
,ime stone
--185.6
iandstone
"-210.0
,imestone
--255.7
lands tone
--277. 1
'otsdam
iandstone
--322.8
'otsdatn
iandstone
"-347.2
-* —
-363.3
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Dri'ft W" Drir't W"r>rifr
- 214-3 |- 21*'9 I 2 ro 3
• I _- 198.1
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- -42 4 >--42.4
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- -63.7
- -70.1
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- -94.2 c y'J
Sane stone
Sandstone
- "^-S, - -146.3
- -170.4 Shale '--170.7
Limestone
-197.5
Drift
•164.0
Coal
Measures
-86.9
Maquoketa
-51.2
Galena
Dolomite
- -6 7
Plattville
Dolomite
- 36 . 6J
--64.6
St. Peter
Sandstone
--168.6
~ -185.6
Sandstone
~ -210.0
Limestone
- -255.7
Sandstone
~ -277.1
Potsdam
Sandstone
322 8
Potsdam
Sandstone
-346.0
r 187.5
Drift
165.2
,imestone
md Shale
- 3.4
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ind Shale
-~32.9
Limestone
- -132.6
St. Peter
Sandstone
-170.7-
'-174. 4
Limestone
- -267.6
Limestone
-316.1
- -364. 5^
Limestone' Limestone'
—400
—500
— 600
•140.2
Pennsyl-
vanian
21.3
Silurian
--109.7
Maquoketa
--158.5
- -166.4-
Galena
Plattville
- -276.5
St. Peter
Sandstone
• -320.0
• -373.4
New Rich-
mond Sand-
stone
' -413.0
Oneota
Dolomite
--472.4
Trempeleau
Dolomite
- -544. 1
Franconia
- -588.3
GaLesville
Sandstone
--644 7
164.6
.•
Pennsyl-
vanian
-11.9
Dolonzite
Waukesha
--42.7
Joliet
)olomite
-9 370
-112 . 5
Lankakee
Dolomite
laquoketa
-160.0
-195.7-
Galena
Plattville
--278.9
lenwood
Sandstone
"-306.0
--321.3
St. Peter
Shakopee
Dolomite
--374.3
New Rich-
mond Sand-
stone
--414.5
Oneota
Gunter
Dolomite
--462.3
--486.2
Trempea-
leau
Doloirite
--532.8
Franconia
--586. 1
Ironton
Sandstone
--631.2^
-643 r*~
140.2
Shale
89.6
Limestone
and Shale
mond Sand-
stone
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-404.5
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Calesville
Sandstone
{,!:£. 1
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< ••"!• : .',!>,, i-o, »t >'• 'I -" 1'" hau Claire^ Fau Claire1 ~D"'-D 1
;,ui,i' U«,« il t 1 i ' I' Eau Clairel
v,,uli Galesville
Sandstone J
!~700
- 6 -
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Figure 3 Grain Sampler Used For Collecting Resin & Filter Media Samples
-7-
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Figure 4 Pumps Used For Collecting Waste Water Samples
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of radium discharged to waste. Without this information it is impossible to
develop a mass balance of the radium going through the plant.
In an effort to correlate radium with other naturally occurring elements,
mineral and trace metal analyses were done on all raw water samples.
Analyses of wastes coming from the plants were also done to determine where
the radium removed from the water was being discharged. Radium analyses
were performed by Argonne National Laboratories using the radon emanation
method. Resin samples were also analyzed by gamma-ray spectrometry using a
Ge-Li detector. Duplicate analyses were done on 29 samples to ensure quality
control. All sampling containers were prepared by Argonne Laboratories
using disodium EDTA as a preservative to prevent plating of radium on the
container walls during transport to the laboratory.
A limited number of samples were analyzed for both radium 226 and radium 228
by the United States Environmental Protection Agency. The samples were
analyzed by gamma spectrometry using a Ge-Li detector.
All mineral, trace metal, and gross radiation analyses were performed by the
Chicago section of the Illinois Environmental Protection Agency Laboratory.
All testing was done in accordance with the Agency's quality control program.
Under this program, every seventh sample is diluted (90% sample, 10% water)
with deionized water and run as a duplicate to determine the precision of
the analysis. Double deionized water is used as the diluent for the trace
metal samples.
Disposable containers were supplied by the laboratory for all sampling. In
order to ensure that the sampling containers were free of contamination,
each lot underwent a quality control check. This check consisted of adding
distilled water and preservative to the container, and performing all analyses
on the water.
Preservatives were added to the sampling containers, where necessary, to
prevent change in the sample while in transit to the laboratory. Redistilled
nitric acid (20 ml of !:!/-?. of sample) was added to the sample for trace
metal analysis to prevent plating of the metals on the walls of the container.
Sodium hydroxide (I ml of 5N/6 oz. sample) was added to the samples used for
cyanide analyses. This was sufficient to maintain this portion of the sample
at a pH of 12. All samples were refrigerated during transport to minimize
changes in alkalinity and nitrate.
The gross radioactivity of the samples was determined by counting with an
internal proportional counter. The counting error was determined at the
95% confidence level.
1.5 RESULTS AND CONCLUSIONS
The removal of radium, in general, was good for both ion exchange softening
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and lime softening. It does appear that ion exchange softening removes with
a greater efficiency than lime softening, if the unit is regenerated as soon
as calcium and magnesium begin to break through.
The removal efficiency of the ion exchange plants ranged from 70.2% to 98.2%.
The efficiency at Dwight Correctional Center, which has a natural green sand
unit, does not appear to be as high as the others, when figured as a percent-
age. In all cases, however, the radium 226 leaving the softener unit is less
than 1 pCi/1. The plant at Lynwood (styrene-based zeolite), which has an
automatic regeneration system,has the most consistently satisfactory removal.
The softeners in this plant automatically regenerate as the hardness of the
water begins to increase. As a result, the plant is always operating with
a freshly regenerated zeolite unit. Starting with a radium 226 concentra-
tion of approximately 15 pCi/1, the highest concentration leaving the
softener unit was 0.77 pCi/1.
At Herscher (styrene-based zeolite) significantly greater quantities of
radium passed through the softener at breakthrough. In all samplings,
greater than 2 pCi/1 of radium was passing into the softened water at the
end of the cycle. This could undoubtedly be overcome by more frequent regener-
ation.
The efficiency of radium removal appears to change as the cycle progresses.
Although additional sampling would be required to reach a definitive answer,
it appears that both green sand and styrene-based zeolite remove most
efficiency at the midpoint* of the softener run. The apparent poor quality
of removal at the beginning of the cycle should, however, be investigated
further. Since the samples were collected immediately after regeneration,
the slightly higher radium results may be due to incomplete rinsing, rather
than to less complete removal. Samples representing the start of the cycle
could be controlled by monitoring chloride content of the water and
collecting samples only after normal background levels are reached. Radium
begins to break through the softener at about the same time as the calcium
and magnesium. The age of the resin should also be considered. The unit
studies at Lynwood, which shows the highest efficiency, has been in use for
about two years. Both of the other plants are using resin which has been in
the softeners for ten or more years. The removal efficiency is shown in
Table I.
The lime softening plants at Peru and Elgin did not remove radium 226 as
efficiently as the ion exchange softening units. The removal efficiencies
ranged from 70% to 92%. In general, the plant at Peru did not function as
well as the plant at Elgin. Both plants have similar levels of radium 226
in the raw water (6-7 pCi/1). The softened water at Peru had a radium 226
*"The term midpoint is used throughout this report to indicate during the
cycle run.
-10-
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concentration greater than 1 pCi/1 (1.33-1.62) while the level in the
softened water at Elgin was consistently less than 1 (see Table II).
TABLE I. RADIUM 226 REMOVAL EFFICIENCY OF PLANTS UTILIZING ION-EXCHANGE
SOFTENING
First
Sampling
(percent)
Dwight Correctional Center
Regenerated 88.9
Mid-point 96.0
Near breakthrough 98.2
Herscher
Regenerated
Mid-point
Near breakthrough
Lynwood
Regenerated
Mid-point
Near breakthrough
92.0
97.2
85.4
97
98
97.3
Second
Sampling
(percent)
88.4
92.7
70.2
95.3
97.8
84.5
97.0
97.6
96.5
Third Average
Sampling Removal
(percent) (percent)
91.6
90.6
83.7
86.0
95.7
83.8
94.7
98.2
98.2
89.6
93.1
84.0
91.1
96.9
84.6
96.3
98.0
97.3
TABLE II. RADIUM 226 REMOVAL EFFICIENCY OF PLANTS UTILIZING LIME SOFTENING
Peru
pH
10.2
8.4
First
Sampling
(percent)
92.0
89.9
Second
Sampling
(percent)
70.0
86.0
Third
Sampling
(percent)
75.7
87.8
Average
Sampling
(percent)
79.2
87.6
Blending the water to reach a satisfactory hardness in the distribution
system raises the levels of radium which reach the user. Because lime
softened water is not reduced to near zero hardness, little or no blend
water is required to produce a stable product. In this study, however, both
extremes of blending were observed. At Elgin all water is softened so that
the figures for softened water represent water going to the distribution
system. At the other extreme, water at Peru is blended with raw water at a
high ratio (40% raw, 60% softened). Consequently, levels of radium going
to the user are notably increased at Peru.
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The near zero hardness of the zeolite-softened water requires that either
unsoftened water or artificial hardness be added to prevent corrosive action
in the distribution system. In order to avoid adding significant quantities
of radium to the softened water, it may be possible to look for wells in a
shallower aquifer to use for blend water. While the production from such a
well would not be sufficient to supply the communities water needs, it may
be sufficient to supply the blend water.
It should also be noted that the anthrafilt pressure filters at Herscher
removed significant quantities of radium 226 before the water went to the
zeolite softener. From 48 to 56% of the radium was removed by this step in
the treatment process. Exposure profiles of these tanks developed during
the field survey further verified that considerable quantities of the radium
were retained in this process.
Careful consideration should be given to the disposal of the radium waste
from the plant. Presently, most, water plant waste is either discharged to
a sewer, or directly to a receiving stream. Analysis of the wastes indicate
that sizable quantities of radium (up to 300 pCi/1) are being released in
the waste water. The advisability of discharging such waste to the sewer
should be reviewed.
Lime sludge coming from the plants at Peru and Elgin contained a considerable
concentration of radium-226. Samples of both the sludge and the blow-off
sludge blanket were collected in order to determine if any differences in
the radium content occurred. Results were inconclusive. At Peru, all concen-
tration values are essentially the same regardless of the point of collection.
At Elgin, two samples taken from the sludge blanket contained significantly
lower concentrations of radium (1.26 _+_ 0.0 and 3.15 +_ 0.09 pCi/g) while one
sample had a relatively high level (12.53 +_ 0.19). Samples taken from the
lagoon appeared to have higher concentrations (6.01 +_ 0.18 and 30 +_ 2 pCi/g).
It appears that the characteristic deposit of radium in the sludge varies from
plant to plant and is probably dependent on the mineral content of the water.
Considerably more study involving a number of lime softening plants would be
required to determine what characteristics of the mineral content of the
water affect the removal of radium.
Ultimate disposal of lime sludge also presents a serious problem. Although
the actual amount of radium in each gram of sludge is very small, the total
amount discharged becomes rather large. Each plant uses several thousand
kilograms of lime each month. This amount is significantly increased by the
calcium and magnesium precipitated from the water. Returning the sludge to
a watercourse may result in sufficient dilution to avoid a significant
problem. However, if the velocity of the stream is insufficient to disperse
the sludge, it may settle out and produce a build up of radioactive waste
on the stream bottom. Land disposal may present an even more serious problem
if the concentrated radium builds up in a small area. The possibility of
take-up by plants growing in soil treated with this lime sludge should be
-12-
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studied to determine whether or not radium is entering the food chain.
The studies have also indicated that considerable radium is retained in the
zeolite and in the anthrafilt. A field survey of the plants studied shows
that this does not present a hazard to personnel working in the plant under
normal conditions. It may, however, present a sizable reservoir of radio-
active material if it becomes necessary to remove these media from the tanks
for replacement.
Exposure levels at each plant were studied during a field survey. In
general, the exposure levels were insignificant except in the immediate
area of the filter tanks or softeners. At Elgin, one sand filter that had
been drained for maintenance was observed to have significantly increased
exposure rates near the surface of the sand. It was felt that this did not
constitute a hazard to the workmen since they were exposed for only short
periods of time.
Other trace elements are also concentrated in the lime sludge. This was
evident in the build up of barium in the sludge at Elgin. The water at
Elgin contains significant amounts of barium which are removed by the
softening process and precipitated into the sludge.
-------
2.0 DWIGHT CORRECTIONAL CENTER
2.1 INTRODUCTION
The Dwight Correctional Center is a state owned institution located in
Livingston County about two miles west of the village of Dwight (see Fig. 1).
