x, - 'u . v- ~
‘ .‘.:1'... ”4“ ‘ .It
. , ‘s “-1

"I
‘.‘ '

a
§. 0 .'

' 6.‘ :R':‘V~; 3" ‘
~ ' o ' I ‘ ' ‘ ‘ ‘ , . Q “ .' z ‘ L w... h ("if 'L‘? 5‘ ~ ‘;"

‘; -. ' .l ' . . I ‘. k‘ -I . ‘ A u I .2]. "fi‘cftflo "‘ ‘1
Y 4" '7' ._ ,. I“ .“ -- .u'.-'I~C"Hq‘.. .‘ ~
‘.]"\".g".' a; ‘ r VTE’ “a
“3'33: Wu ' '
‘ ,' ,y.
LVN‘ 0-5
I. Q

‘T:
55:21
.7 ' l”

D
s

a»!

V ‘é-

13:7.

f5 ‘.

q ,-
I‘m

m.-
‘J

u ‘5‘

'i; 3’5
"h- ~9-
. U

41‘

'e.”
,1

~ "J“

01.‘ . . , .., g“
‘j up: M: r?
.:l*‘-w.‘.':~.-‘fi 4-3

IN?" ”.Ifia‘fi‘d'.‘
3"»3' ' 5“

.J ‘
, .7 J H
I .»"'.:.'J- ”\é‘:'
‘ ' .'.‘:".-. ‘,
v- , ..

-r.,"‘~- . ‘
w u...“ ..;, 9' . -
’- Situh~u ‘K‘.
."‘I .’
: .-..::!~.h’.l~."a-. .
3“! ' i ‘ .fih-

‘ ‘ ~ I I ‘ I '\9
-. u. . o, . , , - ‘ ' fir‘. '-'

3:45... ‘31; Q .4 ‘h" . "u.“ ‘ _ I - " " '- ' " ' .ffi- ,\ “15:.

. ’y'..h

.‘nt _

o
... -. . . c

Q “h. 511‘}, I‘::~:";.'"'
h. . .tts ';'I§J‘O'

, . as. ‘
3'2." ”by '~.- 8 '
_-. u‘ c.
.

\s
‘p
N
h.
y‘a-
. \
, .. .
V.
~.
8

l.

,‘):(I‘
,t "

.‘ gfiw-zktg .

3h? ' .
t... ‘t:;‘ i-uutg
",~'~.' ' U ‘5'

,

. u. .
. “" 5w...
‘ is u

. ‘3 r.
." .. "\_
‘H; “‘suw

 

MCHIGAN STATE UNIVERSITY LIBRA

 

lllll/flllllllfllll II!!! III III! III llllI/Il/llflflllfil/lll

93 50026 1

 

 

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.

rem--

6/07 p:lClRC/DateDue.Indd-p.1

 

 

 

ooxoirrontno MUNICIPAL
WATER SUPPLIES

A Theeie Submitted to the
Faculty of the

Michigan State College,
Beet Lansing, Michigan.

by

Olaud Robert Erickson

Candidate for the Degree of
Civil Engineer
June, 193k.

THESIS

TABLE OF CONTENTS

Chapter I Methods of Conditioning Municipal
Water Supplies

Chapter II The Chemistry of Water Conditioning

Chapter III Standard Specifications for Chemicals
Used in Water Conditioning

Chapter IV Determination of Quantity of Chemical
Required

Chapter V The Dimensional Homogeneity and
- Dynamical Similarity of Models

Chapter VI Calculations for the Design of a
Lime-Soda Ash Treatment Plant

Chapter VII Calculations for the Design of a
Zeolite Treatment Plant

Chapter VIII Calculations for the Design of a
Lime Zeolite Treatment Plant

Chapter Ix Comparison of Investment and
Operating Costs

Chapter x Conclusions

95066

Page

1 - 29
30 - nu
#5 - 51
52 - 67
6s - 7o
71 - 89
9o - 9a
99 -106
107-121
122-123

METHODS OF CONDITIONING MUNICIPAL WATER SUPPLIES.
Chapter I.

It is the intention of this thesis to present in general
terms the methods used in the conditioning of municipal water
supplies. Three of the principal methods are discussed in
considerable detail, viz. lime-soda ash, zeolite, and lime-

zeolite.

There are three principal sources of water for a muni-
cipal supply, viz. surface (lakes, bays, rivers, etc.),
ground (from gravel or shallow wells) and deep well sup-
ply (water obtained below the glacial drift). Surface
water is usually turbid, may be colored varying with the
season, has a relatively small amount of scale forming
(hardness) elements and occasionally has an odor. In the
conditioning of surface water, sedimentation and filtration
is generally required to remove the color and odor. Chem-
ical treatment is generally not necessary except the addi-
tion of a coagulant to form a floc to aid in sedimentation
and filtration. Liquid chlorine is usually added for
sterilization. Of the 28 Michigan surface water condition-
ing plants listed in the ”Census of Municipal Water Purifi-
caticn Plants in the United States” by the American Water
Works Association, 22 plants use coagulation, filtration,
and chlorination only; the other six plants soften as

additional treatment.

Ground water is usually clear but may contain cal-
cium and magnesium which, combined with sulphates, chlor-
ides and carbonates, form scale and requires considerable
soap to neutralize before a lather is formed. Ground
water may be contaminated, requiring sterilization for
domestic use. In general terms, the conditioning of ground
water will require a chemical treatment to reduce the hard-

ness, and sterilization to make a safe drinking water.

Deep well water, from sandstone or similar formation,
is usually hard, clear and odorless. Treatment of this
type of water with lime or lime and soda ash, or zeolite

is usually sufficient to remove the excess hardness.

Water having a hardness of less than 137 p.p.m.
(S grains per gallon) is considered soft. When hard water
is conditioned the hardness is usually reduced to 85 p.p.m.
(5 grains per gallon). Water, to be acceptable for drink—
ing, domestic and industrial use must also be clear, pal-

atable and free from odor.

Hardness in water can be classified as either temp-
orary or permanent. Temporary hardness is that which is
removed by boiling. Calcium Carbonate is only slightly
soluble in water, 15 p.p.m. When carbon dioxide is pres-
ent in the water, the solubility of calcium carbonate in-

creases and it is converted into bicarbonate. In boiling

the carbon dioxide is driven off and the resultant pre-
cipitate is calcium carbonate. Permanent hardness is

unaffected by boiling and consists of the remaining car-
bonate and sulphate salts. The solubility of magnesium
carbonate is 100 p.p.m. Boiling may cause hydrolysis of
some carbonates and sulphates to produce less soluble

compounds (basic salts and hydroxides). These will also

be included in the temporary hardness.

Dr. Clark of England in 1sN1 discovered that by the
addition of lime the temporary hardness could be consid-
erably reduced. The addition of lime to hard water, either
as calcium oxide or calcium hydroxide, removes the carbon
dioxide forming calcium carbonate. When the carbon diox-
ide is removed the remaining carbonates precipitates ex-
cept the small amount which is soluble. Lime also produc-
es magnesium hydroxide which is very insoluble and precipi-
.tates along with the calcium carbonate. The permanent
hardness can be removed by the use of soda ash (sodium
carbonate). This chemical changes the calcium sulphate

to calcium carbonate which is removed as a precipitate.

Water can also be softened by passing it thru a
filter bed of zeolite mineral. Zeolite is a compound of
almninum, silica and sodium. It occurs both in the natur-

al state or it can by made synthetically. Zeolite has the

-3...

property of exchanging its sodium base for calcium and
magnesium, consequently it removes both the temporary and
the permanent hardness. The process is reversable, after
the zeolite bed has absorbed its capacity of calcium and
magnesium it can be regenerated into its original condition
by passing a solution of sodium chloride thru it. The so-
dium replacing the calcium and magnesium in the spent bed.
The water obtained by this method is of nearly zero hard-
ness. Stations using this method by-pass part of the un-
treated water so the resultant water will contain about

85 p.p.m. hardness.

In some cases it may be more economical to remove
the temporary hardness with lime and then treat the perma-
nent hardness down to 85 p.p.m. withzeolite. Permanent
hardness can be removed by the zeolite for about one half
the cost of removing the same with.soda ash. In a station
using this method, the water is treated with lime and a
coagulant, clarified, recarbonated and part of the water
filtered thru zeolite filters and the rest thru sand fil-
ters. The amount of water filtered thru each kind of
filter would be dependant upon the resultant hardness

finch would be economically desirable.

Hardness in water causes a loss of one-fifth of a

pmum.of soap per 1,000 gallons for each p.p.m. of hard-

- n,‘

ness. Assuming a water having 400 p.p.m. of hardness,
serving a municipality having a population of 80,000, and
that the average use of water for washing and laundring
.is one gallon per day per person and soap at ten cents
per pound, the economic loss to the municipality would be
350% per day or 318%,000 per year. This amounts to $2.30
per person per year. These figures are based on the hard
water and no allowance is made for households with domes—

tic softeners.

One pound of lime will soften as much water as twenty
pounds of soap. Assuming the cost of lime as $12.00 per
ton or 6 cents per pound and soap at ten cents per pound,
the cost of softening with lime is only three-tenths of
one percent that of soap softening. Of the total water
pumped into the distribution, one percent is used as a

cleansing agent.

The following data is the result of a retail soap
survey made in Chicago Heights, Bloomington and Urbana,
Illinois and Superior, Wisconsin by the Illinois Water

Survey engineers.

Superior, Iia.
Bloc-ingten, 111.
Urban, Ill.

(hieago Heights, Ill.

Lansing, lieh. (letinated)

luperior,lia.
Bloomington, Ill.
Urbena, Ill.

Chicago Heights, Ill.

Lena ing, Mich. (Estimated)

Superior, lie.
Bloomington, 1’11.
Urbena, Ill.

dingo Heights, in.

Lansing, Iieh. (Estimated)

Population
36,113
30.930
33,h08
22 ,321

50,000

Annual

Per Capita

Coat of
Soap

t 3.60
“02°
5.58

7-27

6.20

Total

Hardness

of Water
Supply
pepo‘e

ll5
70
298
555

MO

Annual
Per Capita
Soap laete
lb.
Base
3.3
10. It

17.x

12.5

muglap
Per ita
Coap Con-
sumption,lb.

27.5
30.8
37-9
Mag

“0

Annual

Per Capita

Soap laate
Base

0 0.60
1.98

3.67
2.60

Average Cost of
Soap per lb.

8 .131
.136

Water pumped to the mains is used for the following

purposes:
Residential consumption 30 percent
Commercial " 30 percent
Industrial " l3 ”
Municipal " 6 "

Street sprinkling
Sewer flushing
Fire extinguishing

Paving, etc.

Loss in Distribution, due to

Leakage 21 "
Underregistration, etc.

Total pumpage 100 percent

Before an intelligent determination can be made on

the type of conditioning process best suitable for any

given water, the following factors must be thoroughly in-

vestigated:
a. Condition of water bacterially.
b. The chemical and physical properties of the water.
c. The amount of temporary hardness.
d. The amount of permanent hardness.
e. Amount of dissolved gases.
f. Location of conditioning plant in regard to dis—

tribution system and disposition of sludge if a

_._ 7 _

The
treatment

8..

lime and soda ash treatment is indicated.
Turbidity and nature of suspended solids.

Cost of chemicals, lime, soda ash, and salt.

advantages of the lime soda ash method of treat-

The resultant water will be safe bacterially
without further treatment.

This process is more suitable for turbid water.
The water contains a lower amount of total sol-
ids than the raw water.

Treatment can be controlled so as to avoid cor-
rosion of distribution system.

The water required for filter backwash is only

2 percent.

disadvantages of the lime soda ash method of
are:

Disposal of sludge may be a problem. This may
be the determining factor in the choice of
treatment. _

The initial cost is more than for a zeolite
plant.

