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PLACE IN RETURN BOX to remove this checkout from your record.
TO AVOID FINES return on or before date due.
MAY BE RECALLED with earlier due date if requested.

At9r£123126h59_
_-
_-
--
_-

DATE DUE

6/07 p:lClRC/DaleDue.indd—p.1

 

A Comparison of an Activated Sludge and a
Trickling Filter Sewage Disposal Plant

for

Charlotte, Michigan

A Thesis Submitted to

The Faculty of
MICHIGAN STATE COLLEGE
of
AGRICULTURE AND APPLIED SCIENCE

by
U \‘M
R. J{ Theron: I. B: Raff

Candidates for the Degree of

Bachelor of Science

June 1942

 

;

“771,4/ ///

Present Sewer System

 

Charlotte is served with a separate sanitary sewer
system. There are an undetermined number of roof gutters
connected to this sanitary sewer. Immediately before
entering the plant, the sewage can be diverted directly
to the river by means of a man hole at the plant site.

Nearly 100% of the city is connected to the sanitary
sewer, which operates completely by gravity. The entire
sewage arrives at the plant in a single 18" conduit.

The Present Sewage Treatment Plant

 

General Description

The Charlotte sewage treatment plant is of the primary
type, consisting of a bar rack, primary settling tank, float-
ing cover sludge digestor, and glass covered sludge drying
beds. The effluent from the settling tank discharges into
the Battle Creek river.

The present plant was built and placed in Operation in
1934. Its purpose was to removetpart of the suspended solids
and discharge the remainder of the suspended solids and dis-
solved solids into the river. This type of plant should
remove about 30 to 50 percent of organic solids. This, ob-
viously, leaves the preponderance of the solids to be dis-
charged into the river. Additional treatment is necessary
to stabilize the organic matter, making the effluent such

that it will not polute the river.

1433.05

Detailed Description

The sewage enters the plant site in an 18 inch sewer,
discharging into a manhole from which it can be diverted direct-
ly to the river or can be passed through the plant. If sewage
is passed through the plant, the sewage enters the control
building through an 18 inch sewer and immediately passes through
a rack, Which has clear openings of one inch. The sewage then
passes out of the building in an 18 inch sewer and emptys into
the primary tank.

The primary tank is 47 feet long, 14 feet wide, and has a
10 foot depth of sewage. The floor of the tank slopes down
toward the influent end of the tank where are located hoppers
for the accumulation of the sludge. The sludge is brought
down the sloping floor into the sludge hoppers by means of a
scraping and skimming mechanism. This mechanism is power
driven and consists of two endless chains to which are fastened
wooden flights which move along the bottom and along the sewage
surface in the tank. The sewage is distributed when entering
the tank by means of an adjustable wooden baffle placed immed-
iately in front of the influent pipe. The sewage then flows
to the other end of the tank where the effluent flows over a
weir into the effluent channel from which it passes into a
15 inch pipe and is discharged into the Battle Creek river.
Near the effluent and of the primary is the scum trough. The
scum is accumulated in front of the scum trough by the skim-
ming mechanism. This scum is periodically raked into the scum

trough from which it is flushed out by a hose into a pit from

where it is pumped to the sludge digestor. The sludge col-
lected in the hoppers is pumped by a sludge pump through an
8 inch line directly into the sludge digestion tank, and is
pumped twice a day for approximately thirty minutes at a
time.

The sludge digestion tank round, has a diameter of 28
feet and accommodates a 9 foot depth of sludge. It has a
floating cover which rises and falls with variations in the
amount of gas produced by decomposition of the organic matter
in the sludge. As the sludge is pumped into the digestor, it
displaces an equal amount of supernatent which can be taken
from any desired level by means of pipe arrangements in the
tank. The supernatent from the tank is passed into the raw
sewage manhole at the beginning of the process.

A glass covered sludge bed has been provided for the
drying of the digested sludge which has an area of 2700
square feet. The sludge from the digestor flows by gravity
to the sludge bed. The sludge bed consists of a graded sand
and gravel floor underlaid by tile which conducts the liquid
from the sludge to the effluent pipe of the primary tank.

The gas that collects in the digestor is piped to the
control building where it is burned for the purpose of
heating the digestor tank and control building. There is
also provided an oil burner that can be used in case the

gas produced is insufficient.

Treatment Accomplished

 

 

A primary treatment plant of this nature can be expected

to remove from 30 to 80 percent of the organic solids and

this plant removes less than 20 percent of the solids.