This system serves a population of about 235. The average daily pumpage is
112.4 m3 (3 x 104 gpd).
2.2 DESCRIPTION
All water which was pumped through the system during this study was from
well #2. This well was drilled in 1948 to a depth of 366 m. The well is
cased with a 53-cm drive pipe from 0 to 27.8 m. Inside this, there is a
30-cm casing from 0 to 42.7 m, and a 25-cm casing from 42.7 to 155.4 m.
A 38-cm liner extends from 78 m to 128 m.
The water is aerated, primarily for hydrogen sulfide removal. The aerator
is a coke tray unit consisting of four trays, 2.81 m2 each, with a total
area of 11.3 m2. Water is passed through the unit at an approximate rate
of 58.1 m3/day.
The supply has two pressure ion exchange softener units which are 1.83 m in
diameter and 2.13 m tall. The rated capacity is 151.4 m^/day. The units
were originally installed in 1944. They were rebuilt in 1954 and new gravel
and zeolite added. At that time, the units were filled with a natural green
sand ion exchange material obtained from the Elgin Softening Company. Since
then, one unit has been replaced (1964) with the new unit having styrene
based zeolite. The softeners are used on an alternate basis so that one
unit is recharged each day. In order to test the radium removal efficiencies
of as many materials as possible, the unit containing the natural green sand
was chosen for this study.
The water is further treated by the addition of caustic soda and sodium
silicate for corrosion control before passing to the distribution system.
Approximately 10% aerated water is blended with the softened water. See
Appendix A for detailed description of the facilities and equipment at the
Dwight Correctional Center.
2.3 SAMPLING AND ANALYSIS
Samples were collected from this supply on February 4 and 5; 13 and 14; and
19 and 20, 1975. Raw, softener influent (aerated) and softener effluent
samples were collected immediately after regeneration of the softener, at
midpoint in the cycle and at breakthrough. An additional composite sample
of the waste water was also collected. The approximate composition of the
waste water is as follows:
-14-
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Backwash water 3,078 liters
Brine 923 liters
Rinse water 10,206 liters
The waste water sample was composited by placing a sump pump into the pit
where the waste is discharged.
A sample of the green sand was also collected. The port on these softeners
is located on the side of the unit, making it very difficult to sample at
any great depth. Consequently, the sample was collected at a depth of only
22.9 to 30.5 cm below the surface. Analyses for radium were done by both
Argonne National Laboratory (ANL) and the United States Environmental
Protection Agency laboratory. Considerable variation in the results was
noted, ranging from 28.66 +_ 0.46 pCi/gm (ANL) to 46.4 +_ 5.5 pCi/gm (USEPA).
Argonne attempted to extract the radium from the resin using hydrochloric
acid and EDTA. The acid extracted sample gave a radium 226 content of
34.22 +_ 0.55 pCi/gm compared to 28.66 +_ 0.46 pCi/gm from the EDTA extraction.
The sample analyzed by the USEPA was done by gamma-ray spectrometry using a
Ge-Li detector.
A gamma scan of the resin conducted by ANL indicated the presence of both
thorium 228 and radium 228. The radium 228 is apparently in excess, in
contrast to the ratio which is normally expected for transient equilibrium.
Analyses for radium 228 in the USEPA laboratory by gamma-ray spectrometry
and a Ge-Li detector indicated a concentration of 59.0 +_ 2.2 pCi/gm.
The exposure rate vertical profile on the side of the green sand tank
indicated a maximum level of 29 yR/hr near the center of the tank (see
Fig. 5). The samples were collected considerably above this in an area of
the tank which indicated a rate of 20 to 23 yR/hr.
Exposure rates measured at other locations within the plant were 7.0 +_ 1.0
yR/hr above a natural background rate, outside the plant, of 6.7 yR/hr.
2.4 RADIUM REMOVAL
The radium data indicate that the radium content of the raw water is fairly
constant, ranging from 3.12 +_ 0.09 pCi/1 to 3.46 +_ 0.10 with an average of
3.26 +_ 0.12. The radium 226 content of the softened water was low, ranging
from 0.056 to 0.98 pCi/1. The average radium content was 0.36 +_ 0.27 pCi/1.
The finished water going to the distribution system is a blend of 90%
softened water and 10% aerated water. Assuming that no radium is lost during
aeration, the calculated radium 226 content for the blended water would
range from 0.36 to 1.23 pCi/1. Reduction of the radium 226 by the natural
green sand unit is shown in Table III.
Comparing the three samplings, there is no clear cut indication of when the
-15-
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softener is most efficient. During the first two samplings, it appears to
be more efficient at the midpoint than at the beginning of the softener run.
During the second and third sampling, breakthrough of radium was occurring
at the end of the softener run. More frequent sampling would be required
to determine just when breakthrough occurred.
The gross alpha activity is much higher than the activity attributable to
the radium content, and also showed considerably more variation from sample
to sample. The range on the raw water samples was from 9.4 to 43.2 pCi/1.
It appears that the aerator"is removing a considerable part of the radio-
active materials.
Radium 226 analyses were not done on the aerated water samples. Further
study should be done to determine whether or not the coke bed itself may be
retaining a portion of the radioactive material.
2.5 MISCELLANEOUS CHEMICAL DATA
While not directly related to this study, the fluoride data show an unusual
phenomenon. The fluoride content of the raw water is consistently 1.4 to
1.5 mg/1. Immediately after regeneration, the fluoride is sloughed off of
the green sand in the softener and the fluoride content of the softened
water is quite high ranging from 3.4 to 4.8 mg/1. By midpoint in the cycle,
the fluoride is again being retained in the softener and the softener
effluent has a fluoride content, of 0.9 to 1.4 mg/1. At the end of the cycle,
the fluoride content of the softened water had decreased to 0.5 to 0.6 mg/1.
Very little of the fluoride is released at regeneration, with the waste
water containing only 2 to 2.5 mg/1. Potassium is also tied up in the
softener, with breakthrough occurring at approximately the same time as the
calcium breakthrough.
All chemical and radiological data are included as Appendix Table A-l.
An attempt at a material balance of the radium 226 proved unsuccessful.
Since the radium is apparently released from the softener at an uneven rate,
the composite of the waste water was not representative of waste coming off.
Further studies, which would include numerous samples taken during the
backwash, brine, and rinse cycles would be required to give a value of the
actual amount of radium 226 being discharged into the waste stream.
2.6 COST DATA
Cost figures on the initial installation and on salaries are not available.
However, it is estimated that the operator spends 1.5 hr/day in actual water
plant operation.
The chemical and electrical costs on a daily basis for operation of the
-18-
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plant are as follows:
Salt 609 kg @ $.0343/kg $20.88
Sodium silicate 3.27 kg § $ .187/kg .61
Caustic soda 1 kg @ $ .04/kg .04
$21.53
It is also estimated that electrical costs for pumpage averages $2.00/day.
Based on a plant capacity of 112.4 m^/day, the chemical and electrical costs
are about $0.78/1000 gal.
-19-
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3.0 PERU
3.1 INTRODUCTION
The city of Peru, located along the Illinois River in LaSalle County has an
estimated population of 12,400 people (see Fig. 1). The water treatment
plant which is presently in use, was put into operation in 1932. Presently,
the average daily pumpage being processed at this plant is 6,832 m^
(1.8 x 105 gpd).
3.2 DESCRIPTION
Water is drawn from three deep wells, aerated, treated with lime and sodium
aluminate at a pH of 8.4, clarified, settled, recarbonated, chlorinated and
filtered before being pumped to the distribution system.
Well number five was drilled in 1931, and is located two blocks west of the
filtration plant. The well is cased from the surface to 312.7 m. From
312.7 m to 450.5 m there is a 38 cm open rock hole. A 42.5 cm liner was
placed between 450.5 m and 492.5 m. The balance of the well is open.
Radium 226 analyses of the water samples collected were 4.57 and 4.78 pCi/1
with the average being 4.68 pCi/1.
Well number six, located on a bluff above the plant at Plumb and Center
Streets, was drilled in 1952 to a depth of 82.3 m (see Fig. 4). The radium
226 content of this well was 3.08 and 3.73 pCi/1 and averaged 3.41.
Well number seven, located on the north side of Water Street near the foot
of West Street, was drilled in 1963 to a depth of 789.7 m (see Fig. 6). It
is cased to a depth of 335.9 m and is open for the rest of the depth. The
drillers log is not as detailed as the logs for Wells number five and number
six. However, because of the proximity of the wells, it can be assumed that
the geologic formation would be very similar. The radium 226 content
averaged 6.07 pCi/1 which is considerably higher than the levels found in
the other wells. During the time of sampling, this well was being used as
the major source of water.
See Appendix B for detailed description of the facilities and equipment at the
Peru waterplant.
3.3 SAMPLING AND ANALYSIS
Samples of raw, aerated, and filtered water for mineral, trace metal, and
radium analyses were collected on February 20, 25, and March 4, 1975.
Inadvertently, the samples of filtered water collected on February 20 and
25, 1975, were actually blended water as it was going to the distribution
system. To compensate for this error, an additional sample of filtered
-20-
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-21-
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water was collected on March 19, 1975.
Samples of clarifier sludge from the blow-off well and backwash water were
also collected and analyzed for radium content. The backwash sample was
collected by using either a sump pump or "SKIL" drill pump. Approximately
19 liters of the dilute slurry were pumped from the settling tank and were
allowed to settle, and the supernatant liquid poured off, leaving the solids,
The sludge sample was collected from the sludge pit manually with a scoop.
This plant has three filters, each with an area of 15.6 m^. The filter
medium is composed of anthracite, sand, and gravel. Over the years, the
anthracite has become completely encrusted with what appeared to be a lime
scale. An analysis of a sample of the filter media conducted in the
Illinois EPA laboratory indicated that the material contained 29% calcium
and 0.2% magnesium. Analysis for gross radioactivity indicated an alpha
activity of 116.0 +_ 41.4 pCi/gm and a beta activity of 116.3 +_ 24.6 pCi/gm.
Analysis of a sample collected during a plant visit indicated a radium 226
content of 4.6 +_ 1.3 pCi/gm and a radium 228 concentration of 3.6 +_ 0.4
pCi/gm. ~ ~
The filters are backwashed once each day at a rate of 7570 1/min. for a
period of three minutes. Radium analyses of composite samples of backwash
water show considerable variation with the range being 9.65 pCi/1 to 87.7
pCi/1. Presumably, the method of sample collection was responsible for this
wide variation. Because of clogging of the pump, it was extremely difficult
to accurately composite the sample during the entire backwash cycle.
Samples of the lime sludge were collected on February 19 and 25, and
March 4, 1975, from both the sludge pit and from the blow-off sludge to
determine whether or not the radium value was consistent in the various
fractions of the sludge. There was no appreciable variation in the radium
results on the sludge samples with the radium 226 content ranging from
8.84 to 9.31 pCi/gm with an average of 9.06 pCi/gm.
Sludge samples were also collected on March 18 and analyzed by the United
States Environmental Protection Agency using gamma-ray spectrometry with
a Ge-Li detector. The concentration of radium 226 was 3.9 +_ 1.0 pCi/gm
and of radium 228 was 3.1 +_ 0.3 pCi/gm.
3.4 RADIUM REMOVAL
The softening process reduced the radium 226 by 70.6 to 92.4%. Since
samples were collected from the individual wells on February 25 and March 4,
1975, the radium 226 content of the raw water was calculated on the basis
of pumpage from each well.
-22-
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During the first two samplings, samples were taken of the blended water
rather than from the softened water. The content of the softened water was
calculated from the blend ratio. Values and reduction are indicated in
Table IV.
The radium content of the blended water is quite consistent and averages
2.94 pCi/1 of radium 226 which is going to the consumer.
Exposure rates at the plant indicated no measurable increase above back-
ground, except for an area above the clarifier sludge pit and near the
aerator where there were quantities of fly ash from the adjacent coal fired
power station. Levels near the aerator were 20 yR/hr and above the sludge
pit, 3 yR/hr above background. Natural background exposure was about 10
yR/hr.
3.5 MISCELLANEOUS CHEMICAL DATA
Mineral analyses of the three wells indicate that the water from well number
seven is somewhat higher in total dissolved mineral content than the other
wells with the major difference in the chloride content. As previously
noted, the radium content is also higher. At the time of sampling, 78 to
87% of the water being processed at the plant was coming from this well.
Heavy pumping of this nature could influence the quantity of water being
drawn from a given portion of the aquifer and thus directly influence the
mineral character of the water.
Trace metals are negligible, with the possible exception of barium which is
present in very small quantities in nearly all of the raw water samples.
All chemical and radiological data are available in Appendix Table B-l.
3.6 COST DATA
Cost figures for the plant and equipment are not available. Power and
maintenance costs are combined with other city utilities and cannot be
separated with accuracy.