Operating costs may be higher than for a zeolite
plant.

Occupies_more space than a zeolite plant.

The
are:

I033 are 8

b.

0.

d.

advantages of the zeolite method of treatment

The resultant water will be soft regardless of
changes in composition.

to sludge to dispose of.

Lower initial cost of plant.

Lower operating cost.

lo excess chemicals required.

Does not require the use of skilled labor.
Hardness may be reduced as low as desired.

disadvantages of the seclite method of treat-

The resultant water contains a larger amount of
total solids than the ram sneer.

Possibility of corrosion due to lack of chemical
balance to calcium carbonate.

i! ran eater is not safe bacterially, the soft
eater must be sterilized.

The quantity of wash or rinse water may be 10
percent of the total Inter treated.

Turbid tater requires filtration before treat-

ment thru seolite.

There are several plans for controlling the hard-

ness of seelite treited eater.

a. The zero-hardness water cgn be mixed with the
proper proportion of hard water for any resul-
tant hardness desired. This method is not
satisfactory if the raw water contains consid-
erable iron.

b. The iron can be precipitated by the addition of
lime and allowing it to settle out.

o. The raw water to be mixed with the zero later
can be aerated and filtered before mixing.

The conditioned water should have the proper rela-
tion between the alkalinity and the pH. marts 1 and 2

shows the proper balance.

These curves ere known as the calcium carbonate
solubility curves. The values shown are for the solubility
of calcium carbonate in distilled water at 22° C. These
values are approximately correct for natural water which
is low in soluble salts. Iater high in soluble salts
should be checked by making an actual determination of the
calcim carbonate solubility. Inter treated to the lower
curve will not stain toilet fixtures but there will be an

occasional occurrence of ”red water“. later treated to

~10 -

"i

 

 

 

 

multiplexii- , . . _ s
an . ow. . ow. 8 a 9. M . e _, s m
_
_
.

 

 

 

'-
I
I
A
I

I
I
I
I
I
I I

.4
..-—4
_.
I
-r-->‘—‘
..
<

 

I“ .g . .L.. “- he:

I"

 

 

 

       
   

 

I

.I

;“
‘t-'--.I
I
“I

 

 

 

 

 

I
r

T

I

. -

‘ I

' ' - > v
W———-—~—hv~.o—.‘m—‘-

- v .
. I
. . . .
- .
-

wIIvIIIII .IIIOIIII I I-t ITIIII III

I

I

V
-Ii

I

' I

I
I
I
u I
I

.
ts..IO

. : . -‘ .
- s I - .
“...-.4”...- JL...“

 

 

 

I

     

- L
I

I .
I
I
I
I
l-
I
I
I

 

,4,
I

. . . , .. . .. . A .
.L‘.II‘|II-v‘~.lut.li ItItflllIlI-IIICIIII.IIIIIIVIIIIIYIIIIO‘I'IIIIFII‘IIiI-im
. a i _ .. L . ..
.y s . . . .. . . a
4 . u, ..

at... want—u use; our-.540 z. a w

o
O
O
I

. . . . . - .‘ .
~Q.-“.—q-$—-p.>_-_...
-. . s .

 

I
~I
inimgwam--- mun... .1 t

1
I

¥
I
I

.. I ‘ .‘ .

O
I
-e
I
I

_L
7

1.-
I
I
.._._I_- -.l -

I
t
I
I
I
I

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

I» p
... . . .. v . u .... .. . . e.
._ ........ .. . n . .. .
.- I: Tux-L.-- .--..-. ...... . .. .. .-
. .- fi..~ M Mr... ... ... . . . , a .
.,. . . . . e . , . . ... .. . . _
IIIIOI. I» iI-I+ IO'I‘III'L . III IIIII roll-It|ut.l
. . . . .
v.. .. o . . u
. . - . . . w
H § ' v . O. . — t.
fits-I o I“ i.|II. ..III. .A "..I ”I
. . e. o w ,
o. 8 As. .«.A . .
. . ...rr.I n. . I.I .F I.
. ... A 1..h_ v. ”I a
. .e . cl. I
. “.... ..w . H... . .
II. .._ v'leele.' .I'xvl- I e .1“
. _ . H . .
. _ . . .
._ . , .
I. _ 4 -- III-v III -L.l-III
. u.. . . . .. ..
I n. h a ..H . M . .
.e A Iwoenvif. evl o- . I. 4
. . .~ _ m
. n . ~
'r. [In

 

 

 

 

 

 

 

 

 

 

 

.1 -

 

t.z:<5diz»~-...--... .- mII- I..--

 

 

 

 

_ .
s _. I
IL . . . ..-
. _ .
.

 

 

. .
.‘IIIII II It. IIIIflI lI-lrIIII.1I‘IAPI I III v.4
, I, . . . . .. .
.. . . . . . .
_ . - .
I. I.- .II.i II . 0.3.0 .
i .. . .
fl . a . . -. . .
. .. .

m . .... .- , IL -..
- _ f. _ . H ._.H ..L
rII _I. . _- 1

fl
w
a
o
.

 

 

 

I
I
V
I
I
O
f‘v
I

l
. . .$
v .
l
e
-. . .-
*mVsF—‘->r

I.

I
I
I
I
I
...Ir -4 -14-...‘.;+_._2..g--.
-. :
I
i

 

-i
.. n

-- m©f.fl-.;;
...n .

I -I L- IIIIIIQ‘I. IILFI‘lIII wIIII IIIILIIIII- ‘..‘I

rang-.58 2.333% .0-

I

°+-

 

:.--.;..—4»-.

 

.
.

 

 

 

 

I~s e

' .

. .

. T.- --M<MH§doma-Q

 

 

 

 

O
L
...
‘<»-—o ,-......_-.
. ....

 

 

 

 

  

 

 

: ts... . . v "
wi;-~---—.—_odko——- +;--
. I ..u . .L
‘ ‘. . ‘
.-. . .._-. ,
I
I
I
wT
I
I
I

 

 

. .... .
. . v. -.r - ...w q.-
B-E-uvmaeb _ -M.--_- .

 

 

 

 

 

 

 

e .
' o
- I
.|- .I
a .. -.. ..
. I
l
I
I
I
I
I

.
- Wm...“ .
‘ . . ,

 

 

 

 

 

 

 

 

--o--—p-v- .

ALIQNMLNT LHART FOR
H, AIKAI INITY AIIC \Jx.)

'DF I"
PH

 

fl}
—4
I
Q -——4
I
-9
,
ALKALLHTY
-0 ‘
Z’“ " Ix. "
_. —. soc
_. 2‘“ ‘4
—-" 50
* r 00
~ "7(- IC‘I‘
- _ 5:
ii'}- — ‘30
x- 4“
+— -- .'_-,'I~
U I»-
..“v— - an
I? [3— 0 Li. ,L
u“
_‘ I-- «
I :1 I: "
“ S;
v. P ~- ‘1
I f 4
~ ‘3‘ r "3
I I__. '
"" 2
I
_ I— I
5.5)—
—4

“ HAJED 3:

T3 PfI=-LC)J-*

TH,—

'HLUWAJB FORMUIAE I

ALKAIINITY >g £5433 x IO]
ALKAI I. J'TK \AS C6.CO3)8- cod. ARE IN PPM.

C. JAL LIATIOF‘J
”I I \II’IATCR

g

(3
"""-O
m

7 I

V 9! r 7 (111] Y'HIIHII'W‘IIIII'IWI I I

1"?
I

R MIL L !f‘I

.-
.—
I Y I
I
I

LAPTQ p

VVFHLN

 

CHART 44

’1)

 

TIIII

 

 

 

 

.I \OI. I\.III I'IJIIIIIIIIII

   

 

 

 

 
    

 

 

 

 

 

 

 

 

 

   

 

 

 

 

 

 

 

 

 

 

 

 

      
  

 

 

 

 

 

 

 

 

 

 

 

. . . .

_ a M H m H . .I ..I I. IIJ.
. w m . . . . . .
_ . u . . . . w H
I o . . . v a v I I . y I w I III I. I IIIoI ~.I o '5
. ¢ w _ M u ..
A g . . . m
. , . . , .
. . . . a . .
I I IIoI III» II ArI III I.. I l IL I I I vII I IIIII I I II fin I IIIw IIIII III . II. I I-I IIIIIL III' III. fiIIC NII+IIOII I I..
. _ . . . . , . _ _R
. _ v . I.
. _ fl . . . * A
§ . . . . . o I . * I. III I- . I r I . «I .1
. v . . . . . ,-
. . w . . w . m * .H
. . _ . . . o .-
. . _ u . .. . n
I I III-WI I IJrIII I I M IIIIII . A ”I II 4 I I PIP
_ _ . . a 3 i _ -. , .
. . . . . . a . m _ fi . _r f“. fl .
u . . . . . . . * . .
. . I . . _ L w .- ~. ~ . . w
‘ IA 0 a 4 A I . I a I . v I; .I4I .II‘III.0 I II .l.44II and I I ha II I I II JIIYI . .4
M _ . . _ _ n u + . , . H
. . . - .
_ M n. . a . .~ .~ . . _ v
. . . . ._ , . .... ..
I .I u I II I .I I I. II I ;I III . rI .. II I I. .III :II L II. II . I I IkIv IIIII .I I v.II ..II—I II II: VI III II4 IIIIIIII.I;_7II III III “IIIIII‘TI‘IIIII.i III III-«III VII I IIII+ I. II IIIII .
- . _ . .. . - . - . - . ..
w _ ,_ . . . H _ . . .. . . . . _ _ . ‘ ~
. . . . “ - . . . _ . . . .
. . . _ . — .. I o .
I I I . I L 9 I . . I I . . ID. no I II.I I I . I .I»... I. IIII ..... .I. IIIIII I I II I I ».I .
_ . . fl _ . . _ . . - . M . _ .. . .
. . ¢ . . < . .. - . . 1 . I ‘
_ . . a _ . o . . . o. 4 I ...
a I. . . . . I .- I w .I _ .. M _ .
. . p I I J. I I
_ . < .- _ . . . H . . .
w\ . . M . . . . I . . ,I
. .- . . . .. o . . . . . - .
.. I * - 4. I. I. ..I .c I I. A . .I .o . I A_ I I r I A I I WY I. .n . . I.¢.4II.I. I 1..le
, . . - ‘ . . .. I . l ._
a . . u. o . _ v . .. h to. . I
.. - . ... . . . . _ p . .
_ . . . .. o .. . I t
.I I LIIII 1‘.qu I: I I I I - tIIII “ III I o FIG... I III ‘YI .t It “I u I“ .IVIIILTIII If .II. I .P. I I I I“. ’I IILf.I . Li I ‘ . DI .vItIIOL‘IIII IO-IQIII.IIIA ‘ _ I H “II 7»
. . _ . $ . . . 1* . .. 4.. I“ ..1 .
. . . . . a . ~ * . . n“ .l - .. . I a .I . II
. _ . . .. . . . 4 . . . a I . .a I . I . ..
. . . — . . . r . ._ I. I s .._..
.- . - t. w t. - W. ..- . . . . . m - .- T ..-..I -.....-..L: r11:
fl . . . : . ...; . .. .r v.
. c m . ‘ . . . . . iv. g v Q .I I r.»
w . p b r . ~ _ I» .. b I ,. I . ~ . I
. . _ . . . 4 . . b .. . . L. .
I I - _ I I . I I _ - I 4 J-
. . . . . a . .. _. H .
. . . _ . . W t
. . . . w . I . ... I . _ I. . .- .. .7
. .. . H . .h......
. fi . v a
IIIIIII II I o IIIIIIIIIIIVI It I b I IIIIIVI IIIIIIA IIIIIPII IIIII . III-II 0 I III I
. . _ h _ H . ._ . n M.
. _ u . — . - . . .
v . . ._ _ v .
. . I I .4 II I I I u I a IIIIII a v- * III I “I II;
M H . . .. . I-
. . H . . _ .
_
III I I II .I I w I. »
. . — H
_ . . m . .. . fl
. _ . . . . _ .. .
I . o I‘ u I. OI t I..g .-a4I
. . _ ..
. _ H w . a .
5 O ‘ fl -
. . . o . . . ..
I I I OH II 0!. I4 IOIoIIIIIIwII fiIIIIIII¢IIII.I IIIOWII IibIIIA 4|I .I
_ ._ h m g . m . . W
. . .. .
q . . m p. 4 p _ a. A I
. 0 Ir I a . H . 1 ..H. o“ .l I“ _ I. s. .d. .I c It 4 “I .
. _ « . . u . .- ... .. u
_ r. w u h m . _
. L I
IIIII II A I {M -
. _ . u I f. C . . m
. k -
_ . . . -
. . . . . fl _
. .c H o ‘ I . . s I. ml . ¢ ...... o
_ ~ _ . n . a
_ . * _ . .H . . n
- . .
. . _ . . . .. . , _ .
~ I . IIIII I I. II I .. II I v I I--. II I 0 II. 0 I III“! III. III . .I.I|..I III IIIIOIII. - sII «ID-u vII-I...Ol"u|.’..n‘l O ‘I III
_ . a . . . . .. .‘ .
_ . . ..
. _ _ . a k . .
. .. w . . . .
p 0* l c * . I . .II I ll ‘0 I
. _ . _ . _ H . _
. n . . . : . .
. u . w . . . . . . Mml .. ._
I I I by V II .
I I A 4 A a . . _ . __ . H . a . V
. . . . . N a . . . u a .
. _ W 2. . . . - ..-...“ .- - * «Inu- - - ..- - -- L .
. . . . . . . . . . . h w a