Chemical analysis of the influent and effluent of the

plant are given in Table No. 1.

Table No. 1
Chemical Analysis
April 16, 1942

(Values in p.p.m.)

 

suspended Loss on Total
Solids Ignition Solids

Loss on 5 Day
wignition B.O.D.

 

 

 

 

 

Influent 168 133.3 685 343 328
2 PM-l AM .
Effluent 98 86 650 338 168
3 PM-l AM
% Reduction 41.1 35.3 26.3
Influent 124.6 106.6 585 392 138
3 AM-l PM
Effluent 83 73 545 276 87.3
3 AM-l PM
% Reduction 33.3 32.8 61.5

 

The following tabulation, Table No. 2, gives the values

of different types of sewage and the average of the Charlotte

plant.

-5—

Table No. 2
Strength of Sewage
(Values in p.p.m.)

 

Total Loss on Suspended 5 Day

 

 

 

 

Item Solids Ignition Solids B.O.D.

Weak Sewage Less than Less than Less than Less then
850 325 175 150
Medium Stg. 800-1000 300-500 150-850 125-235
Sewage

Strong 950 plus 460 plus 225 plus 800 plus
Sewage
Charlotte 640 310 146 180
4-16-1943 '

 

The values in Table No. 3 shows that the sewage is of a '

weak to medium strength.

 

 

lorulfition

 

Any sewage rlnnt must be desinged to herdle the nnticiroted
flow for some future flute. A common practice is to design on

the bseis of the population expected in twenty veers.

TLBTE 5

lilPPIuJEICfiT O}‘(3I?£{LOTWKE, 11??017(30UI?fY

Year Population
1390 5867

1940

4fl95
4:88 6
5196
5507

5354-4

In table No. 5 is shown the population of Charlotte for
the 19st 60 years. These values were plotted on a graph and
the curve extended to include the year 1902, as shown in Fir.
No. 1. According to this curve the population should be 6110
in the year 1962. This is a relatively small increase for the
twenty yesr period. Charlotte at the present is a typical small
rural community, with several industries being present. Although

the population of such communities 18 is fairly constant, here

of its industries expending, or

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of nevrindustrios being developed, which could cause a large

pouulation increase. For this reason it is advisable to arbitrar-

ily add a safety factor to the future nooulat on estimate. The

1962 population res therefore estimated to be 7000 persons, as

a design basis.

TABLJL‘ 5

Charlotte Serese Flow on Anril 16, 1942.

 

£2212 Heisht L - .2h Heed C.F.S. G.P.U.
2IHI 2.07' .72' .52' .900 404
5 2.07 .72 .52 .900 404
4 (.08 .72 .51 .878 594
5 2.10 .72 .49 .821 569
6 2.09 .72 .50 .849 581
7 {.11 .72 .48 .788 554
8 2.15 .75 .46 .759 241
9 2.17 .74 .42 .675 "02
10 2.15 .75 .44 .708 518

11 2.18 .74 .41 .646 291
12 2.12 .75 .47 .781 551

1 AM 2.18 .74 .41 .646 291

2 2.21 .74 .58 .577 259
5 2.24 .75 .55 .518 255
4 2.26 .75 ..55 .475 212
5 2.26 .75 .55 .475 212

2.2. .75 .54 .495 222
2.15 .75 .46 .759 241

.75 .57 .562 252

to C) Q 03
‘3
o
0'3
\3

2.15 .75 .44 .708 518
10 2.11 .72 .48 .788 554
11 2.08 .72 .51 .878 594
12 2.09 .72 .50 .849 581
1 PM 2.06 .72 .55 .925 415

Average Flow = 325 G.P.M. - 468000 pe1./dey.

.|.|k‘l\ :I 1

ALIJILJ hi
1 .. , 41

I. {I ‘lvl

 

f; (an-m be 1210...

 

Charlotte has a scncrote sanitary sewer system. The sewace
flovris derived from_thc nublic rater susnly, cround rntcr in-
filtration (if any), and runoff from roof Putters durine storms.
Table No. A shove the veter numnsce for the year 1941.