Chemicals used at the plant over a period of twelve days were:
Lime 18,273 kg
NaAlO (Dearborn 502
alkaline coagulant) 680 liters
for an average daily use of:
Lime 1,523 kg
NaAlO 56.7 liters
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of 6,832 m3/day, the chemical costs are about $0.04/1000 gal.
-25-
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4.0 HERSCHER
4.1 INTRODUCTION
The village of Herscher is located in the west central part of Kankakee County
(see Fig. 1). The estimated population served by the public water supply is
1,000 with the average daily pumpage being 379 nr> (1 x 10^ gpd).
4.2 DESCRIPTION
The present water treatment facilities were placed in operation in 1965. The
water is aerated, settled, chlorinated, filtered, treated with polyphosphate
and potassium permanganate, softened, and pumped to the distribution system.
Water used for this =tudy was obtained from well number five, drilled in 1953
to a depth of 240.5 m. The well is cased from 0.46 m above the floor level
to a depth of 199.3 m. At that point, sandstone was reached.
The aerator is 1.11 m^ and 3.65 m high, steel coated with plastic and has
steel baffles. A blower forces air up through the falling water. It is
located above a 4.3 x 4.9 x 3 m collecting reservoir. The water is filtered
through an anthrafilt filter before passing to the softener. The pressure
filters are 1.8 m in diameter a~nd 1.5m high and have a total capacity of
567 1/min. The filters are backwashed twice a week.
From the filters, the water is passed to the zeolite softener. The softener
is 1.67 m in diameter and 2.13 m high and contains 2.4 m^ of styrene-based
zeolite.
See Appendix C for detailed description of the facilities and equipment at
the Herscher water plant.
4.3 SAMPLING AND ANALYSIS
Samples were collected on March 25, April 1, and April 8, 1975. Samples of
raw water, filter influent, filter effluent, and softener effluent were
collected immediately after regeneration, at mid-point in the cycle, and near
breakthrough.
4.4 RADIUM REMOVAL
Radium content of the raw water was relatively constant, ranging from 13.95 to
14.94 pCi/1 with the average being 14.34 +_ 0.37.
Reduction of the radium 226 is illustrated in Table V.
Removal of radium by aeration was unpredictable. In one case a reduction of
-26-
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- 27 -
-------
12.3% was noted, while in others, no removal or even a slight increase was
indicated. Since these samples were taken from the collecting reservoir,
the amount of suspended material in the sample may vary from one time to
another. To fully evaluate this step of the treatment process, the water
would require filtering at the time of sampling.
Water at Herscher has a very high level of hydrogen sulfide. It is treated
with potassium permanganate after aeration to further aid the control of odor.
The anthrafilt filters are designed to remove any insoluble sulfur compounds,
rather than for iron removal. Approximately 50% of the radium is removed by
filtration through the anthrafilt. The efficiency of the filter appears to
remain nearly constant throughout the filter run.
Since considerable radium 226 is found in the filter backwash water, most of
the radium is probably removed by physical filtration. Potassium permanganate
is used to oxidize the sulfide prior to filtration. If the radium is in a
soluble form when pumped from the well, it could combine with the oxidized
sulfur to form insoluble radium sulfate.
Exposure rate profiles vertically on the side of the filters (see Fig. 7)
indicate that the highest concentration of activity is approximately 0.6 meters
from the bottom of the tank. A sample of anthrafilt was collected from
approximately 0.762 m below the surface of the medium. Analysis of the sample
indicated a radium 226 concentration of 111.6 +_ 3.4 pCi/gm and a radium 228
concentration of 38.9 pCi/gm.
The radium 226 is further removed in the zeolite softener. The efficiency
of the softener is greatest at the midpoint of the cycle with 90.6 to 93.9%
removal. Near breakthrough,the efficiency of removal is reduced to about
64.5%. At this point, 22 to 42% of the calcium and 76 to 100% of the magnesium
are also passing through the softener, indicating that the softener should
have been regenerated sooner, and that breakthrough had already occurred.
Wastewater coming from the filters and softener contains considerable quantities
of radium. The average radium 226 content of the filter backwash water was
150 pCi/1. From 17,000 to 28,000 liters of water are put through during each
backwashing of the filter. It is impossible to determine the exact amount of
radium removed from the filter, since the method of compositing the sample
may not be accurate.
A special group of samples of waste water from the softener regeneration cycle
was collected on April 8, 1975. During this regeneration cycle, samples were
collected at approximately six minute intervals with the first sample being
collected seven minutes after the start of the brine phase and continuing
until the end of the fast rinse cycle (see Fig. 8). For the first 26 minutes
of the cycle, the radium 226 concentration in the waste water remained' approxi-
mately constant or even decreased slightly. From 26 minutes to 43 minutes,
the concentration rose sharply, peaking at 315 pCi/1. From this point on
-28-
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- 29 -
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- 30 -
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through the remainder of the cycle, the concentration decreases rapidly.
Figure 8 was plotted based on time; however, since there are different flow
rates for each phase of the regeneration cycle, this gives a somewhat
distorted view. Therefore, the data were replotted in Fig. 9 with radium con-
centration versus wash water used. From this curve, the calculated radium 226
concentration in the 16,000 liters of waste water was approximately 54 pCi/1
for a total of 0.864 pCi of radium 226 removed.
Using the sample analysis of the composite regeneration waste, the average
radium 226 concentration was 79.3 pCi/1 for a total of 1.30 pCi of radium 226
removed. Using the average values of the softener influent and effluent and
an average of 250,000 liters between regeneration, the total radium 226
removed is calculated to be 1.25 pCi. As can be seen from these figures,
more accurate data concerning the quantity of the water filtered, quantity of
regenerated water, and levels at which radium 226 comes out in the waste
water are needed.
Eighteen percent filtered water is blended with the softened water to produce
a satisfactory hardness in the distribution system. This would result in an
average concentration of 2.37 pCi/1 of radium 226 reaching the water user.
4.5 MISCELLANEOUS CHEMICAL RESULTS
The overall water quality of both the raw and finished water at Herscher is
somewhat poor. The raw water is highly mineralized, having a residue of 1450-
1500 mg/1. Both the chlorides and the sulfates are higher than desirable for
an esthetically pleasing water. The natural sodium is high enough to be
unsatisfactory for persons on a sodium-restricted diet. Softening the water
by means of ion exchange increased the sodium to an even higher level.
Barium was present at 0.2 mg/1. No other metals of any significance were
found.
All chemical and radiological data are included in Appendix Table C-l.
4.6 COST DATA
No cost data were available from this plant.
-31-
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5.0 ELGIN
5.1 INTRODUCTION
The city of Elgin, located in Kane County (see Fig. 1) has a population of
of 58,000. Water for the city is processed in three separate treatment
facilities. The Slade Avenue Plant and the West Side Plant both utilize lime
softening, while the St. Charles Plant has zeolite softening. Radioactivity
levels of the water which feeds the Slade Avenue Plant are much higher than
those which go to the West Side Plant. Therefore, even through the facilities
are much older than the West Side Plant, the Slade Avenue Plant was chosen for
this study. Approximately 25,000 people are served by this plant.
5.2 DESCRIPTION
The original Slade Avenue water plant was built in 1887-1888 and was designed
to process water from the Fox River. Because the river water was of such poor
quality, wells were drilled in 1904. Portions of the old plant and the wells
that were drilled at that time are still in use. The softening units were
added in 1937.
Wells which were in service at the time of sampling were wells number one,
number two, number three, number five, and number six. Well number one was
drilled in 1904 to a depth of 656.2 m. It was opened to a depth of 638.12 m
in 1945 and reopened to that depth in 1960. Casing records indicate that it
is cased to a depth of 177.09 m. It is located at the south end of the
treatment plant.
Well number two, located on the west side of the treatment plant, was drilled
in 1904 to a depth of 426.51 m. In 1924 it was deepened to 639.76 m and in
1946 it was further deepened to 644.69 m. It was reopened to 634.84 m in
1946. The well is cased to 177.70 m.
Well number three, located about 98 m north of the treatment plant was also
drilled in 1904. The original depth was 426.51 m, but was deepened to 643 m
in 1924. In 1961 it was reported to be 588.25 m deep. It is cased to a
depth of 178.31 m.
Well number five, drilled in 1949 to a depth of 411.75 m, is located about
164 meters south of the plant. It is cased to a depth of 186.23 m. Well
number six, also located south of the plant, was drilled in 1958 to a depth
of 426.51 m and is cased to a depth of 136.09 m.
Water from these wells is discharged into a raw water reservoir and then pumped
to two air diffusion type aerators to remove the hydrogen sulfide. Lime and
ferrous sulfate are added in the mixing basin. The pH is raised to 10.2
during treatment. The water is allowed to settle before filtering through
-33-
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rapid sand filters. See Appendix D for detailed description of the facilities
and equipment at the Elgin plant.
5.3 SAMPLING AND ANALYSIS
Samples to determine the radium removal efficiency of this plant were collected
on March 7, 14, and 21, 1975. Although the wells are drilled in close
proximity and, in general, the mineral data are similar (see Appendix Table D-l),
the radium and barium levels are significantly higher in well number six.
5.4 RADIUM REMOVAL
The radium is removed by the softening process as follows:
TABLE NO. VI REDUCTION OF RADIUM AND HARDNESS - ELGIN
Filter Percent Percent
Raw Effluent Radium Hardness
Date sampled pCi/1 Hardness pCi/1 Hardness Reduction Reduction
03/07/75 7.45* 226 0.75 99 89.9 56.0
03/14/75 5.7 243 0.80 112 86.0 53.9
03/21/75 3.51 242 0.71 95 87.0 60.7
*Calculated on basis of pumpage from individual wells.
All water is treated so that the values given for the filter effluent
represents the water which goes to the user.
During each backwash cycle 287,690 liters of water are used for each filter.
In addition, 15,142 liters are used for surface wash. The filters are back-
washed at approximately 50 hour intervals. This waste water contains signifi-
cant quantities of radium. The gross alpha counts, however, appear very low
when compared to the radium values. This is due to the method of handling the
samples in the laboratories. The aliquots for the gross activity determina-
tions were taken from the supernatant portion of the sample, while the aliquots
for the radium analyses were taken from the complete sample and contained a
portion of the solid material.
Lime sludge is removed from the mixing basin and from the final sedimentation
basin by continuous sludge removal equipment. The radium results on the
sludge samples are very erratic. Samples #107, 113, and 119 were collected
from the sludge blanket by means of a pump. Results were 12.53 +_ 0.19;
1.26 +_ 0.04, and 3.15 +_ 0.09 pCi/g of radium 226. Samples #114 and #120 were
taken from the sludge lagoon at the point where the sludge enters the lagoon.
The radium 226 concentrations found were 30 +_ 2 pCi/g and 6.01 +_ 0.18 pCi/g.
-34-
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All results are expressed on the basis of dry weight.
Records indicate that 1,900 to 3,800 kg of lime are used at this plant each
day. It is estimated that approximately 2 kg of sludge (dry weight) are
produced for each kg of lime used, which would result in 3,800 to 7,600 kg
produced each day. Calculating on the lowest and the highest values of
radium 226 found in the sludge, this will result in the deposition of 22.8
to 228 uCi of radium 226 each day.
The supernatant liquid from this lagoon is discharged to the river. Although
this waste was not analyzed for radium 226, the gross counts (2.9 +1.4,
4.1 +_ 1.7, 2.1 +_ 1.2 pCi/1) which were done on the supernatant portion of
the waste water indicate that the major portion of the radioactive material
is in the sludge.
During a survey of the plant, a sample of filter sand was obtained. Analyses
indicated a radium 226 concentration of 16.0 +_ 1.6 pCi/g and a radium 228
concentration of 8.3 +_ 0.4 pCi/g. After the initial analysis of the sample,
the fine material which appeared to be clarifier sludge was washed from the
sample with water. Analysis of the washed material showed no significant
difference.
Exposure rates at the plant indicated 9 pR/hr above the natural background in
the area of the evaporation pond. It was, however, not possible to get good
measurements in this area because of limited access. Water had been removed
from one of the sand filters for maintenance. Measurement just above the
surface of the sand filter indicated an exposure rate of 0.5 mR/hr. Over a
similar filter which was covered by water, the exposure rate was about
30 yR/hr.
5.5 MISCELLANEOUS CHEMICAL RESULTS
Reduction in the barium levels have also been observed. Although the raw
water levels are exceedingly high (6.1 to 18 mg/1), all samples of the
softened water contained less than 1 mg/1.
All chemical and radiological data are available in Appendix Table D-l.
5.6 COST INFORMATION
Information on the capital costs of the Slade Avenue Plant are not available.
However, the cost for the West Side Plant which was built in 1963, and which
is of similar design, have been included.