  

 

 

I

I

- I

I

I

, I

~eI

mi
I

K‘s-II
'*--I .
21 '

WWI}:~|
4i ,

..awg-mm§-s mm-mwm- E... u- I... . I".

II [I .IIIII I .

the upper curve or higher will for. e protective coating
of calciu cerhcnnte. The precipitnte will for: only on
eolid eurflcee if the treetnent ie on the upper curve
but it it ie much higher, calcium cerbonete may be pre-
cipitsted throughout the eoluticn. After the formation
of e protective cceting the treatment ehculd he to the
«turetion curve or elightly above. By eeturetion or
eclubility equilibriu ie meant the point at which the

water will neither for. nor dieeolve celoim curbonete.

if the wester conteine cerhon dioxide thie rector
wuet an be ocneidered. The pH nuet then he edJueted
by the eddition of eode eeh eo the» reletion conform to
the following: . '

3003 Free 002 f pa
4 15 p.p.m. O p.p.m. >8.)
100 ‘ <1.75 J. 8.1
200 < 9.25 1.8
300 436.00 77.)
>300 >llo.oo 77.1

The reenltent water will then be non-ccrroeive.

mm It ie eleo ueeful for the detenineticn or
fectore which heve e heering on the condition of the
final Met. Thie chert ehowe the relntionhetween c.1-
minty, oer-hon dioxide ad hydrogen ion (pH) concen-

‘11 '-

traticn. If any two are known the third can be determin-

ed by alignment.

To prevent after precipitation when using lime—soda
ash treatment, the clarified water before being filtered
should be carbonated. This is accomplished by the use of
carbon dioxide. 'Coks or oil is burned and the flue gases
passed thru a scrubber and then a compressor. The oom-
pressed gas is then released under water at a depth of ten
feet. Ninety percent of the carbon dioxide in the gas is
absorbed by the water. The flue gas will contain approx-
imately fifteen percent carbon dioxide, the remainder be-
ing principally inert nitrogen. To eliminate most of the
incrustation of the sand in the filter beds the water
should be carbonated to a pH of s.u to $.6. This will
also prevent deposits in the distribution system. Calcium
carbonate is the least soluble at a pH of 9.4. If this
value is used for recarbonation colloidal precipitates
are formed and will crystallize and deposit and cause in-
cuustation in the filter beds. Recarbonation also re—
stores to water a sparkle and makes the water more palat-
able, removing the flat taste caused by the addition of
Jdme. The life of the filter beds are also materially
inc>I'eased by recarbonation. As a general rule the life
without recarbcnation may be 5 to 6 years and with re-

Carbonation this may be extended to 12 to 15 years.

_ 12 _

Ir. Charles P. Hoover lists the design requirements

of a line soda softening plant as follows:

1. To require a ainism aacunt of labor in their

. operation;

2. To be practically dust proof;

3. To provide for an accurate and uniform applica-
tion of the softening chemicals, thus insuring
a ainimn of variation in the hardness of the
softened tater;

h. To make possible the reduction of hardness to
practically the theoretical.sclubility lisit;

5. To produce water in chemical balances and there-
by" eliainate the building up of incrustations or
deposits in the distribution system, or red!
water trouble in hot water heating systems;

6. To be capable of softening auddy ester as suc-
cessfully as clear ester and should eliainate
entirely fro. the softened water all turbidity,
practically all color, free carbonic acid, iron,
sangsness, hydrogen sulphide, harsful bacteria,

ebiecticnable tastes and odors.

“KW
There are tsc distinct sethcds of airing the cheni-
Oals with the water to be conditioned. One nethcd 'is by

the use of baffles and the other is sechanical agitation.

-13-

Ip.

There us many different arrangements of baffles, the ones
commonly used are the over and under type and the around

the end type. Ieohanical agitation can be accomplished

by means of paddles mounted on a vertical shaft. One type
of mixer has horisontal shafts, normal to the direction ‘of
flow. The paddles are also normal to the flow. Another

type has the shafts parallel with the flow and the paddles
also parallel. This type tends to give the water a spiral
flow. heat types start with the mixing at a high rate and
' as the water progresses in the tank the rate of mixing de-

OIOHOI e

Oars must be used in the design of mixing equipment
so that the energy required will not exceed a head less
equivalent to one foot. Losses above this figure are pro-
bably not Justified.

After the chemicals are added to the water, the re-
sulting particles due to the precipitation may be from 500
t0 5,000 per cubic centimeter of water. The function of
finishing the mixing with a slow motion is to coalesce
these particles so there will be 5 to 10 larger particles
Der cubic centimeters. This bringing of the particles to—
Eether so they will settle out. more readily is called

'rlooculatiod' and is the primary function of the mixing
fink. The time necessary for flocculation will vary with

-1h-

different waters but as a general rule, 30 minutes will

be required.

The accepted design velocity of water thru the mix-
ing tank is from 0.5 to 1.5 feet per second. The velocity
must not be too low or sedimentation will take place in
the mixing tank. Velocities of 0.3 feet per second will
permit sedimentation. The proper velocity will depend
principally upon the type of floc produced. If the floc
is light or weak, a low velocity may be used but if the
floc is heavy or strong the velocity must be high to pre-
"m sedimentation in the mixing tank. The mixing tank
should produce as strong a floc as podsible. This will
result in better clarifying efficiency.

WM
lmhoff states that sedimentation in smoothly flowa
ing water, provided a certain velocity is not exceeded,
goes on Just as in still water. This limiting velocity
has not been determined, but lmhoff states that it is
surely at least 10 feet per minute. Very seldom will
velocity affect sedimentation.

lhether volume or surface area is the controlling
factor in the design of clarifying basins has been a.conp

troversial subject. Encode abductions from his experi-

- 15..

mants was that sedimentation depends only on surface area
and not on depth. it is customary to rate clarifying hep
sins in the retention time, which will consider only the
volume and neglects the area. Imhoff's conclusions were
that for granular sediments, area was the true criterion
and.for floocular sediments, volume or time was the true
criterion. Both classes of sediments may occur in water
conditioning and the type of water and treating will imp
dicate which factor should be given the greater consider—
ation.in the design of the clarifying basins.

lerrill lists the following items which must be de-
termined in the design of clarifying basins:
l. lumber of basins
2. Length
3. lidth
#. Effective depth
5. Velocity of flow
6., Detention time
7. Sludge storage volume
8. lethod of sludge removal
9. Inlet arrangements
10. intermediate arrangements
11. Outlet arrangements

12. Basins open or covered.

-16..

The length of the basin should be at least three
times its width. This is necessary to obtain good volur
metric efficiency. lo limiting rates of the depth and
width exists; this factor depending upon economy of comp

struction.

if no sludge removal equipment is installed, then
sufficient volume must be provided for the accumulation
of sludge for a 3 to 6 month period. In most cases it

is more economical to install continuous sludge removal

equipment.

One of the most difficult problems to solve is that
of the proper arrangement of the inlet to the clarifier
basins. The velocity of water in the conduit from the
mixing tank to the clarifier basin must be such as to
properly transport the floc. This velocity will be from
50 to 100 times more than that in the clarifying basin.
The kinetic energy of the water in the transmission con-
duit will be d,000 times as much as the kinetic energy
of the water in the basin. Due to this relatively great-
or amount of kinetic energy the water to the clarifier
basins must be started thru uniformly across the basin.
There is a considerable tendency to create eddies and
disturbances which may viciate the sedimentation action.
Thiewhigh entering velocity may be properly reduced by

- 17..

the installation of a perforated baffle. Another method
is to use vertical slots. To aid the water in starting
in.the proper direction short training walls may also be
placed in the inlet, the length of which should be approx.
imately 101» of the length of the basin.

For the outlet, a submerged wier is sufficient. The
loss of haul over the wier should not exceed one inch.
The wier should extend across the entire end of the clari-
fier tank. If this wier results in losses over one inch,
auxiliary wiers may be installed to reduce the loss of

head.

The clarifier basins should be entirely free from
all columns. If columns are necessary they should be

either stream lined or round.

The following data is from the water purifying

plant at 8t.l.ouis, lo.:
Detention Through Through

Velocity time . Gates Blots
ft.per min. hours ft.per min. ft.per min

Presedimsntat ion 0 . 81$ 3 50 9
Coagulation basins 1.25 2 s3 16
ledimentation basins 0A5 12 1&1 8

-18...

filtration is the last step in the conditioning of
any water. The function of filtration is to remove my
remaining suspended matter. The filtering material is
usually a bed of silica sand supported by a well graded
bed of gravel. There are a few installations using crush-

ed anthracite coal .

filters can be classed as either rapid or slow. The
present tendency is entirely toward the use of rapid fil-
ters. Blow filters are efficient for the removal of bacteria.
Since the use of chlorine for sterilisation it is more
economical to use the rapid filter and chlorinate if nec-
essary. This fact is more concerned with the filtration

of turbid surface water. later conditioned with lime needs

no sterilisation.

The filter should be designed to obtain thslongest
possible run between backwashing. The same quantity of
water will be required for backwashing and if the filter
can be operated twice as long, the famount of wash water
will be halved. ‘ The cost of wash water is the major item
of expense in the operation of filters. The length of time
that a filter may operate before backsashing is determined
by the total resistance built up during the run. The econ-
omic limiting resistance is usually on the order of 12 feet.

-19-

The initial loss of head thru the filter is approximate-
1y 2 feet. .

Filters constructed with large sized sand grains will
have a. small head loss, the length of filter run will be
the maximum before building up excessive resistance but it
may be necessary to wash the bed more often due to passage

of f1 occulated materials .

The conventional depth of sand in a filter bed is 30
inches, The present tendency is to reduce this depth.
Several beds of 2h. inches are in operation giving excellent

rfaults. The depth of the supporting gravel bed varies

fr0m 12 to 18 inches.