TABLE 4

water lunnare Record for‘1941

fionth ca1./day Lonth cel./day
Jan. 647000 July 861000
Feb. 655000 Au”. 896000
Kdrch 692000 Sent. 57000
Anril 668000 Oct. 752000
Ifiay' 687000 Novu 704000
June 709000 Dec. 650000

Table No. 5 shovs the measured serene flovrat the nlant on
Anril 16, l9i2. As “ill be noted, this measured flow is consid-
erably less then the normal veter nunnene records. Since all of
the senses nesses thru the slant, this indicates that there is
either an error in the Water numnese records due to excessive
slinnase, or there are important leaks in the water distribut-
.

ion systmn.

Kethod of Treatment

 

Present nractice amend sanitary'ensineers is divided be-
treen two systems of final treatment of sewape. One is the act-
ivated sludse process, and the other is the tricklind filter

UI‘OCBSS o

Since the desienine encincer is usuelly faced with the
necessity for desidine which of these methods to use, both
“fig-:«ruuw’
tynes of treatment rill be investigated in the following treet-

ise in order to afford a comparison of the relative merits of

L)

each.

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menthtion tank find is prern to tfie
box. Esra the 930933 activ:tef sltfl
goes to the primiry Ftttling tank

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tion of F hours, tfla diqg°3n
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Gos

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AZT?TC t»r* flurizg coldost veitVir, daily hoof loss from

taxks : lCOF.

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order to measure the so ago flow. It will be con octefi to a

continuous recorflor device.

 

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TF 1

Trickling Filter Process

The Trickling Filter process is the treatment of sewage
by applying it upon a bed of stone in order to obtain oxida-
tion of the organic matter in it. There are two types of
trickling filter processes, the standard rate and rapid rate
filter. The standard rate filter is, up to the present time,
the most widely used of the two, and in this type of filter
the sewage is applied at a rate of about 300,000 gallons per
acre foot per day and does not require the recirculation of
any effluent, while the rapid rate filter applies between
25,000,000 and 30,000,000 gallons per acre foot per day and
has to recirculate at low flow the necessary effluent to
maintain this rate. The trickling filter is an oxidizing
device, whose function is to oxidize as much as possible
the organic matter of the sewage. This is done by applying
the sewage as uniformly as possible over a bed of stone of
various sizes ranging from 1% to 3% inches in diameter which
are placed in a bed 6 to 8 feet deep. It can be seen from
the large size of the stone that they do not act as a screen
or strainer for the suspended matter or other impurities of
the sewage. Purification is obtained by the formation on
the stone of a thin organic surface of slime containing bac-
teria. The sewage flows over this slimy surface and the
oxidizing bacteria accomplish the process of oxidation with
the help of the available air that is in the voids of the
bed. Due to the periodic slushing off of the slimy surface,
it is necessary that the effluent from the filter pass

through a final sedimentation tank.

TF 8

Operation g£_proposed trickling filter system

 

 

In the new system, the sewage will pass through the
coarse racks, as at present, but before it is placed in
the primary settling tank, it will pass through a grit
chamber. The function of the grit chamber will be to re-
move the heavier solids such as sand and gravel that are
washed into the system during heavy rains. The chamber
shall be connected so that during very low flows or when
it is desired to clean out the accumulations of grit, the
sewage may be by-passed directly to the primary settling
tank. The primary settling tank will Operate as at the
present time. The effluent from primary settling tanks
will go into a sump pit where it will be pumped to a dos-
ing tank. There will be two pumps, one that will contin-
uously operate at normal flow and the other will Operate
intermittently during high flow. At the sump pit there
will be a possibility of by-passing the secondary treat-
ment if the occasion arises. From the dosing tank the
sewage will be sprayed upon the bed of stone by the re-
actionary type of rotary distributor. The rotary distrib-
utor is considered by present day engineers to be the
standard method of distributing sewage in trickling filter,
due to the high degree of efficiency obtained. The sewage
will pass from the filter bed to the center of a round
final sedimentation tank. At the center it will flow from
the bottom of a vertical pipe with a radially outward and
upward direction to the weir on the outside of the tank

TF 3

and then into the effluent channel.

The vertical-flow tanks are particularly adapted to
the clarificatiomxof the effluent of trickling filters,
due to the reduction of contact time between the liquid
and the sludge. If contact time is quite long, the sludge
reduces the quantity of dissolved oxygen from the effluent
which is not desirable because a high dissolved oxygen
content in the final effluent is one of the goals in the
treatment of sewage.

From the final sedimentation tank, the effluent will
go through a chlorination tank. The chlorination tank will
be designed so that the sewage may pass directly through
without chlorination, or may go around the baffled tank
and be chlorinated when desired or directed by the State
Health Department.