-------
Cost figures taken from the original bid are as follows:
General Conditions $ 17,600
Earth Work 5,170
Mason Work 269,772
Misc. Iron and Metal Work 44,662
Carpenter Work 8,930
Pipe Insulation 12,000
Painting 14,900
Rate Controllers 7,000
Flash Mixer 1,400
Recarbonation Equipment 21,000
Lime Storage and Conveying
System 12,830
Filter Instrumentation 20,000
Plumbing Work 119,800
Pumping Equipment 14,000
Up FLow Clarifier Equipment 19,410
Flow Meters 4,000
Electrical Work 68,570
Supervisory Control and
Telemetering Equipment 38,000
Engine - Generator 42,000
Aeration Equipment 3,000
Heating 7,000
Ventilating Work 300
Service Elevator 13,997
Laboratory Equipment 1,300
System Sterilization 1,600
Chemical Feeders 12,000
Gravimetric Lime Feeders 8,000
Lime Slakers 10,059
Chlorinators 9,000
Sewer Construction 14,000
TOTAL $821,300
In 1970, it was necessary to expand the West Side Plant. It is felt that this
work would be necessary to build an adequate treatment plant at the present
time.
-36-
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Cost figures for the expansion are:
General Conditions $ 50,000
Preparation of Site 6,000
Mason Work 188,400
Miscellaneous Metal Work 20,000
Carpenter Work 6,000
Painting 15,000
Rate Controllers 10,000
Recarbonation Equipment 6,000
Filter Instrumentation 32,000
Plumbing Work 110,000
Pumping Equipment 17,000
Upflow Clarifier Equipment 40,000
Electrical Work 27,000
System Sterilization 2,000
TOTAL $529,400
OPERATING COSTS
Chemicals Used Daily
Lime $28/3775 m3
Flocculant 3/3775 m3
Other Chemicals 1/3775 m3
Carbon Dioxide 3/3775 m3
Personnel
Operators - 3 @ $40/day
Supervision- 1 @ $60/day
15,100 m3/d
$120.00
12.00
4.00
12.00
$120.00
60.00
-37-
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6.0 LYNWOOD
6.1 INTRODUCTION
The village of Lynwood is located in the southeastern part of Cook County
(see Fig. 1). This is a fast growing area and, at present, it is estimated
that the supply serves about 4,000 people. Approximately 600 m^ of water is
processed at the plant each day. The supply went into operation in 1972, and
in 1973 softeners were added to the system.
6.2 DESCRIPTION
All of the water used by this supply is being pumped from one well known as
well number two. The well is 599.4 m deep and is cemented to a depth of
240.5 m. The well is open to a sandstone aquifer.
The water is softened by passing it through a styrene-based zeolite softener
(Permutit Corporation) and chlorinated before passing to the distribution
system. The plant is equipped with a series of three softeners and automati-
cally switches from one to another on the basis of hardness passing through
the softener. Raw water is blended automatically, so that the hardness of the
water reaching the user is fairly consistent. Consequently, the typical
increase in hardness normally observed as the softener is depleted is not
evident.
See Appendix E for detailed description of the facilities at the Lynwood Plant.
6.3 SAMPLING AND ANALYSIS
Samples of raw and softened water were collected on March 27, April 2 and 10
at the Lynwood Plant. Samples were analyzed for mineral trace metal and
radium content.
Softener backwash, brine and rinse water were composited and analyzed for the
same parameters.
6.4 RADIUM REMOVAL
Radium removal by this system is quite consistent. By the design of this
plant the water is always passed through a softener which has recently been
regenerated.
It was not possible to obtain samples directly from the softener and samples
which were obtained were blended water and represented the final product
which goes to the user. According to the manufacturer, the units are equipped
to detect the hardness of the finished water and automatically adjust the
amount of raw water in the blend to keep the hardness of the finished water
30
C.1-
-------
constant. Assuming that the hardness of the finished water is essentially
zero, the blend ratio is approximately 90% softened water and 10% raw water.
Near the end of the cycle, it is assumed that a small amount of hardness is
passing through the softener, and that the blend ratio is 91% softened water
and 9% raw water. Using these assumptions, the radium content of the softened
water ranged from 0.26 to 0.77 pCi/1.
The radium content of the raw water is consistent, ranging from 14.28 to
15.19 pCi/1 with the average being 14.71 +_ 0.24. The radium removal data are
shown in Table VII.
TABLE VII. RADIUM REDUCTION--LYNWOOD
Regenerated
Midpoint
Near
Breakthrough
Regenerated
Midpoint
Near
Breakthrough
Regenerated
Midpoint
Near
Breakthrough
Sampling
Date
3/27/75
3/27/75
3/27/75
4/2/75
4/2/75
4/2/75
4/10/75
4/10/75
4/10/75
Radium 226
Content
Raw Water
pCi/1
14.69
14.80
14.73
14.50
14.70
14.38
14.49
14.90
15.19
Radium 226
Content
Softened Water
(estimated)
0.40
0.26
0.40
0.44
0.36
0.51
0.77
0.27
0.27
Radium 226
Percent
Reduction
97.3
98.2
97.3
97.0
97.6
96.5
94.7
98.2
98.2
The gross alpha activity of the raw water samples is very erratic ranging from
58.4 to 178.4 pCi/1. This may in part be due to the period of time that the
samples were in the laboratory before counting. While the radon would be
lost through the evaporation process, the solid radon daughters would not.
The radon daughters decay rapidly and could account for significant changes
in the count. The samples collected on March 27 were counted within three
days of collection, and those collected on April 10 were held for five days
before counting was started.
-39-
-------
Another theory for the widely divergent alpha counts is the possibility that
the trace amounts of radioactive materials are plating on the walls of the
container. The addition of a preservative may prevent this erratic behavior.
The gross activity is somewhat high compared to the radium content. No
information is available as to the isotopes which contribute to the total
activity present.
The automated system regenerates the softener after 174,128 liters of water
have passed through the unit. For each regeneration, 8,327 liters of water
are used for backwash, 757 liters of brine for regeneration, followed by
5,450 liters of water for rinse, and an additional 17,033 liters for fast
rinse. The average concentration of radium 226 in the waste water was
72.35 pCi/1. Since a profile of the waste was not done, this may not be
representative of the amount of radium 226 being removed from the softeners
during the regeneration cycle.
The survey of the plant indicated that there were no measurable exposure rates
above background except at the surface of the zeolite tanks. The exposure
rate profiles (see Fig. 10) vertically on the sides of the three tanks
indicate that the maximum concentration of radium is near the bottom of the
zeolite.
Samples of the zeolite were taken at approximately 1.06 m and 2.3 m above
the bottom of the tank. Radium concentrations found were as follows:
226 Ra (pCi/g) 228 Ra (pCi/g)
1.06 meters 9.6 ^ 1.8 6.6 ^ 0.6
2.3 meters 6.2 ^ 1.5 5.0^0.5
These results appear to confirm the exposure rate profile of the tank.
6.5 MISCELLANEOUS CHEMICAL RESULTS
Detailed information on mineral, trace metal and radium analyses are available
in Tables E-l and E-2.
6.6 COST INFORMATION
Cost information for this plant,as built in 1972,give $100,000 for the
equipment and $50,000 for installation. Monthly operating costs are about
$1,520 with the breakdown being $1,000 for salaries and $520 for salt. This
covers the cost of producing 6 x 10^ liters of water/day. The operating
cost thus are about $0.32/1000 gal.
-40-
-------
Figure 10: Exposure
Rate Profile
Lynwood, Illinois
(0
1-1
o
,£>
•a
-------
APPENDIX A
DWIGHT CORRECTIONAL CENTER
-42-
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Dwight Correctional Center ;R
Office Bldg.
WELL #2 - Showing Sampling
Tap
(Above Bucket)
Aerator § Holding Reservoir
Figure A-l (Cont'd.) Scenes at Dwight Correctional Center
Water Treatment Plant
-43-
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High Service Pump House
Softener Unit § Flow Controls
Softened Water Sample Tap
Softener Flow Control Valve
Figure A-l (Cont'd Scenes at Dwight Correctional Center Water
Treatment Plant
-44-
-------
Supply. DWIGHT CORRECTIONAL CENTER
Item
Well #2
Location: 137.2m North, 30.5m West of
the SE corner of Sec. 1
T 30N, R 6E, Livingston County
Pump:
7.57 i./s Pomona Water Lubrica-
ted above base discharge
Motor: 14920W, 184.3 rad/s, 3ph,
60 Hz, 220/440V
Chronology: Drilled in 1948 by Milaeger
Well Drilling Company,
Milwaukee, Wisconsin
Notes:
Sampling tap
Production Data
Date:
Static Level, m
Pumping Level, m
Pumping Rate, Jl/s
Specific Capacity
1951
45.1
64.0
7.57
0.40
Figure A-2 Well Log, Well #2,
Dwight Correctional Center
-------
Well #2 - 366.1 m deep
Pump capacity - 7.57 1/s
PARAMETER AND REMOVAL EFFICIENCY
Ra226
Coke tray aerator
4 trays - 11.24 m total area
Capacity - 7.63 1/s
Chlorination
Capacity - 10.9 kg/d
Collecting reservoir
Volume - 757 m^
Detention time (minimum) - 27.8 hr
High service pumps (2)
Capacity - 4.73 1/s each
Ion exchange softeners (2)
(Green sand unit tested)
1.83 m dia X 2.13 m high each
Capacity - 45.36 kg each
Chemical feed -
Sodium hydroxide at 8.9 mg/1
Sodium silicate at 28.8 mg/1
Elevated storage
Volume - 473 m
Height - 30.5m
Distribution
3.25
Gross
Alpha
22.9
0.36
88.9
24.3
3.7 83.6
0.65' 80
Hard-
ness
286
43.2
85
5.6
75.5
67
76.6
Figure A-3 Dwight Flow Schematic
- 46 -
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Dwight Correctional Center
Aerator
Location: Atop collecting reservoir at treatment plant
Type: Coke tray with spray nozzles
Construction: Four trays housed in wooden structure with 45 degree
louvers screened outside with 24-mesh plastic and stainless steel
screens.
Dimensions: Each tray 1.68m x 1.68 m (5 i1 x 5 i1)
Area: 11.24 m2 (121 ft2) total
Capacity: 7.63 L/s at .68 L/m2s (121 gpm at 1 gpm/ft2)
Note: Coke changed twice per year
Gas Chlorinator
Location: Service building (not located in isolated room)
Manufacturer: Wallace and Tiernan
Capacity: 10.9 kg/d (24 ppd)
Chlorine Source: One 68 kg (150 Ib) cylinder on platform scale
Injects to: Aerator discharge
Collecting Reservoir
Location: Adjacent to north side of treatment plant
Construction: Concrete-two sections with dividing partition
Dimensions: 11.9 m x 16.5 m x 4.9 m (39' x 54' x 16' )
Capacity: 757,000)1 ( 200,000 gal. )
Vents: Vent box on platform cover with fine screen opening
Manholes: Two with raised curbs and overhanging covers.
Overflow: Down turned and screened
High Service Pumps
Location: Pump pit adjacent to south side of collecting reservoir
Manufacturer: American Well Works
Number: Two-pumped one at a time alternated monthly
Capacity: 4.73&/S (75 gpm) each
Take suction from: Collecting reservoir
Discharge to: Softeners
Power: 5595 W (7.5 HP)
Angular Velocity: 376.9 rad/s (3600 RPM)
-47-
-------
Softener #1 (west)
Size: 1.83 m dia x 2.13 m high
Exchange media: Styrene based zeolite
Capacity: 45.36 kg (700 kilograins)
Regeneration: every 132,500 I, (35,000 gal.) using 181.8kg (400 Ibs) salt
Softener #2 (east)
Size: 1.83 m dia (6') x 2.13 m (7') high
Exchange Eedia: Natural green sand zeolite
Capacity: -45.36 kg (700 kilograins)
Regeneration: every 132,500 £ (35,000 gal.) using 272 kg (600 Ibs) salt
Chemical Feeder
Location: Service building - east side
Chemical: 1.18 kg (2.4 lb) NaOH and 3.82 kg (8.4 Ib) sodium silicate
dissolved in 189 A (50 gal. ) of water is fed to each 132,500 £
(35,000 gal.) of water treated
Type: Positive feed
Manufacturer: Hills McCanno
Fed from: Mixing drum
Injects to: Softener effluent
Elevated Storage Tank
Location: East of main building
Construction: Steel
Tank Dimensions: 7.6 m (12.51 ) dia x 10.7 m (35' ) high
Capacity: 473,000 A (125,000 gals.)