Present practice indicates that high wash rates are
deglrable. 15 gallons per minute per square foot of fil—
tel. area seems to be the present predominating rate. This
is equivalent to a vertical rise of 2h inches per minute.
If the temperature of the wash water varies with the season,
the rate of backwashing should also be varied to obtain the
8sum results. Tests made at the Baldwin Filtration Plant,
Cleveland, Ohio showed that the optimum of filter operation
“as obtained when with the variation of wash water tempera-

tSure the backwash rate was varied as per the following

BChedule:

-20..

‘l'enperature of lnches Rise

Iash water °l' per minute
32 - #2 2k

#2 - 52 . 28

52‘. 62 32

62 - 72 36
72 (and 38

These tests closely checked the nasen fornula for
“0 determination of backwash rate which is, .

Rate - 30 4 1-5(1 4 0.060 x) (t 4 30) 180

where

Rate is in inches of rise per minute

dis effective sise of sand in u.

t. is temperature of wash water in °l'

x is percent of expansion expressed as a whole

nmber.

Filter send is usually rated by the tern effective
“to. 'lffective else of sand is that also which is coar-
'°1‘ than ten percent of the sand grains by weight. The
‘1ae of a sand grain is always taken as the disaster of a
'bhere of equal value. Unifornity coefficient is the
1‘ttio between the sine, such that 60 percent of the sand
1- finer than it and the effective use."

-21..

 

w
.- ‘-a.

 

 

 

.

cAo-e-

 

 

 

-e--e

«l

 

 

 

 

 

 

 

 

 

 

mmw...m2......=2 z. oz<m do "3.5230
7. ..b 5. 4. 3 2

              

       

1.

...¢

?4~‘-—l
1 -
I e O
s . e

 

,.._.--., .1--e—.- 5......l ea

-‘

r

la. ...—.9. ..— ' .

{we

4—'

e- -e
,

-O

..-

r

 

 

.i,

A.VJ ”f-

T
- 1

<—~.— ..--‘

+—-e—

.——.>4

    

._—‘

          

--«4 ».—.-+

      

 

|02030405060708090

PERCENT BY WEIGHT FINER

PHADT ‘

 

 

 

 

 

 

 

 

 

__l l ‘_ . --—. r. .— -_--‘-«__. _——- - 7.4— —_~—.—f
.. .—. —— W v
~ - . ... . ..l_T.'I.... _'
. . . . . . . . . . . . ..., _
. . . 7 . . . . . - . . e . - . . . _ . . ... .
' I . ' ‘_ ‘ ‘ o e e ' I .. h. -
_ ma _. ..- _ .7 --. . - -7+.ll----- - - _._.__._.._ ._- .-_....-_--.___.---_.- -..—...
.. _ . . . .-. .. .. .. . ..L.-..... .
_ . . . . . . . . . . . — .. .. ....
' e - . - e . . .-a.- .7. . .. . _ . _ . _ _
4 - - - - e ‘~ . c. - e I .. ‘ . g _ _ _
.—.—w_._ ._......__._.—-- —- --_._..,_- .H._._ -._.
.. _ . . . , I ... -
' ‘ v. o . . . . l . . . . _ ._.. . .i e .
‘ . e . . . . ' . _ ,
"“ ‘ ’ e~- . - . . . . .-. . -.
..._*—_.._..
Wh-..__._.. -..... .-..— -..“...
-. . . _ . _ ‘ __ _
‘-w-‘ - . . . . . . - A . v . . a - e . ‘ r ‘
. -.- e , ‘ -
. . , . . . '
—- .—___._—

 

 

 

  

 

 

- . . -¢ a . . . . . 1 . . . . . s
,
\
... . . . .. . , . . _ a . , . . . 4 . .— . —. .« e
. . , -
l
, . . . . _ _ . . .. . . . . . o
*. _- -..—w“,
. V " . ‘ ' I ' . ' ' . ' U u I ' 1 .- ‘ Q
. " .. .. ..-.-,......._ -... .n.. . .7.. . ... .. .-.e.
“e- .. -.. 4.5. ...—..._... e» .... . . . _,_.,. .. .7 .e
,
_ ' ’ . . . . a . . A . . . . e .- ' . . . - . . , .
-'—‘~—~ A A «..-—a L —— ._._...__-_.‘__...__.___.H-.._~__. ...- . -. ...l.-....._-_.__._....
.4_ _. ............ I .- . .. .. . .. .... .
e . . . . I s e o J
a . u .
. e . . -
. . . . .-
- . . . . . .
.... - .....- +4
§ . n I. , .
‘ . . I .
Q . e . .
e. e A I y -w 9 C - u
-‘4 . . ‘d—O--—+—.—c ~H-b-u-—' *0.- ——~ ‘——.
- ' O. o - . - . . .
3.: - - .. . . . . . . . . , .
' O
-- ' . —- . .. . . ,, . . .
N— . . ‘ .. . . . . .
.- . _ M ...... “Wm—-m -... -.e—__.-—._.._..-__.__-—_.-M#
'— ' - l v
'w I . ¢ . w < Q s - . r
be ' ' ~ .... .e . . . . . l _
~--. . Y ‘ +- w 47- . . . . . .
‘ ‘0‘. u a . ~ ,.
Fe .- M“ “F- -_—_.__—-. ...-_
~ V '
t—e . ‘ ‘ " ‘ e—o - b- I v .7 - - . . .-
.-.
4 ‘ e . e . V - . . - .- . . . .
. -__ J - ‘
,4 ‘ s . a... . - < »— a . .
Nb; .-. fi‘ ‘ ' h I .
r. . _ ‘ ...- ...... -_._ .§—..--. - __._
>__. - l .. , . . . . . . . y . . - . . . . . .
...._ -. . . . . . . . . . . . . . -.. .
-. e e s e - e -e o o A . - - - - . - l . s
. o
...-
v . e
e .
. . ¢ .
. . .
_. . .. I
.
. .
. . - .
. . .
I I
. . . . . . . . . a .
- 9 - - r . . . . - . . _
_4_
O I D ' I . . ‘ -.~ ' I l '
v . - . — . .
0 ~ . . . . . . _ . - . . . . . _ .
. . . . . . . . . l
Md—fi ‘.H*—_.—. A _.
.. . . . . . . . . .
. . . . . . . . . . . . - .
‘ . - , . . . . . . .
. e e - . . . n . . . -.
..__._
. . . . . . . u
e . 't . . , - . .. . n . - . . - . . .
. . e . . . . - . y . . s O . s I . — u
r t . .
. . . . . . . . . . . i . ... . _ . . .
..f-.. ._ .._.- M“.-- TY‘Y
Y . , . . . . . . ,. _ . .m .
. e a— . - Q e I - . e n . . a .
I
. . . . . , . - - . . . . . . . . . .
- » . . ~ . b . . . . . r L-._
_A__
A —_“‘-.q A v— V— ‘7
I ‘ -‘. D - - I O I d . ' C ‘ I ‘ Q C s A 1 l —' I "» l—I
~e e - e . I - - e a .7 . ~ A a . n e -a ’ 9 -o - . --..
' ' H 4......
.. . r e . . _ ,_ .. . al._.4 ...-a e ; I e .- ... -.. .

 
         

 

 

 

. . -.._- -— _-
A . .

---d- ...— ___.-_.._,.-_ —
- - - - e . .

 

 

 

 

 

.0005

 

 

 

 

 

 

._.__._.___._ ..-..- -~-~—---_.~

. o

. u . .

. . - A-

0—. ”-—.——.——~ ...-...-..

_ . e . . .
e a . o . .. . . ,
-. .— e . .. ._ . . . .
._~

- , . . . .-- .
. . . . . - . .
e . ~ - . . . _ .. . .
. u e e a .. -. . . .

 

 

 

v ‘ .
e . . .
- - > . -
. . . .
>—.—.—-<
. . .. . . 4
- - a - . . . .

. -fi‘--__. -._l

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

.0003

.0002

WEIGHT IN GRAMS

 

 

 

 

 
  

 

 

 

 

 

 

    

 

 

 

 

 

 

 

 

 

 

 

 

a i

. ...

. 'LJ‘IJLLIUIITN
no. N. «2 «2 v. "2 n!

1.‘

GRAINS IN MILLIMETERS

 

 

.0000!

 

 

 

I
I
1
a

a. II, III. ||.|I .Il' .JII"- III.DIIII»A..I .i. I I I v...- .II II! {It all!" ‘t..-.|\II..! .Il! Ii'lltl‘li |l.\ (1.!
— .

. . _. _ . ._ l . 4
. . M

 

forznamoztmi H. ...M ,, ...
6285334. .n :5 <29 . _. l . W . H

4
n.’ IIVIIIIII ‘II .TII . i. . ... .I . .p . rw IIIII «lg I. luv. IIIIIIYuliulalrvOIeIfO; Io...“
.

, e, . . . . l mnwruzr 2...,

 

3.

955819

 

 

I
o
I
I
i

 

 

 

 

<17
carer.

V
..—

9
I
9

 

 

...—...r”- -__-,_-

    

 

 

 

 

 

.II ‘It‘VI'QII.’ ..
_

 

 

 

 

s
--9 7r-

H ...-......— <0 7-..

 

 

 

 

 

 

 

Y
.
-

 

 

I

_ 9;...— e H+F¢¢W'
O P .

- ...- o-‘

r :-

 

 

rIII....I‘ t

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

.
at" 1.0"; ‘IIIIL «III...» I «e
. _ .
. .
.
¢ _
, . l .
_ .
. . .
_ _
» bl
ll |fl 1 4‘ -
.
. . T T.
_ .
_
r h
1|! III}?! I I e I
- fil .
.
l. .
~
I I -I IIIIII h w - \ It.

 

 

LO

 

I .
v ~ . V
SS - I ‘
..¢.-

.0

a
-
I
v

3..
. .
.23: 3

.D

--.._' 4

§

_
.
l
a;
an“.

—..

v
I

E.

..-;_T,

0

L

H

t

I
0" >4". e -—e

4
v
as

‘
...

q

1

 

Rho--

mmmkwijfli Z. 02<m “.0 uN_m

(‘4
(‘J

 

.Vesp
_

$4444.34.

9....

"Y

e.
*.pt

.04

f.
.o

e '--»L-O—e.

I»

I
\
o
n

V.
...
T.
or?»

‘ v

+¢9
p re

,4-
.~+«

eIe

1
e

he

-i

+17%

.

:3. Z.

.eeAeo nee-tee.

v

vi‘t

I
4

.....e...

9|. .Ieuo.
.

.1

.911.

A..-

we

.4
e

u-eoI

. lu.
.'r'9*.i“‘
$1.1‘06
.
I

toue‘.
.ede‘t.e

.s
‘L

 

 

 

--....c-o -'—-— “—-
I I

m

e.

ozfimuo- 5523

.
.
.P..
V
o

«L

n

lit ‘It‘ 1‘!!!" Ills- 16"“I II'I..‘. I"

 

... 0......—
l

 

 

 

 

 

 

 

 

 

.
.
I- IIII... I. IL
.
L-
_
_
a
. .
[Ir L
a
a
.

.
.
1.3+ 111.3-1}? - L

.

 

. . .

, , .. ..
.-—.—..r———.-—.—-——-A.‘.--.--e—c---
. .. . .

e . . .
I

 

 

 

 

      

i .
fl .
.1 ,. . I I l

p l . fl

. l _ . ... . _
vi-.- I auw . cl. ‘v "I I h:Itu.LII_P—Il .‘I. I $AV IclelI v I A II?

. _ . . ¢

1. ,. . .

o _ . .

Ir , .- g

fl - ‘

_.
. o .

v
.\9.
t ‘g. ._

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

I.
.e . . e-
,
‘ I
n u
. .0 . -
-- -4- - ..
- s
.
I
,
a— ‘ ..
»
.
....-L...—._—.—»-... -_._.

 

It IoIr’ijI’I‘ ”-1 ..D

IEKFEI

 

I
i
I
I

.