The sludge in the final tank will be forced by a mech-
anical scrapper to a pit at the center and may be removed
without emptying the tank, therefore, making it a continu—
ously operating unit. The sludge from the final tank is
returned to the influent channel of the primary settling
tank. It will then go through the complete process again,
with the majority of the final tank sludge settling out in
the primary tank. The sludge from the final tank will be
delivered to the primary influent by gravity due to the
hydrostatic pressure existing above it.

The sludge from the primary tank will be pumped into
the sludge digestors. The sludge digestors shall be con-

nected together so that they may be used in parallel or

TF 4

series as the plant operator desires. The new tank shall
have a fixed cover and the floating cover tank shall act
as gas storage for both. The digested sludge will flow
by gravity from either tank into the covered sludge bed

or the new proposed open sludge bed.

Summary of Design Date

Grit Chamber

 

The grit chamber shall have a velocity of one foot
per second and a detenticn of one minute, therefore, the
length will be 60 feet.

The area required for an average flow is A = .915 =

.915 square feet, with a width of 12 inches, d = .915

 

.915 feet.

Primary Tank ,

 

The present tank will be used without any changes.
With a design flow of 592,000 gallons per day, the detention
period will be T =.§§g8 = 2 hours and 14 minutes. As recom-
mended in Metcalf and Eddy, Page 573, the surface area,
A : égggggg = 900 gallons per square foot per day, will be
sufficient.

Sump

The sump shall have one pump operate continuously at
average flow and an auxiliary pump operate at higher flows.
At the avera e flow, a pump of size = 592 000 = 400 g.p.m.

g 21 x 60
shall be required. The auxiliary pump shall be 618 - 400 3

218 g.p.m. and for a safety factor a 850 g.p.m. pump shall

TF 5

be used. The sump will be square with 6 feet on a side. The
400 g.p.m. pump shall have a drawing depth of 1% feet, and
the 250 g.p.m. pump a 1 foot drawing depth.

At average and maximum flow the 400 g.p.m. pump shall
operate continuously, while at low flow, it will operate
for 2 minutes and 5 seconds, and be off for 1 minute and 58
seconds. The 250 g.p.m. pump will operate for 2 minutes

and 4 seconds and be off for 44 seconds at maximum flow.

Siphon Tank

 

The siphon tank will be square and have a surface area
of 100 square feet. In order to have the siphon tank empty
at maximum flow, the maximum flow will be increased by 20%.
The discharge from the siphon will than equal 1.38 X 1.2 =
1.88 c.f.s., and the tank will have a drawing depth of 3
feet. This tank will empty in 3 minutes and 40 seconds when
400 g.p.m. is entering and will fill up again in 5% minutes.
At an inflow of 750 g.p.m., it will empty in 8% minutes and

fill up again in 3 minutes.

Filter Bed
With the normal rate of application of 300,000 gallons

per acre foot per day and a 7 foot depth, the size of filter
92 000 x 43 560

= 5 : 126 feet.
will equal D \f300f000‘i_7_i"77854

Using a 4 arm distributor, Q per arm =.Zg§ = 186 g.p.m.

 

With a 2 foot net head and 7/16" orifices, the number of

orifices = .lgg : 35. The area being covered by each
0

orifice will equal .7854 ( 1253 - 93) = 345 square feet.
56

 

TF 6

Final Tank

 

The final tank will have a 2 hour detention and be of

a circular type with sludge removing mschghism.

= 592, 000 x 2
VOlume ‘7.48 x 24

Size of unit with a 8. 81‘ average depth d JVé-Tasigg 81:

= 8590 cubic feet.

 

 

35.4 feet.

Chlorination Tank

 

This tank shall have a detention of 20 minutes and a.
velocity of .1 foot per second.

Volume = .915 x 80 x 20 - 1100 cubic feet.

With 8' depth, A =-l%99 = 183 square feet.

Size will equal 13.5' x 13.5' x 8‘ with baffles spaced

at 1.52 feet apart.

Sludge Digestion Tank

 

2
Volume of present tank - 9 x428.3 x 3.14 a 5880 cu. ft.,

 

This allows for a volume of .81 cubic feet per person, which
is not considered sufficientx Using a desired 2% cubic feet
per person, the volume will equal 17,500 cubic feet. The dia-

meter of the tank necessary using a 15 foot depth equals

 

 

x 11,840 _
3.14 x 9 _ 32 feet.