Tower Height: 30.5 m (100' )
Overflow: screened
Installed: 1930
-48-
-------
s e
- 49 -
-------
X3SS
HCMW
Oo»-i c5
/1POQ3
« §
3 tti
- 50 -
-------
APPENDIX B
PERU
-51-
-------
I
Peru Water Treatment Plant:
Raw Water Inlet & Sampling Tap (Arrow)
Plow Channel Front AeraCor Sludge Blow off Pit
Figure B-l Scenes at Peru Water Treatment Plant
-52-
-------
Well #6 Sampling Tap
Filters
Manhole of Clarifier Unit-
Sampling Point for "Sludge Blanket"
Figure B-l (Cont'd.) Scenes at Peru J
Water Treatment Plant ?
-53-
-------
Supply: PERU
Item: Well #5
Location: 121.9m South, 304.8m West of
the NE corner of Sec. 20,
T 33N, R IE, LaSalle County
Pump: Byron Jackson Line Shaft
Turbine, 63.1 !,/a @ 91.4m TDK,
185.3 rad/s, 6 stage, S/n
701C--37, set @ 76.2m
Motor: General Electric 89.250W,
185.3 rad/s, 3ph, 60 Hz, 460V,
144A, 60 C, 1.15 Ser. Fact,
Model 5K6268 x HIA s/n
DFJ 401108
Chronology: Drilled in 1931 by Sewell Well
Company, St. Louis, Missouri
Notes: Casing vent, airline with gage,
air relief valve
Production Data:
Date
Static Level, m
Pumping Level,m
Pumping Rate, i/s
Specific Capacity
1947
11.9
63.1
5.30
t6-°C»t(l.l/i>f
S13-L"!
Rtchywond
£ji-&i
f r*-nc,on 10-
11&-S* -
£o.
-------
Supply: PERU
Item:
Well #6
Location: 161.5m North, 103.6m East
of the SW corner of Sec. 16,
T 33N, R IE, La Salle County
Pump: Byron Jackson Line Shaft
Turbine, 75.7 2/s, @ 51.8m TDK,
183.2 rad/s, 3 Stage, s/n
681C026, set @ 76.2m
Motor: General Electric 93250W, 185.3
rad/s, 3ph, 60 Hz, 460 V,
144A, 60°C, 1.15 Ser. Fact.
Model 5K6268 x H 1A s/n AEJ
122,983
Chronology: Drilled in 1952
Notes: Casing vent, sample tap,
airline with gage, air relief
valve
Production Data:
Date:
Static Level, m
Pumping Level, m
Pumping Rate, i./s
Specific Capacity
1952
13.4
45.7
96.8
3.00
fTllm
Lnim
-£V«v. /4V.C*n|..--*-
i'.\'^:.\: '„•'•!•'•.**»"•" ;".•;"•
Pe. r\ * s '.-'.V"/':i»-'.Y
| ^ _^_- It. ser*
1 ^""*""' 7 7^>?
||-^ -y , y
*~1f>~,
< <, 1 O C rvi
L . /* Z 7*1
^ 331. t> m
SS
0^1. ,S
7r^ ?/»^ ———
Figure B-3 Well Log-Well »6 - Peru
- 55 -
-------
Supply: PERU
Item:
Well #7
Location: 61.0 m South, 61.0 m East of
the NW corner of Sec 21, T 33N,
R IE, La Salle County
Pump: Byron Jackson Line Shaft
Turbine, 63.1 i/s @ 98.5m
TDK, 185.3 rad/s, Model DWC
6 stage, s/n 711Col54, Set
@ 82.3m
Motor: General Electric, 93250W, L85.3
rad/s, 3ph, 60Hz, 460V, 144A,
60°C, 1.15 Ser. Fact,
Model 5K 628 x H37 A, s/n
KGJ 1027 100
Chronology: Drilled in 1963
Shot in 1972
Notes: Casing vent, sample tap, air
line with gage, air relief
valve.
Production Data:
Date:
Static Level, m
Pumping Level , m
Pumping Rate, £/s
Specific Capacity
1963
0+
57.6
92.2
1.60
f* ti~\ —
]
'*1
,J- — 3JS- f
H.fe
fl'nm
f&7 ?**?
aff e.
i m e sro
5 W/e
*— 789. 7 '
Figure B-4 Well Log-Well l!7 - Peru
- 56 -
-------
Wells -
#5 - 792.8 m deep, pump cap. 63.1 1/s
#6 - 812.3 m deep, pump cap. 75.7 1/s
#7 - 789.8 m deep, pump cap. 63.l' 1/s
Coke tray aerator
Three stacks of three trays each
Area - 30.1 m2, Capacity - 102.2 1/s
Chemical feed
Lime, Capacity - 113.6 kg/hr
i Q Chemical feed
/ Sodium aluminate, Capacity unknown
Mixing tank
Volume - 136 m
Detention time - 30 min
Clarifier
Volume - 280 m3
Detention time - 60 min
Settling tank
Volume - 575 m3
Detention time - 120 min
Recarbonation tank
Volume - 24.6 m3
Capacity - 7.1 1/s at 5 min detention
Chlorination
Capacity -'22.7 kg/d
Filters (3)
4.3 m X 3.7 m each
Area - 15.8 m2 each
Capacity - 1850 m^/d each
1
1
-1
Clearwell
Volume -
121 m3
Suction well
High service pumps
#1 - Capacity -44.2 1/s
p" ^
f —
— ^
~- — " if/ - capacity - 44 . / i/s
#3 - Capacity - 113.6 1/s
Elevated storage (stand pipe)
Volume - 4920 in3
PARAMETER AND REMOVAL EFFICIENCY
Ra226
5.8
1.15
3.0
7.
80.1
48
Gross
Alpha
26
%
I
4.93
11.4
81
56
Hard-
ness
317
117
181
*
63
43
L_
Distribution
- 57 -
-------
Peru
Water Meter
Location: Well 6 house
Manufacturer: Sparling
Size: 25.4 cm (10 inch)
Measures flow in: Well 6 discharge
Records flow as: 378.5 £
Booster Pump
Location: Well 6 House
Pump Data
Type: Double suction horizontal split case centrifugal
Manufacturer: American Marsh
Model: HIM
Serial: 6101197
Size: 5
Impeller: 3.43 cm
Stages: 1
Angular Velocity: 183.2 rad/s (1750 RPM)
Capacity: 75.7 L/s (1200 gpm)
Head: 48.8m (160 Ft.)
Takes suction from: Well 6 discharge
Discharges to: Distribution
Installed: Standard
Driver Data
Type: Induction motor
Manufacturer: Fairbanks-Morse
Model: QZK
Serial: F169935
Power: 44760W (60 HP)
Angular Velocity: 182.2 rad/s (1740 RPM)
Electrical Requirements: 3ph, 60 Hz, 440V, 61a
Rating: 40° C
Service factor: 1.15
Water Meter
Location: Well 7 house
Manufacturer: B.I.F.
Model: Propeloflo
Size: 20.3 cm (8 inch)
Measures flow in: Well 7 discharge
Records flow as: Hundreds of gallons (378.5 0
-58-
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Aerator
Location: North side of treatment plant
Type: Coke tray with forced draft
Construction: Three stacks of three trays inside wood"ten housing
Dimensions: Each tray 1.83 m x 1.83 m ( 6' x 6' )
Area: 30.1 m2 (324 ft2)
Capacity: 102.2 i/s @ 3.4 £/m2/sec (1620 gpm § 59pm/ft2)
Blower: yes
Chemical Feeder
Location: Chemical room at treatment plant .
Type: Volumetric feed lime slaker
Manufacturer: Omego
Capacity: 113.6 kg/hr (250 Ib/hr)
Fed from: Lime hopper
Injects to: Mixing tank
Chemical Feeder
Location: Chemical room at treatment plant
Chemical: Sodium aluminate
Type: Piston pump
Manufacturer: Warren Cook
Model No.: Crown Jewel
Fed from: Chemical drum
Injects to: Mixing tank
Anti-siphon device: None
Mixing Tank
Location: Beneath chemical room
Construction: Concrete
Dimensions: 6.1m x 6.1m x 3.7m (20' x 20' x 12')
Volume: 136,000 H (36,000 gal)
Manhole: one with flush cover
Agitator: Horizontal paddles driven by vertical shaft, 1119W
(1.5 hp motor)
Capacity: 6.54 x 10 i. (1,728,000 gallons) per day @ 1800 second detention
Clarifier
Location: North side of treatment plant
Construction: Concrete
Dimensions: 9.1m dia. x 4.3m deep (30' dia. x 14' deep)
Volume: 280,OOOL (74,000 gallons)
Capacity: 6.72 x 10°£, (1,776,000 gpd) at 3600 sec detention
Wier: Around circumference - 26-8m (88') long
Wier loading: 2.9 i/s/m (14 gpm/ft.) @ 77.8 l/s (1233 gpm)
Manhole: Two with flush lids
Manufacturer: Graver Tank and Manufacturing Company
- 59 -
-------
Settling Tank
Location: Beneath aerator and lab at treatment plant
Construction: Concrete
Dimensions: 11.0m x 9.1m x -4.4m + 4-.9m x 6.1m x 4.4m
(36' x 30' x 14.5' + 16' x 20' x 14.:'')
Volume: 575,3801 (152,000 gal.)
Capacity: 6.9 x 106L/d (l,824,OCO gpd) @ 7200 see. detention
Recarbpnator
Location: Under stairs to filter room at treatment plant
Construction: Concrete
Dimensions: 4.4m x 1.5m x 3.7m deep (14.5' x 5' x 12' deep)
Volume: 24,6401 (6510 gal.)
Capacity: 3.55 x 1C6 l/d (937,000 gpd) @ 600 sec. detention
7.1 x 106 L/d (1,875,000 gpd) @ 300 sec. detention
C02Generator: Walker Process Natural Gas burner
Serial No.: #607-2897
Gas Chlorinator
Location: Filter room at treatment plant
Manufacturer: Fischer - Porter
Type: Wall-mounted, vacuum operated, solution feed
Capacity: 22.7 kg/d (50 Ibs per 24 hrs)
Chlorine Source: One 68 kg (150 Ib.) cylinder
Booster Pump: None - operates off distribution pressure
Injects to: Recarbonator discharge
Chlorine room: none
Scale: yes
Filter
Location: Filter room at treatment plant
Number of Units: three
Type: Gravity rapid sand
Dimensions: 4.3m x 3-7m (14' x 12'2' )
Filter Area: 15.8m2 (170 ft.2)
Capacity: 1.85 x 106 2,/d @ 1.36 >Vn2 /s (490,000gpd @
Filter Media: Anthracite over .76m (30" ) sand supported by .46m
(18" ) gravel 5cm (2" ) laterals on 15.2m (6" ) centers
Backwash: Manual using distribution
Clear Well
Location: Beneath filters and operating floor at treatment plant
Construction: Concrete
Dimensions: 7.1m x 13.1m x 1.5m deep (20' x 43' x 5' deep)
Capacity: 121,OOOL (32,000 gallons)
Vents: One, turned down
- 60 -
-------
Suction Well
Location: Under high service pumps on west side of power plant
Construction: Concrete
Manhole: Two, with flush covers
High Service Pump
Location: West side of power plant
PUMP DATA
Type: Single suction horizontal split case centrifugal
Manufacturer: DeLaval
Stages: Two
Capacity: 44.2 £/s (700 gpm)
Head: 79.2m (260 ' )
Takes suction from: Suction well
Discharges to: Distribution
DRIVER DATA
Type: Induction motor
Manufacturer: General Electric
Model: 5K505DG1
Power: 55,950 W (75Hp)
Angular Velocity: 185.8 rad/s (1775 rpm)
Electrical Requirements: 3ph, 60 Hz, 2200V, 17.la
Rating: 40° C
Water Meter
Location: West side of power plant
Manufacturer: B.I.F.
Model: Venturi
Size: 20.3 cm (8")
Measures flow in: High service pump 1 discharge
High Service Pump
Location: West side of power plant
PUMP DATA
Type: Single suction horizontal split case centrifugal
Manufacturer: DeLaval
Stages: Two
Capacity: 44.2 £/s (700 gpm)
Head: 79.2m (260' )
Takes suction from: Suction well
Discharges to: Distribution
-61-
-------
DRIVER DATA
Type: Induction motor
Manufacturer: General Electric
Model: 5K505DG1
Serial Mo.: 5380268
Power: 55950W (75 HP)
Electrical Requirements: 3ph, 60Hz, 2200V, 17.8a
Rating: 40°C
Water Meter
Location: West side of power plant
Manufacturer: B.I.F.