HARTIO

I
I
I

I
L

9
I

_ l
L.

 

 

 

 

* ram: m“

 

 

 

 

 

 

 

 

 

 

 

 

 

 

.J.

 

 

 

 

..- H magnifies; 3.5.0 H5.24m no. 55530 , _ --.m - .- - -

 

I???

 

 

..
. _
w _ l
_ . . F .
I e I I n vI.*I n I II I .V v 0 II .0 ‘I , I IvIII v 1
. . . _
. m . _
. ~ . l I .
. . . .
. . . .
III ...II II L L I... I1.
. 4 _
. . .
.
. . . ,
. . .
_ _ M
. I III’I III I . - I II I T 0 IOI
.
~ . . _
l u b
. V . .
l , . _
m . l . _ .
. . t r!
. 4 .

e—— ‘ 7—- o—c—wT .. w---—rv—v-an
I ' l
_ I , . a .
I

 

7; .I's+i.91 ..

 

 

 

 

 

20.5.30“on :33 bmpémooz.

.H

 

 

.
.

 

 

t I III IPYIIIIIIIII
a .
. II 0 '
IF .
l
_
‘
I‘ u . .-

.

 

 

 

   

.31., I -IIWJFI. I- - 17-..“? I: 11.-..-.
M Who «5000...... 0 2.5..
... H .

.II‘o..

 

.
I ' '
---- ..- o .— “---“-.. —.
I .
I
l

IIIII LIIII -.III III -
.

I
I
I
I
I
I

_. .

.

...

.

  

 

 

 

 

  

. ...eIIoII. L

o

L, I I
We?

, —

. . .

... ._- . .
. . , _

IIJv IIe-‘IIII I... It': 0 II
. . .
l .. . .
l. I l I I- ..
. .
_ .
. . . a _
.:
_ . . .

I
L

 

 

 

 

 

}_-.---

.....

 

 

 

..m. 004.0 0.... 02..

:45. .2 0<.

I ll I‘llltl '1'

... ...0 30..

.llII.I I

 

 

 

 

5.1..--
i
i

 

 

 

 

...”.-i .
um .

. .. . \
‘

...- . \
. ...
... .

III I IIIITI - - _
I..-

II .

...

III: I v.11-..
7., fl

 

he average else of filter and ueed ie.” an. The

renge of eiree 1e froa .32 to .6 an. in dieaeter. The

else and quality of filter land auet be deterained not
only froa ite efficiency of filtration but also the effi-

ciency of backwaehing. The filter bed auet prevent the

paeeing of any floc and eleo hold a large volume of floc

before building um a high reeietence. The eand auet aleo

be of euch else ae to properly looeen the eediaent and
floc during backwaehing and not waete out with the back-

'uh water.

W

later conditioned with line ie not etable due to

1" being euper-eaturated with normal carbonatee. If line

“outed water ie not etabliaed before filtration, the
llnd gran. grow in eiae due to the carbonate depoeit.

1Whittle ie aleo experienced in the cementing of eand graine

t° 1"31‘ hard lunpe in the filter. The chemical reactione

"11 continue and carbonate deposit will reeult in the

“'tribution eyetea, netere and houeehold plumbing. Un-
To

't‘blixed line treated water aleo hae a £1“ '60“-
“011 theee difficultiee, the water can be etablired by

th‘ ‘ddition of carbon dioxide 89‘- Th“ 8“ can b. p“.
“19.1 by burning either coke, oil or game in a eaall fur-

“°§ and puning the flue gae through a cooler, ecrubber

and dryer and then conpreeeing, after which the gae ie
diffueed thru the treated water for a period of about
20 ainutea. fhie proceee in known ae recarbonation.
the following table indicatee the yield of carbon diox-
ide gae froa varioue fuele:
1. One pound coke yielde three pounde of carbon
dioxide.
2. One thoueand cubic feet of natural gae yielde
ll5 pounde of carbon dioxide.
3. One thoueand cubic feet of artificial gae
yielde 80 pounde of carbon dioxide.
1|». One gallon. of keroeene or oil yielde 20 pounde

of carbon dioxide .

The water ie recarbonated eo that from 5 to lo p.p.a.
°1 Cuban dioxide reuaine in the water. The coet of re-
“rbonation in very little, mounting to only 25 oente
”1’ lillion gallone.

The actiOn of the carbon dioxide ie to convert the
“1‘31 carbonatee which are alightly eoluble into bicar—
b"‘lttee which are very eoluble. In thie fora they will

he“ torn troubleeone preoipitatee.

-23-

W

There are aany reasons and methods for the aeration

of water.

Hale presents a very concise tabulation of the

functions and aethods of aeration in Volume an of the

Journal of the American later lorks Association. His

list is as follows:
1 The functions of aeration.

1.

'fhe removal of or reduction of undesirable

gases.

a. Oarbonic acid gas

b. Hydrcgen sulphide

c. lxcess chlorine

d. Possibly other gases such as nitrogen or
marsh gas.

The addition of oxygen.

the removal of odors.

a. Of decomposition, musty, noldy or un-
pleasant. -

b. Due to microscopic organisms, aromatic,
grassy, fishy, oily. I

c. Due to action of chlorine on organic
substances, nedicinal, carbolic, iodcforn.

d. We to trade wastes.

Aeration as a part of other purification pro-

cesses, to

Aid coagulation

-21}-

b. Promote admixture of chemicals and water
c. Assist in washing the sand in filters
d. Help remove iron and manganese
e. Prevent red water
f. Freshen stagnant surface water
g. Break up colonies of fragile microscopic
organisms.
h. Assist in softening water
i. Assist in lime and iron sulphate treat—
ments.
J. Point of application in filtration pro-
cesses:
Applied to ran water
Applied after adding chemicals
Applied after filtration.
k. for esthetio effect.

ll The methods of aeration

1.

Simple exposure to air, as in aqueducts,
basins , and reservoirs.

Flowing over Isirs in thin sheets.

Cascades by steps, descending troughs, or
rifled: slopes.

Trickling devices, stone or cake beds, per-
forated trays.

Sprays or fountains.

-25..

.\w
.e.\

6. Blowing air through by pressure, through

perforated pipes, strainers or porous plates.

Drawing air through Aeromix.

Spraying water into air under pressure, Elgin

process.

Activated Carbon

The principle function of activated carbon is to re-

move dieagreeable tastes, colors and odors. Activated oar-

bon can be used in beds or put into the water in powdered

for‘sr. When used direct in the water the dosage should be

on the order of l to 3.0 p.p.m. The cost of treatment with

activated carbon '111 vary from 8.50 to $1.00 per million

gallons.

Activated carbon will remove almost any kind of
“3‘38 found in water, including fishy, earthy, vegetable,

musty, grassy, disagreeable, moldy and chlorine.

Activated carbon can be used by removing some of

the Band from existing filters and refilling with 2” inches

°f activated carbon. This need be done with only a necessary

number- of filters so when the water has a taste it may be

run thru the filters having a bed of activated carbon. This

method 13 used in Bay City. At Dundee, the water from the

c
193-1: well reservoir is pumped thru a bed of activated carbon

-26-

before going to the distribution system. A pressure type

of filter is utilized in this plant.

Activated carbon has also been successfully used

by applying it to the coagulant mixing chamber thru a chem-

ical dry feed machine. When applied in this manner the

quantity will be on the order of l to 3 p.p.m.

Application can also be made to the raw water and

the water then coagulated and filtered in the usual manner.

According to data compiled by the Committee on Con-
t1‘01 of Taste and Odors of the Merican Water Works Associ-
ation in 1933 on 219 plants, 50 percent applied the activated

carbor: in the coagulation process and 50 percent immediately

before filtration .

- 26-a -

 

 

 

.....- --—

HART I2 I

 

 

 

 

I :

 

A
-—-—..>~*--

 

-..
.....— 4-

 

 

 

      

 

 

 

O
. s o .

I
——_o—-.Ab~._.

I

I

I
2

I ,

r

I

 

 

   

 

I

DAILY- ,
3.0

 

 

.TYPIICAL..DAY . ,
seer. 24.1930 .
I
II!

I

  

I
“I
I
. , I .
. I .
- Lflm A..-__.__.o_~—.-

I-

I
I0. ..
-I

 

7.4 '
5-

 

I

 

. I AVERACE

 

. —..O

I

I

I

I

I

. ——-u

I

I

I

I

I

I

I

I

I

I

I _.
.¢ . . . . I. ' . . - . . . .
.a. -—w~- - -_L~—*-~ “...“. 6- WH~—--§— . —-~—-. -

I . I

I

I

I

~——-—~L—v¢o~-—m—.-

'4
?
M.

I
I
I

o I
. .
. . , . . .. .p
N. . . H .
I I I . ...I. IIIAI l..-. ..-. - -
. _ . .

awe-— -
2350.- .e I

2.700" -
42A?

’ 306.0

I
I

1' .. ..
I

 

 

.. - ANNUAL
-EWW%G&
29

 

_
......T... I.

   

 

 

 

I

I
_ a I...
I929

I
I

 

 

 

. ‘ _ UJU-
-’.:-;I93'
-1932
» \--,"._...;-.-.- -.-...

H ’7‘ fl”.

 

 

XL

 

 

 

 

I
I .
I“ I

 

 

I...I'I

 

 

 

.
,
.
.
I.
-.. . .
. q _ w , . , u .
.. H. . _ _ _ , . _ .o.
-.x I.I..%.III h... ._ . .. My

.- 59... mm ezej<e.-_ _ - : .
-III-ILIII-,.,.u,- .;g_::wm_-~-- .}.,-_Ii.

 

mZOI...._<O ZO_JI=_2

m02<mDOIk I 20_._.<I_DQOQ

 