Sludge Beds

 

The present beds, which are glass covered, have an area
of 2,870 square feet. This area will serve 5,340 people and
the additional area required will be 7,000 - 5,340 - 1880
square feet. With two beds at 15' x 55' this is accomplished.

TF 7

Heating Equipment

 

Additional heating equipment will be installed in the
present building that will utilize the gas produced in the

sludge digestors.

Meter
A venturi meter will be installed between the sump and
siphon box and will be connected to a continuous recorder

giving a record of plant flow at all times.

Laboratory

 

The present plant does not have any laboratory equip-
ment. For efficient operation it will be necessary to in-

stall laboratory equipment.

Miscellaneous

 

There shall also be installed a switch board, temper-

ature recorder for sludge tanks, and landscaping.

Cost Estimate
Grit Chamber

 

Concrete - 3 cu. yd. @ $35.00 105.00

Excavation - 7 cu. yd. @ $1.00 7.00 112.00
m

Pump - 400 g.p.m. 800.00

Pump - 250 g.p.m. 300.00

Concrete - 15.85 cu. yd. @ $35.00 554.00

Excavation - 28.5 @ $1.00 28.50

Sump Pump 40.00 1,522.50

 

TF 8

Filter Bed

 

Concrete - 382 cu. yd. @ $35.00
Excavation - 928 cu. yd. @ $1.00

Drainage Tile - 12402 sq. ft. @$.20.

Ballast - 3210 cu. yd. @ £3.50
Rotary Distributor

Final Settling Tank

 

Concrete - 53.1 cu. yd. @ $35.00
Excavation - 272 cu. yd. @ $1.00

Mechanism

Chlorination Tank

 

Concrete - 18 cu. yd. @ $35.00
Excavation - 53 cu. yd. @ $1.00

Digestor

 

Concrete - 125 cu. yd. @ $35.00

Excavation - 505 cu. yd. @ $1.00

Sludge Bed

 

Sand - 73 cu. yd. @ $1.50
Concrete - 13 cu. yd. @ $35.00
Gravel - 147 cu. yd. @ $1.00
Underdrains - 150' @ $.10

Miscellaneous

 

Venturi Meter
Laboratory and Office Equipment
Piping and Valves

12,890.00

928.00

2,480.40
11,240.00
1,400.00

1,880.00

272.00
900.00

830.00
53.00

4,380.00

505.00

110.00
455.00
147.00

15.00

800.00
700.00

28,736.40

3,032.00

883.00

4,885.00

727.00

TF 9

 

 

Landscaping 400.00

Electrical 800.00
Heating Equipment 800.00 3,500.00
Engineering and Contingencies §,OO0.0Q
TOTAL PLANT COST . . . . . . . 58,492.80

Operating Costs
Cost is based for flow of 500,000 g.p.d., and cost of
electrical power at $.02 a K.W.H.

Power - Kilowatt Hours

 

Sewage Pumps - 3 H.P. at 85% efficiency.

 

 

K.W.H. : -7Tg5xx3é53 53-4 = 54 54
Raw Sludge Pumps-3 H.P. @ 3 hours day 7
Final Settling Tank - 1 H.P. @ 24 hours ‘18
I TOTAL POWER . . . . . . . . . 79 K.W.H.
Cost
79 K.w.H. @ $.02 = $1.58 per day A 577/ yr.
Operator 2,000.00
Miscellaneous 200.00

TOTAL YEARLY COST FOR OPERATING . .2 2,777.00
Plant Cost @ 4% 2,540.00
TOTAL YEARLY COST . . . . 8 5,117.00

 

 

 

 

 

-9-

001-101; 53101:;

 

The foregoing analysis shows that the trickling filter
plant rpuld cost $58492 to build, vdth a total yearly capital-
ized cost, including operation, of $5147, whereas the activated
sludge plant would cost $55858 to build, with a capitalized
and Operating cost of $5400 per year. In other words, the trick—
ling filter plant would be much more costly to construct, but
the activated sludge plant, due primarily to the electricity
consumed by the aerators, rmuld.be much more expensive to 0p-
eratc. It should be recognized that the true cost of the pro-
ject is revealed by the capitalized and operating costs fig-
ure, which gives the total yearly expense of the project over
the design period of twenty years. However, to construct the
trickling filter plant rpuld necessitate an additional capi-
tal of $24858, which might easily be prohibitive.

Another factor to consider is that whereas the trickling.
filter plant may be expected to prOduoe an effluent with a
B.O.D. of less than 20p.p.m., the activated sludge plant
should reduce the B.O.D. to less than 12 p.p.m.. Either of
these results vould be satisfactory.