Model: Venturi
Size: 20.3cm (8")
Measures Flow in: High service pump 2 discharges
High Service Pump
Location: West side of power plant
PUMP DATA
Type: Double suction horizontal split case centrifugal
Manufacturer: Peerless
Model: 6A19B
Serial: 1-45908
Stages: One
Angular Velocity: 185.3 rad/s (1770 rpm)
Capacity: 113.6 £,/s (1800 gpm)
Takes Suction From: Suction well
Discharges to: Distribution
DRIVER DATA
Type: Induction motor
Manufacturer: U.S. Motors
Model: SC
Serial: 1245250
Power: 149,200W (200 HP)
Angular Velocity: 188.4 rad/s (1800 RPM)
Electrical Requirements: 3ph, 60 Hz, 440V 240a
Rating: 40°C
Water Meter
Location: West side of power plant
Manufacturer: B.I.F.
Model: Dall flow tube
Size: 25.4 cm (10")
Measures Flow in: High service pump 3 discharge
-62-
-------
Elevated Storage
Location; Shooting Park Road and Pike Street (West)
Construction: Hemispherical bottom, vertical sides, conical top
Capacity: .757 x 106L (200,000 gal.)
Tower Height: 12.2m (40 ft.)
Surface Elevation: 192.0m (630 ft.) msl
Overflow: Down leg to ground surface
Maximum Surface Elevation 198.1m (650 ft.) msl
in Supply: 198-1 m (650 ft.) msl
Date Installed: 1931
Elevated Storage
Location: Shooting Park Road and Pulaski Street (East)
Construction: Hemispherical bottom, vertical sides, conical top
Capacity: .757 x ICPi (200,000 gal.)
Tower Height: 15.2m (50 ft.)
Surface Elevation: 189.0 m (620 ft.) msl
Maximum Surface Elevation in Supply: 170.7m (560 ft.) msl
Overflow: Down leg to ground surface
Data Installed: 1931
Elevated Storage
Location: Plaza booster station (North)
Construction: Steel standpipe
Tank Dimensions: 17,1m (56 ft.) dia
Capacity: 4.92 x 106J? (1,300,000 gal.)
Head Range: 21.6m (71 ft.)
Tower Height: no tower
Surface Elevation: 196.9m (645 ft.) msl
Maximum Surface Elevation in Supply: 198.1m (650 ft.) msl
Overflow: Down tank >to elevation + 4 L.S.D.
Installed: General American Transportation Corporation, 1964
High Service Pump
Location: Plaza Booster Station
P_UMP DATA
Type: Double suction horizontal split case centrifugal
Manufacturer: Aurora
Model: OJP
Serial: 6327077
Size: 5£ x 6
Stages: 1
Angular Velocity: 176.1 rad/s (1690 RPM)
Capacity: 63.1 £/s (1000 gpm)
Takes Suction From: Standpipe
Discharges To: Distribution
-------
DRIVER DATA
Type: Induction motor
Manufacturer: Marathon
Power: 37,300W (50 HP)
Angular Velocity: 186.4 rad/s (1780 rpm)
Electrical Requirements: 3ph, 60Hz, 240/480V H6/58a
Design: B
Code: F
Rating: 40°C
Auxiliary: None
Remarks: Fluid coupling to vary speed of pump
High Service Pump
Location: Plaza Booster Station
PUMP DATA
Type: Double suction horizontal spilt case centrifugal
Manufacturer: Aurora
Model: OJP
Serial No.: 6327078
Size: 5£ x 6SL
Stages: one
Angular Velocity: 183.2 rad/s (1750 rpm)
Capacity: 63.1 Vs (1000 gpm)
Head: 39.6m (130 ft.)
Takes Suction From: Standpipe
Discharges To: Distribution
DRIVER DATA
Type: Induction motor
Manufacturer: Marathon
Power: 29840W (40 BP)
Angular Velocity: 186.4 rad/s (1780 rpm)
Electrical Requirements: 3ph, 61 Hz, 220/440V, 110/50a
Design: B
Code: F
Rating: 40°C
Auxiliary: 6 cylinder Waukesha natural gas engine
Water Meter
Location: Plaza Booster Station
Manufacturer: B.I.F.
Model: Dall flow tube
Size: 30.5 cm (12 inch)
Measures Flow In: Booster station discharge
-64-
-------
Test Equipment
Chlorine & pH: Hach DR Filter Photometer
Hardness & Alkalinity: Hach Titrametric
-65-
-------
a 3
1 S
5 b
o o
- 66 -
-------
H" -
•36
- 67 -
-------
APPENDIX C
HERSCHER
-68-
-------
c
rt
C
CD
rt
CD
fn
f-i
CD
O
(/I
f-i
O
c
CD
O
CD
f-l
3
Herscher Water
Treatment Plant
Top of Softener &
West Filter—Showing
Manholes Used For
Sampling Anthrafilt &
Resin
Filter Backwash
Drainage Pit
-69-
-------
Well //5
Softenfi- & Sar-.pling Tap (Arro«0
Figure C-l (Cont'd.)
West Fijter & Filter Effluent
SaiapJIrg Tap (Arrow)
Softeiier
Scenes at Herscher Water
Treatment Plant
-70-
Tlrainage Pit
-------
Supply:
Herscher
Item:
Well #5
Location: 30.5m South, 304.8m West of the
NE corner of Sec. 29, T30N,
R 10E, Kankakee County
Pump: Sumo Submersible
10.09 ils, Set @ 128.0m
Motor: 18.650W
Chronology: Drilled in 1953 by an oil
field contractor to 199.3m and
finished by Layne-Western Co.
/^
/•:"•*•
<£"/«* /y«./i «/:.>'. . •
{.-W . : : •$>-•'•'. :-:-':^'
i.
t/« k not*J>i
5 a-n at ' s te> n €
/^
I
6
r
T?\
:; :"?:\
•/->.-••. L
•:-..-i: .;.•.:•.->•. :-:.-:^:---f
Production Data:
Date:
Static Level, m
Pumping Level, m
Pumping Rate, « /s
Specific Capacity
1975
65.5
118.8
10.09
0.19
Figure C-2 Well Log-Well #5 - Herscher
- 71 -
-------
Well #5 - 240.5 m deep
Pump capacity - 10.09 1 Is
* O Chemical feed -
Potassium permanganate
Capacity - 113.6 1/d
Forced draft aerator
Capacity - 13.56 1/s
Chlorinatlon
Capacity - 45.4 kg/d
Collecting reservoir
Volume - 60.6 m-'
Detention time - 100 min
High service pump
Capacity - 13.56 1/s
Filters (2)
1.83 m dia X 1.52 m high each
Filter area - 5.25 m each
Capacity - 9.45 1/s each
Chemical feed -
Polyphosphate
Capacity - 189.3 1/d
Ion exchange softener
1.68 m dia X 2.13 m high
Capacity - 110 kg
Elevated storage
Volume - 283.9 m3
Height - 30.5 m
PARAMETER AND REMOVAL EFFICIENCY
Ra226
14.43
13.75
6.75
1.31
2.37
%
4.7
50.9
80.6
83.6
Gross
Alpha
56.6
51.3
19.7
6.68
15.7
%
9.4
61.5
66
72
Hard-
ness
404
83.2
141
%
79.4
65
Distribution
Figure C-3 Horscher Flow Schematic
- 72 -
-------
Herscher
Chemical Feeder
Location: Pumphouse near aerator
Chemical: Potassium permanganate solution^
Type: Piston pump
Manufacturer: Warren Cook
Capacity: 0 - 113.6 £/d (0 - 30gpd)
Fed From: Plastic drum
Fed To: Raw water discharge to aerator
Aerator (Forced Draft)
Manufacturer: General Filter Company
Location: Pumphouse
Type: Square Steel (Epoxy-coated inside) with steel baffles
Size: 1.07m x 1.07m x 3.66m (42" x 42" x 12')
Inlet pipe: 12.7 cm (5")
Outlet Pipe: 15.2 cm (6")
Capacity: 13.56 £/s (215 gpm)
Blower: Perriess Model 122A
Capacity: 1.47 m^/s (950 CFM) % 2 SP
Motor Power: 124.3W (1/6 HP)
Motor Type: Drip and Weather proof hood
Gas Chlorinator
Location: Separate room at pumphouse
Manufacturer: Wallace and Tiernan
Type: Wall mounted, "Advance" type
Model: A-741
Capacity: 45.4 kg/d (100 ppd)
Chlorine Source: Two 68kg (150 Ib.) chlorine gas cylinders,
platform scale mounted
Booster Pump: None. Operates from mains
Injects To: Aerator discharge
Collecting Reservoir
Location: Pumphouse
Dimensions: 4.27m x 4.88m x 3.05m (14' x 16' x 10')
Capacity: 60,566 £ (16,000 gal.)
Type: Concrete rectangular tank 3.05m (10' )
Manholes: One with flush cover
-73-
-------
Booster Pump
Location: Pumphouse near Aerator
Make: Layne-Bowler five stage shallow well turbine
Capacity: 13.56 0,,/s (215 gpm)
Motor: "Hollow shaft" (U.S. Motors)
Type: H U - 3 (#3276819)
Power: 7460 W (10 HP)
Angular Velocity: 188.5 rad/s (1300 RPM)
Suction From: Holding Reservoir
Delivers To: Filters
Filters (Two Units)
Manufacturer: General Filter Corporation
Performance: Type: Pressure Type vertical
Filter Area: 5.25m2 (56.5 ft.2)
Filtration Rate: 1.80 i./s^/s (2.65 gal./ft.2/min. )
Backwash Rate: 4.07 Jl/m2/s (6 gal./ft.2/min. )
Backwash Source: Mains
Specifications: Nominal Diameter: 1.83m (72")
Height: 1.52m (60")
Filter Media: #1 Antrafilt
Type of Underdrain: GFC multiplate baffle
Working Pressure: 689500 N/m2
Filter Bed Depth: 0.61 m (24")
Gravel Support Bed: Depth - 0.38m (15")
Air relief valve: Manual
Operation: Manual
Location: Pump house
Softener
Manufacturer: General Filter Corporation
Performance:
Softening Rate: 7.38 l/s (117 gpm)
Unit Capacity: 280120* (74,000 gal.)
Salt Required: 232 kg (510 Ibs.)
Back Wash Rate: 6.31 l/s for 900s (100 gpm for 15 man.)
Brine Rate: 1.89 A/s for 1200s (30 gpm for 20 min.)
Rinse Rate (slow): 1.89 */s for 1200s (30 gpm for 20 min.)
Rinse Rate (fast): 5.05 «./s for 1200s (80 gpm for 20 mir. )
Operating Control: "Solomatic"
Specifications:
Nominal Diameter: 1.68 dia. (66")
Height: 2.13m high ( 84")
Filter Medium: 2.4 m3 (85 ft3) of "HCR" resin
Exchange Capacity: 110 kg (1700 Kilograins)
Operating Pressure.: 689500 N/m2 (100 psi)
Underdrain: GFC Multiple Plate
Overdrain: Standard Baffle
Location: Pump house
- 74 -
-------
Brine Pump
Make: Aurora Pump
Type: Self-priming
Capacity: 1.07 H/s at 15.24m TDK (17 gpm at 50 ft. TDK)
Motor Power: 559.5W (3/4 HP)
Electrical Requirements: 220V, 3ph, 60 Hz, 188.5 rad/s (1800 RPM)
Model: AA 1321-0-11
Operation: Automatic by "Solomatic" Valve Control
Chemical Feeder
Location: Pumphouse near softening unit
Chemical: Polyphosphate
Make: Milton Roy
Type: Positive displacement, three stage
Model: Simplex
Capacity: 189.3 Vd (50 gpd)
Fed From: Steel' tank .76m dia. x 1.22m high (30" diam x 48" high)
Injects To: Softener inlet stream
Master Meter
Location: Downstream from softener and Filtered water (bypass)
discharge at Pumphouse
Make: Badger "Easy Read"
Size: 15.24 cm (6")
Reads: in 100 gallons (378.5O
Test Equipment
Chlorine & pH: Hellige Colorimetric
Hardness, Iron & Phosphate: Hach titrimetric Kit
Elevated Storage
Location: Alley between Main & Oak (100 block south)
Construction: Hemispherical top and bottom. Vertical sides
Capacity: 283,900£, (75,000 gal)
Height: 30.5m (100 ft.)
Installed: 1954 (S No. 7-2891)
-75-
-------
—[-
•ii ¥i
HI C
5 d
- 76 -
-------
! t -h
V-1]--
?
-------
S .3 i
u S
I 1
M f
o 3
- 78 -
-------
APPENDIX D
ELGIN
-79-
-------
Aeration Tank Vent
(With Exhaust Fan on Top)
Filter #6
View of Lagoon
Figure D-l Scenes at 31gin Water Treatment Plant
-80-
-------
Filter #3 Filter Beds
Slush Pump-Sampling Tap for Fresh Sludge
(Arrow)
Slush Pump-Locations of Intake Valves
Manifold (partial view)
Figure D-l (Cont'd.) Scenes at Elgin
Water Treatment Plant
-81-
-------
Supply. ELGIN (Slade Avenue Plant)
Item:
Well #1
Location: 381 m South, 396.2m West of the
NE corner of Sec. 11, T 41N,
R8E, Kane County
Pump: KSB Submersible
63.lVs set at 182.9m
Motor: 149200W, 480 Volt
Chronology: Drilled in 1904 by Frank M.