mm

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

4 {I .II a I
dI ”Lv1wm-“h’N pug-YIulu .I. v..A.h 5.. . IJV n... LWI
. + _ . .. 44.4 ... ..4. ... .4 . .. .~09 .~ . .. v. o
. .. 4 . .
. :4 .. . .4 .. . ..I. .. ... : .T;
... .. ... ..H. ”O4 n .... t ... ~ 0 0h.l .on 0’4
.. .v .. . . ”m... .4.. o. a...k..o” ..44 *..o
j.0.w-. .. .... . . o .4 .4 .n - ... . . ..I . o IOII
v.. . or. a - 4 ....*u . .... . u -. .0 t 1.0”” O. a” 0.. no. - I, u... ..vJW T‘-
T. .. 4 . . . .. . a... .4 ... ro>I . . .. ... . . ”.04. 4.. .0“ I”-.. . .
.fi. _. . .. 4 ..o .... ..* ... o. . .. . .. . .... .I.... -. ok0~.. ... ..d
. . . . 4. . _. . I _ 4
WIHOLH. ”I 49 on ..— .. h 4 . . . . 4..”.fi ~ua‘ . A.&4Ja ”0 a FL. .
Yo...” ~‘.. _ . “L. 4. . .. . on. .A u .14 t bou‘ m..4 ....If.u 9.04 .5 U. .
._._ mu . . . .... .4 4 . . ..~. .. .. o . . .. . o N. ...Arhh....l..u .u 4. . .IQ
I . . . . __ . . 4. 4.... ._4. . . . .... 4..u_. . ‘9“. u» . *rf .. 14..
.M . .. .. . .4 . .. . 4.” “Yr. v“. . .I . ”o a. _4‘s ...
H . u... . . . ... . fi _ ... ...~ . . o . . ... o
_ u 4 _ . . a . . . . .04 on.. ..I .»L a . . ..9 4 t
.. . .. . .w 4. ..u . ... . "JIAIF... .Y. . . . . .I. .
. . o . ~05 ..’ u... 5 . .p‘ .704 ...” ...o. . .I‘ . 4.
, . . . ./ .. .. 44. 4.... . . .. ”For; ... ..4 w: a. . . .. . .
. .I . . .4 I . > . . 4 ...¢.. .fn.. .. . .. h .40...J. . .. o. . I .
4. . . I. .+ . .. 4L~f.oI .. .. . ... ... . .. . a... vytov .. . 0.... .
. ” . 4 . .... .._ ._ . .. .. . .4.. $7.. .... .. .Io .I.. . . .
. . . 4
4 _ .. . .. . .. . ..I. . ... 4:... 7 ... . ..
4. .4 . . 4 4 .. . . ..44. ......4? i .L I.I . I
4 .. _ 4. 4 . 4. . . . 4.
.4. . ._ ... 4 . .. a ...H 4 . 4 O.
...41 4; ..., 4. 4
4.4 .4... .... . 44.404. . .4 .4 .444 . 44.
”4. . _ _ oh '.I. o . 4 N . 4 ....IIJ ..1k . n . .m.. o o v w
. 4 . . . ¥ 4 . ... . . .... m.. r.wr4H—.W .L.... .wIIIL . 4._
4.. . _ 4 . 4 .I. . . ... o. I
. _ 4 .4. 4* ...“... .. ._ I. 444%.. .....I 4.. e...”
.” ~ 4 . . I .< .I. s. A
. _ _ . w b _ ... .I. . I.. 4 A..”. h... .~ . 0c .5 ¢ .
. 4_ 4 a H . 4 i 4 .4 . 44. 4 4 4 .. . . 4.. 4 ..
. h . ... G. . H“ ... .. .4 4 4.. I. r o 4
.4. 4.44444_ .4... 4. . 4 444 : 44
4. a. . . _ . _ . . 4 .. A . .. up A u . d
. . m. . i _ * .9. . I . .. . .OIu . . ..AI. .o_ I . Io. .
... . . . _ .4... .. .. 4. .. . .. . .. .. .47 . 4. :4. 44
.4 .... w .4 _ . 4 4 .... . .4 L. .-..I .4 4m. 4.. 4. I4”
. o. . r 4. t v .. . .. . o al.v In. I . .. .
.. fl. . ._ .4 4’ 4 _ a . .. . r A o ... 444A 4.. u . . L "4.
.. .. ¢ . . . u .- .. ‘no‘Taolfi -. a... _ 4 4
.4 4 H 4 . . . .4 4. . 4 .. 4. : .. . . .3
.. ... .. 4 . o . ... O Iv Q fi.. . .. .'.-
. h. .4 _ . . _.. o. 00.0 . ‘I .4..A.a ..... . . fl _
I 4... 4 ... . . . . ... .4 II r.. I. o. o . ... . .. v V. I .
..w .. . fl “ I _ .. . o. .p. .. co 1. ' J o .o “I” I V . . .J
4.... . .._ fl. 4.... .. . *. . I.
44“.... . u _ .4... . .4 . . . M 4;: . o .0. . “I
4.. .4 :4 4 54.4 4... 44
o . h . 4. w . .I . . .
. u o . 4 a ¢ 4 . . .
.... . I . . .... . .o I ~ . +. n ..+.. «.‘ .. . Y 4 . a. .. o .
..... I . Ia . ...... u . . H.. 4 4 A #5 . .«wwLL .. . . ._ .>7 4
4 . .4 .. u 4. A . a? o. 4 . g _ o . . . .. I J o o p
.0. . . . . I. >.. .4... .‘A ..¥¢ ...4. o. . .. . I . ..4... ...Luh.+4¢4 4 h ..A . .4 r . . .
(OH. . . .4 ¢. 4 ..... .vo. ...¢ . . v 4 Ann“. .,a... . FWUrw a. . r
. c u . _... o. . . ._ . . . . o .. o 0 . . .
..o .._ . . ... .v4 . . <4. . .4 _ o . a . o v«4. ... 0.45;. o. . I 7?. f.
. _ ......jf ... .4. . 4 I. 4 »p. .... ....4 44
.. o p”. 4 a. H 4 ...5 .o I AIIOI II.- 4..; .o‘ . 0.00.. « .vl o! o J.’ u
_ .. v... .o _ 4 0a . . . _ . . 4 4 _
... “.4 ... H. ”4 .. H1143”. ...... . .... . f .. g .13.; 4. :H_ o ..I 4... Irifi. .I..
.I. 4.. I I ”IOILL ... I 44* “L7. -. 4 “40‘ ... 0444.— JI'Infl .4“ 4n ...-n. I ~u.Dtnr I+T& «A by —
. .. ... .. v ..... o .I 4 ... ..r. .. . I .
. .. o. .04 n b ‘.>. +. o . ; “‘0‘, $1.. 4 . . c F.‘. I. TVA II‘L nfl
Iur. ....fi. 4P 1 VI. .4 . 49 .V; ”o fi*u.j4lu‘ ¢ 0 HI! A IO IL: 0.1 HIAWO roj+ be “ Ob‘* “AI. 0 “fa II I. A“
I. “4; ..J’. ._. _ : L+L.w‘4. 9-. L-..-I.I .1141; 4» I .fio TI“..44J.4F¢II.,4. 4
_ 4 4.44 44-41 I 4 “4; 4 4 ...I. ., 4:4. 4... 4:; 444:4. 4I L 44-.. SO—
. - .3... 49.44 ._ 4 4+4 .4
. 144:. 4. 4 3. . It... [44444r4331 41:}: . 4 ...4
r ...4 . 441 .... 144.4 :4 111431... 2.4 $ 4 41.4.;4... .11.. .-....
I.. .44 4,... _ -I 4.. . .I. LJIIJ -.q. 1 I 5 4. I... I4 I... ...;o .
I . . . 4. $. .
I‘ '0“. I Idl m td“? A.“ O vafinHJ . 4'“ ‘ . J I fly Ohs.q‘ *r r‘ ‘ YnL I_ 1 UL ‘ m . 44g Q
.0 4m.."4+jJL.. w.M.—§ *hkfk.oo.‘.c 1+... I...<.QI.1 .IIL .I:%L §~WO . # “N“. k 4k . $ 4. 1% A
. 1m 10 v . H.0 FL .. >4 l6..4 “I‘AHA 411 ..<~ .24 ‘ g . 4. A.
'4... ”pa: mars. “...—u H.44b H. ~ ‘how .96 4i. . 4 4km” t * x. 5‘ _.L~4.+4~. 9 .43.“ .44.“ -
4 . 4 .. 4w.44.flnmw..44 .W ...D I. 4.4.. 4 . .4 ......Kw I
‘0

I

   

The first factor to determine in the design of any

water treatment plant is the capacity. The capacity is
expressed in terms of gallons per day. Reservoirs or

(near wells are usually provided to take care of the max-
imum demands so the water conditioning may be done at a
more or less constant rate. From Charts 12 and 13, shows
ing pumpage data, the capacity of the proposed plant is
determined at 15 million gallons per day. Many factors
enter into this determination. Rate of growth of the pop—
udation and past pumpage are the initial controlling fac-

tors.' Judgment of future requirements is the final and

determining factor.

In the design of any continually growing utility
as a water works in a large municipality, provision should

always be made for future extensions and additions.

After the capacity of the plant is fixed, the char-
acter of the water to be treated must be determined and"
Studied. The water to be treated will be assumed to have
the following chemibal and physical properties:

-27..

' .
q?
HI

n:

D”

“non. nitrate or nm to BE connnrom

Source - Deep well supply from Sandstone.

”“0 - Ill 15. 1933

Temperature - 51°F.

dolor - none, Turbidity - none, Odor - none, Taste oncellent.

Total solids - “33 p.p.m.‘

'1 02 '- 3~5 '

Dissolved Ietsllio lone

Calcium Os“ 108.0 p.p.m. 5.39 as.
iron, ferric 16"” 1.0 " .05 '
Isgnesius lg” 32.1 " 2.“ I
seem- n‘ 18.9 I __._§_2_ I
Dun of letallic Kiln-equiv. 8.90 me.

Dissolved lon-Ietsllio Ions

Bicarbonate noo3‘ 3%.0 13.3)... 5.62 no.
M‘bonate 00;” none I .. I
fluoride 01" 64.9 ' 1.83 "
Hydroxide 03' none " .. I
Phosphate For" none I - I
litrats [03" none I .. I
Sulphate sou“ 69.6 I 4,5 I
Sum of lon-lletsllic Milli-equiv. 8.90
Dissolved oxygen 6.8 p.p.m.

l'rse Carbon Dioxide we 10.} '

pl! 7.6

-26..

he} I!
‘

vfli'v"

225:1

  

an.

lids.

 

I
In.
a
up.

‘a.

ll.-

..J

Carbonate, Alkalinity as Ca003 none p.p.m.

Bicarbonate, Alkalinity as CaCOB 281 "
Hydroxide, Alkalinity as Ca003 _p._n_e_ "
Tetal, Alkalinity as CaCOB 281 p.p.m.
Calcium Hardness as Ca003 270 p.p.m.
Magnesium Hardness as Ca003 130 "

Total Non-Carbonate Hardness as Ca003 #00 p.p.m.

After a study of the characteristics of this water
the necessary steps in the conditioning process should be
determined. This water being free of suspended matter
will require no presedimentation, no colors or odors be-
ing present, no consideration need be given activated car-
bon treatment; the dissolved gases are not excessive, (not
over 30 p.p.m.) no provision for aeration need be provided.
This water, which is from Lansing, Michigan, is typical
deep well water, is objectionable only in that it contains
excessive hardness. The problem then is to condition this
water so the total hardness will be 5 grains per gallon

instead of 23.4.

...29-

 

 

SUBSTANCESIN NATURAL WATERS

 

GASES
CO2 CARBON DIOXIDE
N2 NITROGEN \\
O2 OXYGEN \
CH4 METHANE
H23 HYDROGEN SULPHIDE\
SALTS, ETC.

 
 
  
      
   

ALKALINE

 
    

fill

 

CQCOa
CQSO4

HARDNESS «1:11.
» Ca(N03)2

N250.

NaCL
SALINE

F3203
IRON BEARING

Si 02

H2 504

P- I I3

FROM 'WATER WORKS MANUAL"

 

LL

CALCIUM CARBONATE
CHALK

MAGNESIUM CARBONATE
MAGNESIA

CALCIUM SULPHATE
GYPSUM, PLASTER OF PARIS

MAGNESIUM SULPHATE
EPSOM SALTS

CALCIUM CHLORIDE
MAGNESIUM CHLORIDE
MAGNESIUM NITRATE
CALCIUM NITRATE

SODIUM CARBONATE
SODA

SODIUM SULPHATE
GAUBER SALTS

SODIUM CHLORIDE
COMMON SALT

\ACID

# CORROSIVE

II

 

 

IRON OXIDE
. RUST

SILICATES
SILICA -SANO. ETC.

SULPHURIC ACID

 

 

CHART -I4

 

Chapter II
TH]: MIME! 01' WATER CONDITIOHIIG

In the laboratory, the elements in the water are
determined by ions. The reporting of the results of an
nalysis should be in this ionic fora instead of hype-
thetical or sc-cslled probable combinations. Tab 5
illustrates a recommended fora of reporting a water

analysis.

The mbstmcee which are in solution in water are
present predominantly as ions and not as compounds.
This statement holds for water containing dissolved
solids under 2,000 parts per million. Iater containing
over this amount of concentration is very rare. The ions

in the water are in a state of 98 percent dissociation.