The trickling filter plant has an advantage over activat-
ed sludge in that it is less likely to be upset by an unusual
condition of the sewase. Often such conditions from the vaste
coming from certain industries,the presence of which is im-
possible to foresee. Also, activated sludge plants generally
reouire more skillful operation than do trickling filters.

The above mentioned factors, taken into consideration

 

-10..

with the financial condition and policy of the community in

suestion, should enable its sovcrninn body to some to s

L decis-
ion as to which type of sewnna treatment plant is the more

satisfactory.

   

 

 

Eff/vent Channc/
Sewage Surface
Sludge Mccbcwxsm

5f0f7c Bed

 

 

 

fiaff/cs 7

 

 

 

—-—_-—-—._ ._._.__ ——-—._——~
...—“v.— _. ——
.__‘_—.———-‘~—_——__.__.__——-~—————

 

 

 

   

 

 

 

KM
FILTER BED

CHLORINAI 03 FINAL. SETTLI N6 TANK

PROPOSED

FILTER BED

 

Potorg d/s fr/but‘or

 

PROPOSED
SLUDG E DIGESTOR

  
 

PRODOSED
SI PHON BOX

   

FLOATING
COVEB

O
[J O
O
SLUDGE'.
DIGESTOR

   

 

   

 

 

 

 

   

 

 

 

     

 

 

 

 

 

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Eff/(4233,15 Chtg’lfifle/ f/ < Baff/e S

 

 

 

 

 

 

 

 

PROPOSED
CHLORINE. BOX

 

 

PROPOSED
FINAL SETEING

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

LUMpsa SUMP

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PRIMARY SQTLING TANK

 

 

FLOW DIAGRAM

 

 

 

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Fma/ Eff/vent to P/yer

 

D/qesteoé Sludge

 

 

 

 

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my 3104”,: 707555755 INTAKE ' [I ____...._
CONTROL FIXED COVEB
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G_LASS COVERED
SLUDGE. BEE

FLOATING COVER OPEN SLUDGE BEDS

SLUDGE DIGESTOR

CITY OF CHARLOTTE".
EAION COUNTY

GENERAL PLAN OF SITE.

Date: 5-25' 42

 

Scale =~ I320.
Drawn =- B.-RQ'F'¥

 

 

Pro/DoseJAeraflbn 7517K S

 

 

 

Propos ed
Proposed Final TahK

C I: [or/hafion Tan?

Proposed Press/17‘
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||

 

 

 

 

 

III

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

6 u :4 cf/Vdfe d
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//t-'Proposec/
We? Well

released
614+ Chamber

 

 

 

 

 

(LP

 

 

 

 

 

Preset: 1" Co ”erec/

Sludge Bed

 

 

 

 

 

[8" Ouffall Sewer

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

LI___J_‘__I
\ ___ /

 

Pr- esenf‘ DH Ve way

/

 

ProposedACf/vafea’ Sludge Pump

Pr oposed ch‘ivafed
P d F" I T- K Sludge Dir/$10»? Box
rOFose r{no Oh \ W1. 883.30 [Pr/Mary Tank
J r #11:: v ,
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I: COHW'W’ House ._0 —-— ————— —Ql‘ ——’ 75 Primary S/udje Pam;

NJ.
PROF/LE OF/ICT/VA TED 5L UDGE

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

FLO ased
Proposed P waeaaao Proposed Wef Well ‘
- Ae 'on Tan/<5 WA. 8 .
2

MH.6 rWLS8L52 r ”L. 8822! , Primary M. H. 4 1
875.00 [I ‘ /° """" ‘— ‘Y‘

(— ' I ,_I
T R' e ( IL I V JI Corr/“rel House 87642 6% C d d
o w r PM“, , / m_%¢afl 375,.- \;f were 5w 96 Bed

I _/ .
Chlorinafion 7511‘ ~ Prefosed PUMP Room L— Dlyesfion TanK

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

-——~ —————

 

 

 

 

 

 

 

 

 

 

 

 

 

“In Cover- :2:

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

PROF/LE V/EW CHAPLO TTE SEWAGE
TREATMENT pLANT

PRE SENT é PROPOSED
PL/I N (S ELEV/I 77 ON

SCALE /"=~20' MAY, /942
ROBERT 'THEROUX

 

 

 

 

 

 

 

 

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