Gray, Milwaukee, Wisconsin.
Rehabilitated in 1960-61 by
S. B. Geiger & Co., Chicago
Production Data:
Date
Static Level, m
Pumping Level, m
Pumoine Rate, i/s
Specific Capacity
1931
26.5
37.5
22.7
2.06
V .
Ill*™ •
Si ?
Wt,»~S±«±
i-/me s-f
«-*>'-«*
Co, II Ht>
Uo(e,
ttll-m ~.
plnk
Pink
V//.J-/H -
Foil do. W1
5*x ncl 5Tc?n
STSon-
"Iff 8rt
-AT X.
Figure D-2 Well Log-Well #1 - Elgin
- 82 -
-------
Supply: ELGIN (Slade Avenue Plant)
Well #2
Location! 335, 3m South, 365.8m West of
the NE corner of Sec. 11, T41N,
R8E, Kane County
Pump: B-J Submersible
63.1 l/s
Motor: 149200 W
Chronology. Drilled in 1904 by Frank M. Gray
Milwaukee, Wisconsin
Rehabilitated in 1959 by S. B.
Geiger and Co. Chicago
Production Data:
Date
Static Level, m
Pumping Level, m
Pumping Rate, i/s
Specific Capacity
1960
100
118.3
2.72
n. i-—*-.'"
1*1 ?••* - _'*^_>^» "-r
3fc '/--•' ^-•!•'-'
/V/a q 0. ro-
>~ IK) £ £ to rt
feve
-Vi"-H.
:*.»! *i
It" 4"
J2tfx3»
P<»--k
Si
a-nd\
Jiof«
Figure D-3 Well Log-Well #2 - Elgin
- 83 -
-------
Supply: ELGIN (Slade Avenue Plant)
Item: well #3
Location: 304.8m South, 335.3m West of the
NE corner of Sec. 11 T4IN, R8E,
Kane County. (Well house approx-
imately 90m north of Slade Avenue
Treatment Plant)
Pump: B-J Submersible
56.8 i/s
Motor: 111.900W. 480V
Chronology: Drilled in 1904 by Frank M.
Gray, Milwaukee, Wisconsin
Production Data:
Date
Static Level, m
1960
97.5
Pumping Level, m
Pumping Rate, 1/s
Specific Capacity 1.02
1961
107.3
131.4
23.7
t/f c. q a. r" a.
!~.'M e stone.
/V7.«w -
no- 7m Trent
51 pt.le.r-
Holt.
-nd y
io.3 C^.T >,..(,.
Figure D-4 Well Log-Well #4 - Elgin
-------
Supply: ELGIN (Slade Avenue Plant)
Item:
Well #5
Location: 457.2m South, 442.0m West of the
NE corner of Sec. 11 T4IN, R8E,
Kane County. (Well house 152.4m
South of Slade Avenue Treatment
Plant)
Pump: B-J Submersible
63.U/S set at 182.9m
Motor: B-J Electric
149200W
Chronology: Drilled in 1949 by Layne-
Western Company
Production Data:
Date
Static Level, m
Pumping Level, m
Pumping Rate, i/s
Specific Capacity
1949
30.5
97.6
82.0
1.22
£ lev
0,1* eke
IT. 8»1
O14<>1 '
SS
SS
ZW*,~"'*•"•'
if I s* One.o4c*. Dd t 55
t>"t.
Fr a.n con ta~
„„„ Hoi. iS /Jh
ft cl t f v m <.
Figure D-5 Well Log-Well #5 - Elgin
- 85 -
-------
Supply: ELGIN (Slade Avenue Plant)
Item: Well #6
Location: 518.m South, 457.2m West of
NE corner of Sec. 11, T4IN,
R8E, Kane County
(152.4m south of Slade Avenue
Treatment Plant)
Pump: B-J submersible
Motor: 186,500 W
Chronology: Drilled in 1958 by L. C.
Neely, Batavia
£le\j
/S2x?
i- / we f 7
1 8t
S-freo/fcS
me si o n z
5 In a I e
Production Data:
Date
Static Level, m
Pumping Level, m
Pumping Rate, .1/s
Specific Capacity
1958
124.0
135.3
94.8
8.39
1958
124.0
1975
118.6
}°3 ln-
3iH in -
Figure D-6 Well Log-Well #6 - Elgin
- 86 -
-------
IT
^H C*l
iH iH
Hill L
Iwells-
#1 - 592.8 m deep, pump cap. 63.1 1/s
^ #2 - 589.8 m deep, pump cap. 63.1 1/s
H #3 - 546.1 m deep, pump cap. 56.8 1/s
2 is is #6 - 396.2 m deep, pump cap. 94.8 1/s
Raw water reservoir
Volume - 93A m3
1
ll ][ i^ LOW service pumps (j)
r\f~\ f\ #1 - H3.6 1/s at 10 m head
1 )( 2 )( 3 ) #2 - 132.5 1/s at 12.2 m head
V^VV^X V_y #3 - 72.5 1/s at 12.2 m head
1
VW
, . . _
L"
Forced draft aerators (2)
4.57 m X 13.41 m X 2.44 m each
Capacity - unknown
r~O Chemical feed (2)
/ Lime, Capacity unknown
/ r~O Chemical feed (3)
/ / Ferrous sulfate, Capacity unknown
Mixing basins (2)
Volume - 190 m3 each
Detention time - 30 min
Recarbonation chamber (2)
Volume - 62 m3 each
•* O Chlorination
Capacity - 68.2 kg/d
IM nFilters (6)
6.10 m X 5.49 m X 2.44 m each
Area - 33.4 m2 each
-J LJ LJ Capacity - 3920 m3/d each
..__ —
,(, 1 I r-i _.,«,„ i i .r.
J-. 1^ 1 1 High service pumps (5)
f 1)( 2 )O)©(5) #1 - Capacity - 176.6 1/s
V-XVj-y V' T T #2 - Capacity - 176.6 1/s
1 1 1 1 1 « - Caoarifv - RR.3 1/s
Oc
#4 - Capacity - 50.5 1/s
#5 (Auxiliary) - Capacity unknown
0 Elevated storage
Volume - 1890 m3 each
PARAMETER
Ra226
6.61
6.15
4.78
4.91
12.97
5.57
0.75
%
86.5
AND REMOVAL EFFICIENCY
Gross
Alpha
21.9
14.3
15.7
15.9
54.5
17
10.9
%
35.9
Hard-
ness
254
238
253
248
236
242
102
7.
57.8
Figure U-7 Elgin Flow Schematic
Distribution
- 87 -
-------
Elgin (Slade Avenue Plant)
Raw Water Reservoir
Location: Slade Avenue Plant, under building
Construction: Concrete
Dimensions: 15.24m x 18.29m x 3.35m (50r x 60' x 11')
Capacity: 934 388* ( .25MG)
Vents; 2 Vents - North
1 Vent - East side
Water Meters
Raw Water Meters
Quantity: 2
Manufacturer: Simplex Valve and Meter Company
Model: Venturi MT
Size: 40.6 cm tube x 24.1 cm throat (16" x 9.5")
Serial Numbers: #16-264-4339 and #16-309-5084 MT
Measures flow in MOD, 0 to 8.0 MGD (0 to 30.283 x 106L)
Records flow as gallons
Circular disc belt
Floor-mounted
Low Service Pumps
PUMP DATA
Type: Vertical turbine
Quantity: 3
Manufacturer: Aurora pump
Serial Number: #83923, #83924
Capacity: 113.56Vc @ 10.06m, 132.49Vs § 12.19m & 72.55 @ 12.19m
(1800 gpm @ 33', 2100 gpm @ 40', 1150gpm @ 40' respective)
Takes Suction From: Raw water reservoir
Discharges To: Aerators
DRIVER DATA
Type: Electric motor
Manufacturer: U.S. motors
Model: Type CFU
Serial Numbers: #155320, #975157, #971239
Power: 18659W, 29840W, 29840W (25hp, 40hp, 4Chp)
Angular velocity: 188.5 rad/s (1800RPM),. 125.6 rad/s (1200 RFM),
125.6 rad/s (1200 RPM)
Electrical Requirements: 3ph, 60Hz
-88-
-------
Aerators
Location: Base of aerators are on second floor of plant over the
settling basin
Type: Root blowers with nozzles to diffuse
Quantity: two
Construction: Concrete
Dimensions: 4.57m x 13.41m x 2.44m (15' x 44' x 8' depth)
Area:
Capacity:
Blower: Rotary Lobe Blower, Serial No. 708055
Dresser Industries, Vacuum Pump Division
Chemical Feeder
Location: Chemical room at Slade Avenue Treatment Plant
Quantity: Two
Chemical : Lime
Type: Lime slaker
Serial Number: #83644-1, #83644-2, Model No. 41-02
Manufacturer: B.I.F. Omega
Fed From: Overhead hopper
Injects To: Mixing basin
Chemical Feeder
Location: Chemical room at Slade Avenue Treatment Plant
Quantity: three
Type: Omega Universal Volumetric Feeder
Model #UF-3, Serial # U-3864
dry feeder injects ferrous sulfate
Manufacturer: Omega
Capacity:
Fed From:
Injects To: Mixing basin
1 - out of service
2 - feed a mixture of ferrous sulfate and aluminum sulfate hand-mixed
Mixing Basin
Location: Under the aerator
Quantity: Two
Construction: Concrete
Dimensions: 6.71m x 6.71m x 4.27m (22' x 22' x 14')
Volume: 190,0005, ( 50,000 gal. )
Manhole:
Agitator:
Capacity:
Detention Time: 1800S
Sludge Removal: Walker Process continuous sludge removal equipment
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Recarbonator
Location: Chemical room
Quantity: Two
Type: Carbal unit; Manufactures C02 from city gas
Serial Number: #20/2161, #20/1603
Manufacturer: Walker Process
Capacity:
Fed From: City gas line
Injects To: Recarbonation chanber
Recarbonation Chamber
Location: North end of clariflow
Quantity: Two
Construction: Concrete
Dimensions: 1.98m x 6.71, x 4.72m (6|' x 22' x 15s')
Volume: 62,OOOL (16,000 gal.) each
Manhole:
Filters
Location: Second floor filter room
Quantity: Four
Type: Rapid sand filters, gravity
Dimensions: 6.10m x 5.49m x 2.44m (20T x 18' x 8')
Filter Area: 33.44m2 (360 ft.'-) each
Capacity: 4.73 x 106Vd each @ 1.358 Vm2/s (1.25 MOD each % 2gpm/ft2)
Filter Media: Sand and gravel
Backwash: Manual using finished water
Waste Water: To sludge lagoon
Filters
Location: Second floor filter room
Quantity: Two
Type: Rapid sand filters, gravity
Dimensions: 6.10m x 5.49m x 2.44m (20' x 18' x 8')
Filter Area: 33.44m2 (360 ft.2) each
Capacity: 3.03 x 106 S,/d each @ 1.358 Vm2/s (0.8 MGD each @ 2gpm/ft.")