By using the ionic form of reporting a water analy-
sis, the fundenental ionic reactions may be used. These
reactions are shown in Table I. In this table, the ex-
Dcnents 4 or - indicates that the element or radical is
in a state of ionisation; where no exponent is indicated,

the compound is either insoluble (precipitated) or is un-
dissociated.

Table 2 shows the reagents which are commonly used
in water conditioning, together with their common nuns
and commercial purity. All calculations made are based
on the {unduental reactions and the resulting chemical

-30-

required must be dividedby the purity to obtain the

quantity of commercial chemical necessary.

Table 3 shows the common reactions and the choice
of reagents. The choice of chemical is usually deter-
mined by operating conditioning and by the cost of the
chemical. in table 3 is included a key to Table II.

Table II shows the reagent requirements and the
products of reaction in p.p.m. per p.p.m. of ion in water,

The application of the data in Tables l to It to an
actual water analysis is made in the chapter under the
caption “Determination of Quantity of Conicals Required'.

Table 6 gives conversion factors per p.p.m. tc
uni-equivalents. Every element or radical has a defin-
ite combining capacity and when its weight in p.p.m. is
multiplied by its mini-equivalent the results are direct-
1! preportional. for example, to determine the amount of
000 required to remove the 002, llg and H003 in a given
tater, the p.p.m. of each ion is multiplied by the milli-
equivalent and the sum of these is multiplied by 28. The
result will be the quantity of pure reagent necessary. To
obtain the calcim hydroxide necessary the factor would be
37. Calculations for soda ash are similar, except 5} is
the multiplying factor. Inn-equivalents can also be

used to check the correctness of a water analysis; the an

-31-

of the mini-equivalent of the dissolved metallic ions
asst equal the am of the dissolved non-metallic ions.

Table 7 shows some miscellaneous factors which are

convenient for calculations which involve conversions.

-32..

ITEM

l

—q 0\ \n #7 KN TU

10
ll
12

13
14
15
l6

17
18
19
20
21
22

 

' ' :-, -._'~ II
-- _::-_\’\ R" ——- “a m ‘ __.

TABLE I
MOLECULAR.REACTIONS FOR WATER CONDITIONING***

DISSOLVED TREATING REACTION
SALT REAGENT PRODUCTS
REACTIONS WITH LIME, HYDRATED, Ca(OH)2
Ca++(HCOB)E + Ca*+(OH)§ :2 2(CaCO3) + 2(HZO)
Ng++(sco3)§ + 2(Ca++(OR)§ z: 2(Cacc3) I? Mg(os)§ +EKH20)
2(Na*(HCOB)" +— ca++(OH)§ s: CaCO3 i— Nag 003‘ I 2(H20)
Nag 003‘“ + ca**(OH)§ :3 Caco3 T- 2(Natcs‘)
Mg++804”‘ +— ca++(OH)§ :i Eg(OB7E‘ -+ Ca**SOA
ug++01§ I— Ca++(OH)§ :2 Mg(OH)2 I— Ca++C1§
002 ~+ Ca++(OH)§ :: CaCO; ~+ H20
REACTIONS WITH SODA ASH a Naacc3
Cal+804 + Na2+CO3-= :: CaCOB ‘t N32+804fifl
Ca++cI§ +- Na2+003“‘ ;: c3003 + 2(Na+CI*)
Mg++804 + Nagcc3 :2 Ng++cos“ -+ Na2+SO4
Ng++012 + Na2+co3‘“ ;: Ng++cO3 -I 2(Na+01‘)
Mg++CO3E- + Ca++(OH): ;: Mg (OH)2 —F CaCOB
REACTIONS WITH BARIUM CARBONATE — Eaco3 ~ BARIUM HYDROXIDE - Ba(OH)2
Cai+804-_ +- Ba++co3 r: Ca003 I. BaSO4
Ca++804“‘ + Sa++(OH)§ :: Ca++(OH): 4— 133304
Ca++01g + Ba++CO3 :: Caco3 ' I- sa++CIg
Ca++01§ + sa++(OH)§ :2 Ce++(OH)§ I— Ba++012
REACTIONS WITH zEcLITE x NaEZ‘
Ca++(HCO3)§ +— N322 :i 2(Na+HCO§) 4. CaZ*‘
Mg++(RCO3)§ +- Naaz :2 2(Na+HCO§) 4— Mgz**
Ca+*804“ +- NagZ :2 Nagsou‘" +- CaZ
Ng++soyf‘ + NaZZ :2 NaESOQc‘ I— Mgz
Ca++01§ + ngz :2 2(Na+01“) +—-Caz
Mgl+01§ +~ Naez 4:2 2(Na*Cl*) +- MgZ

GENERAL NOTES:

The reactions shown should be considered as probably occurring at temperature
below 2100 Fahro

Items shown without positive or negative charges are in molecular form, and.are
removed from the reaction by precipitation or gaseous evolution, for example, CaCO5 is

precipitated, C02 is evolved. Items shown wdth the charges remain in solution in ionic
form°

DETAILED NOTES:

Items 1 to 7;

Calcium sulphate, sodium sulphate, calcium chloride, sodium chloride, silica and
oxide Of iron and alumina do not react with lime.

Items 8 = 9.

Sodium sulphate, sodium chloride, silica and oxide of iron ani alumina do not
react with soda. The preliminary lime treatment removes the temporary, or bicarbonate
(calcium and magnesium bicarbonate) hardness, mid some of the permanent hardness (MgSO +
MgClg). The ensuing soda treatment removes the remaining permanent hardness (CsSOh an

CaClg originally present in the water and.the CaSO4 mid CaClg formed by the lime treatm
mento

Items 10 a ll.

Where the water originally has only permanent hardness, preliminary lime treatment
is unnecessary, and reactions 10 and ll take place°

Item 12.

On account of the solubility of magnesium carbonate, a sufficient amount of lime
should be added to the water to convert the soluble magnesium carbonate to the insoluble
magnesium hydroxide as reaction 12.

Items 13 to 16.

Barium compounds after lime treatment are chiefly used for the removal of excess—
ive sulphate° (Soda treatment does not remove sulphate; if calcium sulphate is present
soda removes the calcium but leaves the soluble sodium sulphate). The reactions of barium
treatment after lime treatment are l} to 16.

Items 17 to 2#.
Sodium salts, silica and oxide of iron and alumina do not react with zeolite.

‘ NagZ, CaZ, and MgZ are not the true chemical formulae of sodium, calcium and
magnesium zeolite° Because of their complicated nature the radicals are represented
arbitrarily by Z; The approximate formula of zeolite, which is a sodium aluminum silicate,
18, 2 8102.A1203,N&20.6H20.

 

 

ITEM
NSC

23
24

37
38
39

41
42
43

 

DISSOLVED
SALT

TREATING
REAGENT

REACTION
PRODUCTS

REGENERATION OF ZEOLITE ~ BACKWASHING WITH SALT e NaCI

CaZ
MgZ

+2(Na+cf)

+-2(Na+Cl‘)

g: N322
:3 Nagz

+ 03“”013

.8. Mg" -012

REACTIONS WITH TRISODIUM PHOSPHATE NaBPOq w IBHZO

3(CaII(HCO3}E)4.2(Na3IPOE-u)

3(NgI+(HCO3)§)..2(Na3tpofi’“)

3<Ca*+soA“‘)
3(MSIISOE“”)
3(Csttcig)
3<Mg++Cl§)

REACTIONS WITH DISODIUN PHOSPHATE m NagHPO1+ -

+

f

+

+

2(Nagpofi'")
2(Na3ROZ‘”)
2(Na3tPO;°‘)
2(Na3IPOZ‘I)

:n Ca3(P04)2

:3

ll

3(Ca**(HCO3)§)+ 2(Nagspol”) -+2(NaI(OH)")*;fi

3(Ng+*(HC03 §)+ 2(Nagspofi‘)

)
3(Ca++SOA‘“)
3(Mg++804"”)
3(Ca++Cl§)
3<Mg++cl§)

REACTIONS WITH MONOSODIUM PHOSPHATE - NaHgPOh

4.

+

+

+

3(Ca++(HCO3)E)+
3<Mg**(Hco3)§)+

3(Ca+*sofi“)
3(MSIISOE”)
3(Ca++ClZ)
3(Ms++01§)
Na§003“‘)

+

+

+

2(Nagspog“)
2(NsERROL‘)
2(Nagspofi”)
2(NaEHPOZ“)

aNgnng)
2( Na+H2POE)
2(Na+H2pO;)
2(Na+H2POfi)
2(Nangpoz)
2(Nafsgpol)

+ .—

+2(Na+(OH)”)
+-2(Na+(OH)=)
+2UMNOM“)
+ 2(Na+(OH)‘)
+~2(Na+(OH)=)

+ 4(Na+(OH)T)*

+—4(Na+(OH)E)
+ 1+(Na+(OH)==

)
+ 4(Na+(OR)‘)
+—4(Na+(os)‘)

)

+ u(Na*(OH)“

;fl

4 I

:3
:j
:3
:3
;j
:3
:j

M83(P04)2
Ca3(P04)2
Ltie.:3(POLI)a
Ca3CPOm)2
MS5(POA)2
12H20

Ca3(PO4)g
M83(P04)2
Ca3(P04)2
Mg3(P04)2
Ca3(POR)2
M83(P0u)2
s H20

Ca3(POA)2
Mg3(POa)2
CA3(po4)2
Mg3(P04)2
Ca3(P04)2
M83(P0h)2

Na3+P04“"“

+

6(Na+HOO3‘)
6(Na+HCO3‘)
3(Na§SOE")
3(Nagsog“)
6(NaICl=)
6(Na+Cl“)

6(NaIHCOE)

6(NaIHCO3“)-

3(Nagsog‘)
3(Na5SOfi“)
6(Néc1“)
6(Na*c1‘)
6(NaIHCO§S*
6(Na+HCO§)
3(Nagsog=)
3<Nagso;=)
6(Na+Cl:)
6(Ns+c1”)

002

+

+

+..

+.

.r.

l.

2(H20)
2(H20)
2(H20)
2(H20)
2(H20)
2(H20)

4(H20)
4(Hgo)
“(H20

A(Hgo

VVV

4(H20
4(H20)
H20

 

**Zeolites are exchange silicates, having the power of exdianging the bases
which they contain for other bases brought in contact with theme The sodium of
the zeolite is replaced by the calcium and.magnesium in the water. In the regenw
eration with salt solution (”backwashing"), sodium is reeintroduced and the cal=
cium and magnesium are removed as theéoluble chlorides,

Items 25 to 30.

Technical trisodium phosphate contains 12 molecules of water of crystalliza=
tion, but because the water does not enter into the reactions it is not included
in the equations.

Sodium bicarbonate, sodium carbonate, sodium sulphate, sodium chloride, silm

ice, and oxide of iron and alumina do not react with trisodium phosphate;

When sodium hydroxide, NaQH, is present in the boiler water in excess (which
is frequently the case) the use of disodium phosphate, NagHPOE.12H20 is preferableu
These reactions of disodium phosphate are reactions 31 to 36 incl. Monosodium
phosphate, Na H2P04.12H20, orphosphoric acid, H3904, may also be used, The rem
actions for monosodium phosphate aid phosphoric acid are given in reactions 3? to
4} inclo, and reactions 44 to 51 inclo

Items 31 to 36:

Technical disodium phosphate usually contains 12 moleciles of water of crys~
tallization, but because the water does not enter into the reactions it is not in~
cluded in the equations,

*Sodium hydroxide is usually present in boiler water.
‘*In the present of excess hydrate, bicarbonate is converted to carbonateo

Sodium bicarbonate, sodium carbonate, sodium sulphate, sodium chloride, sil=

ice and oxide of iron and alumina do not react with disodium phosphateo

Items 37 to 430

Technical monosodium phosphate usually contains one molecule of water of
crystallization, but because the water does not enter into the reaction it is not
included in the equations.