Filter Media: Sand and gravel
Backwash: Manual using finished water
Waste Water: To sludge lagoon. Clean water discharged to the
Fox River
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Wash Water Pump
Location: First floor, pump room
PUMP DATA
Type: Single stage, horizontal drive, centrifugal
Manufacturer: Aurora pump
Capacity: 378.5 Vs (6000 gpm)
Head:
Takes Suction From: Clear water reservoir
DRIVER
Type: Induction motor
Style: 50N417
Serial: 1S50N417
Power: 55,950W (75 HP)
Angular Velocity: 12,145 rad/s (.1160 RPM)
Electrical Requirements: 3ph, 60Hz
Clear Water Reservoirs
Location: South of Slade Avenue Treatment Plant
Quantity: Two round, one square, interconnected
Construction: Concrete
Round:
Dimensions: 27.43m dia x 6.40m deep (90* diameter x 21')
Capacity: 3.78 x 106 £ (l MG) each
Vents: One each
'Square:
Dimensions:
Capacity: 7.57 x 106 I (2 MG)
Vents: One
High Service Pump
Location: First floor pump room
PUMP DATA
Type: Single state, horizontal drive, centrifugal pump
Manufacturer: American Well Works, Aurora Pump
Capacity: 176.6 Vs (2800 gpm)
Head:
Takes Suction From: Clear water reservoirs
Discharges To: Distribution
DRIVER DATA
Type: Induction motor
Manufacturer: General Electric
Model No. 95#587G1
Serial No. 5286770
Power: 149,200W (200 HP)
Angular Velocity: 186.9 rad/s (1785 RPM)
Electrical Requirements: 3ph, 60Hz
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High Service Pump
Location: First floor, pump room
PUMP DATA
Type: Single stage, horizontal drive, centrifugal
Manufacturer: American Well Works, Aurora
Capacity: 176.6 SL/s (2800 gpm)
Head: 60.96m (200T )
Takes Suction From: Clear water reservoirs
Discharges To: Distribution
DRIVER
Type: Induction motor
Manufacturer: General Electric
Model No: 95E587G1
Serial No: 5286769
Power: 149,200W (200 HP)
Angular Velocity: 186.9 rad/s (1785 RPM)
Electrical Requirements: 3ph, 60Hz
High Service Pump
Location: First floor, pump room
PUMP DATA
Type: Single stage, horizontal drive, centrifugal
Manufacturer: American Well Works, Aurora, Illinois
Capacity: 88.3^/s (1400 gpm)
Head:
Takes Suction From: Clear water reservoirs
Discharges To: Distribution
DRIVER
Type: Induction Motor
Manufacturer: General Electric
Model: 943350G1
Serial: 5311356
Power: 74600W (100 HP)
Angular Velocity: 186.4 rad/s (1780 RPM)
Electrical Requirements: 3ph, 60Hz
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High Service Pump
Location: First floor, pump room
PUMP DATA
Type: Single stage, horizontal drive, centrifugal
Manufacturer: American Well Works, Aurora, Illinois
Capacity: 50.5 SL/s (800 gpm)
Head:
Takes Suction From: Clear water reservoirs
Discharge To: Distribution
DRIVER
Type: Induction Motor
Manufacturer: General Electric
Model: 5 KF505CG1
Serial: 5311371
Power: 4-4760W (60 HP)
Angular Velocity: 185.8 rad/s (1775 RPM)
Electrical Requirements: 3ph, 60Hz
Auxiliary High Service Pump
Location: First floor pump room
PUMP DATA
Type: Single stage, horizontal drive, centrifugal
Manufacturer: American Well Works, Aurora, Illinois
Model: 8071
Capacity:
Head:
Takes Suction From: Clear water reservoirs
Discharge To: Distribution
DRIVER
Type: Six cylinder gasoline engine
Manufacturer: Climax
-93-
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Auxiliary Power, Engine - Generator Set
Location: First floor, pump room
GENERATOR DATA
Type:
Manufacturer: E - M
Power: Can operate one well and one booster pump, and chemcial feeders.
DRIVER
Type: 8 cylinder gasoline engine
Manufacturer: Climax
Model: R8l
Number: 18033
Gas Chlorinator
Location: First floor chlorinator room on west side of building
Manufacturer: Wallace & Tiernan
Type: V-notch variable-orifice, free-standing, vacuum operated, solution feed.
Model: A-751
Serial: #DD-15798
Capacity: 181.8 kg/d (4-00 ppd)
Chlorine Source: Five 68Kg (150 Lb. ) cylinders on a platform scale
Booster Pump: None - operates off water main pressure
Injects To: Prechlorination
Gas Chlorinator
Location: First floor chlorinator room on west side of building
Manufacturer: Wallace & Tiernan
Type: V-notch, variable-orifice
Model: A7331132
Serial No.: #JJ3098
Capacity: 68.2 kg/d (l50ppd)
Chlorine Source: Five 68kg (150 Ib.) cylinders on a platform scale
Booster Pump:
Injects To: Post-chlorination
Chemical Feeder
Location: Room on first floor on east side
Quantity: One
Chemical: Hydrofluosilicic acid
Type: Proportional displacement chemical feed puirp
Model: No. 12101-11
Serial No.: #6705305
Electrical Requirements: 115 volt, 20 amp. 50/60 Hz frequency
Manufacturer: Precision Control Products, Inc.,
Capacity:
Fed From: Plastic tank
Injects To: Filter effluent
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Water Meters - Finished Water Meters
Quantity: Two
Manufacturers: Builders - Providence, Inc.
Model:
Size:
Measures Flow in 1000 gal. (3?85£)
Records flow as gallons
Round flat chart and counter
Records flow as gallons
Wall-mounted
-95-
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0> 'c
< l-t
SW
3
- 96 -
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- 97 -
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APPENDIX E
LYNWOOD
-98-
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Lynwood - Water Treatment Plant
Top of Unit #1 - Used for
collecting resin sample
Well discharge to soft^ntr^ unit;
Figure E-l Scenes at Lynwood Water Treatment Plant
-99-
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Well
Softener-Unit //I & Sampling Point (.Arrow)
Side view of Softener Units - Front Back wash discharge & drain
Figure E-l Scenes at Lynwood Water Treatment Plant
-100-
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S up ply: Lynwood
Item:
Well #2
Location: 782.7m North, 762.0m East of the
SW Corner of Sec. 7, T 35N, R 15
Cook County
Pump: Johnson Turbine
63.1 L/s @ 249.9m,
Set at 228.6m
Motor: U. S. Motors Holloshaft
223,800W
Chronology: Drilled in 1972 by
Wehling Well Works
Production Data
Date
Static Level, m
Pumping Level, m
Pumping Rate, i/s
Specific Capacity
1972
120.4
153.9
62.4
1.86
iZ.JM^^LL
Cla-
i. ifrtfi 1-ont?
0,1 d
)ti.»m
t~l*n£3 Ton
Iff -I r*
fat Sr*i
n e
-fo.tc.i~r
- 101 -
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Well #2 - 556.9 m deep
Pump capacity - 63.1 1/s
Sand separator
0.46 ra dia X 2.74 m long
Capacity - 44.2 to 75.7 I./s
Ion exchange softeners (.))
2.29 m dia X 2.29 m high
Capacity - 146.84 kg each
c
I
Distri
* (__) Chlorination
Capacity - 45.4 kg/d
^N. Booster pump
J Capacity - 75. 7 1/s
SNV Elevated storage
\ Volume - 2839 m3
\ Height - 32.9 m
Dution
PARAMETER AND REMOVAL EFFICIENCY
Ra226
14.7
1.8
%
87.7
Gross
Alpha
111.8
11.7
7.
89.5
Hard-
ness
848
78
%
90.8
- 102 -
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Lyriwood
Sand Separator (Desander)
Location: Pumphouse. Near Well #2
Manufacturer: Laval Separator Corporation, Fresno, California
Type: Industrial Separator
Model No.: 1S87012
Capacity: 44.2 Vs to 75.7 i/s (700 - 1200 gpm)
Dimensions: .46m dia x 2.74m long (18" dia x 9' long)
Function: Separation of sand from the water
Air Compressor
Location: Pumphouse East of Well #2
Make: Quincy
Model: HKF - 81114L
Size: 8.89 cm x 7.62 cm (3i" x 3")
Pressure: 1.379 x 106 N/m2 (200 psig)
Tank: 227.In (60 gal.) Horizontal
Motor Manufacturer: General Electric
Motor Power: 2238W (3 HP)
Angular Velocity: 183.75 rad/s (1755 RPM)
Electrical Requirements: 3 ph, 60 Hz, 230-460V
Function: Pneumatic Valve Control for Softening Unit
Softening Unit
Location: Pumphouse
Manufacturer: Permutit Company, Paramus, New Jersey
Type: "Progressive Mode Ion Exhange"
No. of Components: Three (3) sub units
Dimensions: 2.29m (90") diameter x 2.29m (7'6") straight shellheight
Under Drain: Double dish
Softening Medium: Permutit Q-102
Volume: 3 at 5.83m^ (206 ft^ )
Bed Depth: 1.35m (53")
Rising Space: .94m (37")
Capacity Rating: 25.19 kg/m^ (11 Kgrains/ftJ)
Total Capacity: 3 x 146.84 kg (2266 Kgrains )
Brine Pump
Number: Two (one spare)
Make: Marlow
Model: 14HEL-9 / 14HEL-9
Serial: 523664/523667
Capacity: 1.26 Vs (20 gpm)
Operation: Automatic
Pumps From: Brine pit
Discharges To: Softener (during regeneration)
- 103 -
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Brine Tank (pit)
Location: Southwest of pumphouse
Construction: Concrete
Dimensions: 4.57m x 3.96m x 3-05ia (15 ft. x 13 ft. x 10 ft.
Master Meter
Manufacturer: Badger
Type: "Easy Read"
Serial No.: 12019567
Operation: Electrical
Read Out: Visual (digital) and recorded on chart. (Recorder not
operating)
Booster Pump
Manufacturer: Weinman Pump, Coluribus, Ohio
Type: Split Case - Centrifugal - Double Suction
Model No.: 6638U 5L1
Capacity: 75.7 t/s (1200 gpm)
Motor: Lincoln
Motor Power: 55.95 kw
Electrical Requirements: 3ph, 60Hz
Serial No.: 022401
Suction From: Softener Discharge
Discharges To: Elevated tower and distribution system
Elevated Tank
Location: West edge of subdivision
Manufacturer: Chicago Bridge and Iron Company
Type: Fluted pedestal tank
Material: Steel ,
Capacity: 2.839 x 106 *> (750,000 gal.)
Working Waterhead: 32.92m - 42.67m (108 ft. to 140 ft.)
Gas Chlorinator
Location: Separate room southeast corner of pumphouse
Manufacturer: Wallace and Tiernan
Type: V-notch - pneumatic feed (U-22341)
Capacity: 45.4 kg/d (100 ppd)
Serial: TT-1359
Booster Pump: Aurora turbine
Pump Capacity:
Maximum Pressure: 8%350N/m (130 psi )
Scales: Wallace & Tiernan (Platform-dual)
Chlorine Cylinders: (2) 68kg (150 Ib, )
Ventilation: Fan near floor
- 104 -
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Testing Equipment
Location: At pumphouse
Chlorine: Wallace & Tiernan colorimeter
Hardness: Hach Titrimetric
Fe, pH: Hach Spectrophotometer
-105-
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^ o
- 106 -
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ACKNOWLEDGEMENTS
The Illinois Environmental Protection Agency, Division of Public Water
Supplies wishes to thank the personnel at Dwight Correctional Center,
Peru, Herscher, Elgin and Lynwood for their cooperation and assistance
during the sampling and the field survey; and to Dr. William Brinck
for his assistance in making the field survey measurements.
-108-
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TECHNICAL REPORT DATA
(Please read Instructions on the reverse before completing)
1 REPORT NO.
ORP/TAD-76-2
4. TITLE AND SUBTITLE
Determination of Radium Removal Efficiencies in
Illinois Water Supply Treatment Processes
6. PERFORMING ORGANIZATION CODE
3. RECIPIENT'S ACCESSION"NO.
5 REPORT DATE
May 1976
7. AUTHOR(S)
Dorothy L. Bennett, Charles R. Bell, Ira M. Markwood
8. PERFORMING ORGANIZATION REPORT NO.
ORP/TAD-76-2
9. PERFORMING ORGANIZATION NAME AND ADDRESS
Illinois Environmental Protection Agency
Division of Public Water Supplies
2200 Churchill Road
Springfield, IL 62706
10. PROGRAM ELEMENT NO.
11. CONTRACT/GRANT NO.
68-03-2088
12. SPONSORING AGENCY NAME AND ADDRESS
13. TYPE OF REPORT AND PERIOD COVERED
U.S. Environmental Protection Agency
Office of Radiation Programs
Washington, D. C. 20460
14. SPONSORING AGENCY CODE
EPA-ORP
15. SUPPLEMENTARY NOTES
16. ABSTRACT
Five water supplies which were known to have radium-226 in the raw water
(ranging from 3.3 to 14.7 pCi/1) and which have existing water softening equipment
were chosen to determine the efficiency of radium removal. Plants using ion ex-
change and lime water softening processes were investigated.
At the plants using ion exchange softening, samples of raw, aerated, and
softened water were collected, analyzed for radium-226 and mineral content, and
the radium removal efficiency was calculated. At the plants using lime softening,
samples of raw and filtered water were analyzed. All plants were operated in a
normal manner during sampling.
In general, the ion exchange softening removed the radium-226 more efficiently
with 70.2 to 98.2% being removed as compared to 70 to 92% for lime softening.
Although the removal efficiency was somewhat lower using lime softening, it was
more consistent since the problem of breakthrough at the end of a softener run
was not experienced and little or no blend water is required to produce a stable
produect.
17.
KEY WORDS AND DOCUMENT ANALYSIS
DESCRIPTORS
b.IDENTIFIERS/OPEN ENDED TERMS
COS AT I Field/Group
Water, Treatment, Removal
Radioactivity, Radium
Potable Water
Natural Radioactivity
Water Treatment
Chemical Removal
18. DISTRIBUTION STATEMENT
19. SECURITY CLASS (This Report)
unclassified
21. NO. OF PAGES
20. SECURITY CLASS (Thispage)
unclassified
22. PRICE
EPA Form 2220-1 (9-73)
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