*Sodium hydroxide is usually present in boiler water.

*‘In the presence of excess hydrate, bicarbonate is converted to carbonate.

Sodium sulphate, a>dium diloride, silica and oxide of iron and.alumina do not
react with monosodium phosphateo

*Usually present in boiler water.

*‘In the presence of excess hydrate, bicarbonate is converted to carbonate. q,

 

LS.1 .1 .1 a

ITEM
NO.

ALI
45
46
47
48
49
50
51

52
53
54
55

***N.E.L.A. Publication 289mll4

DISSOLVED TREATING REACTION
SALT REAGENT PRODUCTS
REACTIONS WITH PROSPRORIC ACID a H3P04
3(Ca (HOO3)§)<+2(H3 P04’_")-+6(Na (OH)‘) :2 Ca3(POE)2
3(Mg (R003)§)+ 2(H3 ROI,”’“)+6(Na. (CRY) «r-emsfipoim
3(Ca 804-") +-2(H3 POE“ v)+-6(Na (OH)‘) :=.Ca3(POn)2
3(Mg 804“") 4—2(H3 P04¢“-)+’§(Na (OH)=) F: Mg3(POM)2
3(Ca 013) +2(R3 POa“‘“)+-6(Na (OH)“) ee-Ca3(POA)2
,3(Mg CIE +-2(H3 Pos“')+.6(Na (OH)3) :2 Mg3(P04)2
Na2 003‘“ +-R3 ROE““ + Na (OH)“ -:= Na3 POATTT
3(Na (OH)=) + HBPOA““ .;= Na} POAI"‘
REACTIONS WITH ALUNINUN SULPHATE = ALUM n A12(Soa)3*
3<Ca (H003)§)+ A12 (804)3‘ is: 3(Ca OZ‘)
3(Mg (HCOE)Z)+ A12 (504)§” s: 3(mg EOE“)
6(Na NCO?) + A12 (804)3u :2 3(NaESOZI)
3(Na2COg‘) + A12 (SOA)§”+3(H20) :2 3(Na2(SOfi)

+

+

+

6(Na H003)

+6(H20)

60:. meg) + sage)

3(NsZSOA““)-+6(HBO)

3<NagsOA””)—A§KHQO)

6(Na CI’)
6(Na Cl“)

+6(H20)
+ 6(H20)

—+H O

2

-+6(CCg)
+ 6(002)
+-6(002)
+ 3(002)

Sodium sulphate, sodium chloride, silica, and oxide of iron and alumina do
not react mith phosphoric acid.

Items 52 to 55

Calcium sulphate, magnesium sulphate, sodium sulphate, calcium chloride,
magnesium Chloride, sodium chloride, silica and oxide or iron and alumina do not
react with alum.

*Although not a water softener, alum is used in water treatment to aid coagw
ulation and sedimentation. Alum is also a "neutralizer" and changes the small
amount of calcium ad magnesium carbonates remaining after lime treatment to cal~
cium sulphate.

**The gelatinous aluminum hydroxide "floc" envelope the finer particles of
suspended matter in the water and gathers them into particles of largensize, thus
aiding sedimentation. Recent investigation indicates the composition of the alum
"floc" in alkaline waters not to be as simple as shown here. Its composition is
not definitely known and considered to be highly complex.

Sodium aluminate (Na A120“) is also used in conjunction sdth lime=soda treat:
ment. Like alum, it aids coagulation and sedimentation. There is also consider=
able uncertainty concerning the reactions involved. With calcium bicarbonate its
reaction may be considered as shown below with greater complexity in the aluminum
"floc" than is shown. With magnesium bicarbonate its reaction is even more ques=
tionable, some investigators have d>nsiderei that a magnesium aluminate is formed.

It appears to have no reaction with calcium sulphate.

Ca++ +>(HCOE)2= A+Na,A1 o + “H20 ;:
Calcium + bicarbonate -+so ium aluminate and water
A12(OH)6**+CaCO T-Nag CO3 4-2H20
aluminum +calc um +—sodium + carbonate +~water
T hydroxide +carbonate
' é?loo") (precipitated)
Precipit~
ated)
2NaOH + Al2(OH)6
p
aNa + 2(OR)=

sodium+—hydroxide

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

M. 5555-55 5o5ousEEOU-fl- 005 x 500..Eo5....\,_. 0.5m 5. 5-020 22 5.005.505 0 7.3-3:.EQU 020 55:50.
.5-..._.\0-5--_.5 53050 0 525M025 E50- £94003 (ON-fitted
5005:5055 . (5000 55050.55. 5705-0va C 0... 5.0 5.0.5.5555 505. A550... .5055 :0 0: )L5- .. -505 05. 50 55505... 551.53:
105/5 .5... 0-0x05 503500-55 0535.0,«1 5.00.55. 0+ Corr-C0025 +005-«0m-W
-__ 035.02 055;. 05-5-5 M30505, 0.4 5.0-0... ....w AC 3505 Es: ...-25059005 «00.55.05». ewe-awash;
.-.-:05..-£O _. .....,.:.LC5-... .C. -5 .... 3.5%: 0.7... 5.0.0. :3: -, ”Since 05.5.0.5 5505+ .05.,3a5rtud 0-2- “COL-00.53i4
0.555505455454255 $.20 ROW 00$. +154 #000 OsrnwfnfiomY-Z - 535-4 05,05m5sw {55:58:54
3553030 ...,mem «on 83 ...-0H5 0.03 ofndmsd 5.5 nitsmwesaou silo/5.5530. mas-ea
€50> 3.550», 0.1.40.0.anZ mm05 G 50540; 0+0w._5..w EETOfl-u
geese-.53.. 5.3a -..oa: .3: .075 Nona 335.8 :52 . N52.5355 £25505
afieééz ...-.05 anew --woa 5055 .02 Nowm 0..: 2.5.0552 8.45393 $25255?
10......3 NOS. -10 3,5. .075 0.3 :0 oz 010% 8.59.00 emcee): genom-
SQJZ Kano 50.0% Lao-5 mom md .02 Own: nOUaOZ 5...-v4 010m). 0+Oc055OU£o510W
#5555345 Mom @505 -IQ tame .Iofl m.m5m 0.10..51000& £2545 +0 «55535 ~33..me custom
60.5 who 8.8 -.8 09$ :3 :2 .0040. 3:25.553 3225505225
.5156 New 5%... -10 8.0-0 ....0 5.: .3800 35-5 53-546 30225;: 5205.6
00-0 NWQ 9009-10 \VNVE :Ov 5.0m. OdU 055-5 delwcb amule 53.50540
N :3 JO-\u .‘NW ...-NW ...-.3
~43WU‘RQ. n.0- jruz to: .9..=4FUZ Jog C‘s-{Lou 0“: £053.00 0E4: _4um£U£U..

 

 

 

 

 

  

 

..A C.C0.._..1COU 303d; 50% 18m) W.dU.:-.U£U £05500.- N 83d. _ _ ..

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

a}: 5..-m5 enema-n5 .... iom - -+Gml. 2.
.. .1 fireman: - --.-saw ...-.5»... >
. -.._, 5.5.... 0-5.. as... sags-52 - 55w . ta: .5
m m. 4.0.5 .85; . .5105: 0.550 . Mocm .. .35 5
he. 4-: .00 .. 519$ .- 0.5:. + 1.8 + if. m
a-~. 0&5 0&5 5&5 555.com - 55w + 19-5 5
M555 8053-.- .5553fi -o.5.m ..-..oom .- I..»d e-
09 .8m + .5553st $50 ...-6% fish: a
“5-0. 9-05 0-05 $-05 55589-5 - -IOm + ...-...... 0
H550 <5. 0..: + ~00 u 250 + EN 55
5-0 .....m. .6055 - 1.53 . .55 2
am am. 0-.... an 0.: - -550 + .55 5
ma 604m - Ion + :60 05
a... 0-5 ...8-0 - ....0 + n8 a
..-5-m.. -505; 50.55 i {.00 .- .00 .
.... .0 ...-0 0.0 ...-5.0 0.3 + :30 n -IQN . .00 55
- ... a... O-.. n. m, -.3: - -10 ,. .00 W
as 5.0.50.0 - Non; ...-tom 5
4-5. moo-U - -..-.00 t 140 s
am. 0..: + ...00 - -10 m3: 5O
4N .6055. + .5105}. no.1m +-...oon + ...-54 u
<5 ..oom + .555354N .35..- + ..oom + ...554N n5
“5-5 55.854 -- -55ono + a
m .V U-J‘ 0* OX: ”—40.5250? Dig-II C03049d cos .$>..._.0<O c.. co‘

 

‘
.. -
.0 -
.‘I I l l
L I

 

Iii

Scar—51:00 5.3.43 Lou» “75.584U $0 Ud~0£Unm163dFth

. 5

 

 

 

TABLE. 4 " Chemical Qequirzmchs and Droduc-Ts of Reaction in ppm per ppm of Ion in Wafer

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

A B C D E F G
Ba 60;, Baa-(0H),;5 H10 Ca. 0 Ca (OI‘I)2 NazCOa Na OH Na, PO4'I2H10
'Oh in w a1. ¢r Chemicalyproducl PrOdUc-T prodUCT Chemical producl Produc-T Produd ChamIcoi producl Droducl DroduolChemimi producl Producl Champ-Ii productL gradual DroduclL [henna-l I PI’OdUJ PrododChemIc-I} Product Produgll Pro-Jog?
5 pme93. {HSOWHG Sciatica pEmRm-i Insoluble Somme 50‘UHQpme89’. insoluble SOIL-He SOZUb/a pmeeg insoluHe Solubh 2 ppm Keg. InSojub/e bomb/e BOW/e ppmiQf/ct )2 Soluble Soluble 32?“ch lnsolot/ego}ot}e SJOHe
' Aluminium I098 A5320 2.4% $21: I755 A5??? 735.: an, i??? , 53:. II. it”; so @389? 53% 25sz 4 I. 9%;
2' A'Uminium 2:95 @1953). 2993 (25;; II 79 A??? Egg; 9?;
3 suntan. 2.59 hi .9532; .I.. first ...}.- ‘Ii? 8.9-5. .... 512$.“ 52:;
4 Cchiu m 482 Czbégf 315:; ‘ 2C4 C5205 Rf; 6.33 C???
5 Ca-rBanDioxidc 3.5a gfig-L35 ‘ 35:: OCA. {mos—5:: O54 Igg- 2.4! 9.207 IIOS 0.91 HI?)- 05ng
6 CN’l’O'TD'bm'd‘ 7.I7 Fifi—(353' 1.28 C2??? lee C2533 I52 {32. H2“;
7 CMBM‘BV 52c. gé’ég (3)97 Osv- 323% Osi I7. 3 $233 337
8 Hydrfif" 39431 éHOCgé 1335i; ’55“ 63%; 27.67 1% 7:; 59% [04.67 147.47 2904:?
9 Hydrogen 07ch 2163 gill: , 52.57
'0 'm" ("‘5 5.45 FIQgOIH)’ 3.5:; ISI FIGS?“ fig; Isa Fffl)’ 2.85 Eff-41h IIOII iN’ZAr :: Is - 1%:
'm" ("0) 5.6.5 F7337” 1%? 9.5::
l"°" (005) 5-55 Fig“ 2%: 5.4.5 Fl???) 2%: 2.933 F??? 290 Flag)" ((529 085;. I43 05;;
In” (“53 707 Fig” gig) 4.3: 3.50 F72?" @3093— INE‘S
M59h¢$ium (2.98 Mféoml ' 552:; 2.31 Mgmmk 655+ 3.05 Mfg-0% 3.29 IHEO; 10.42 M???”
Suipha’fe ZOc 5253534 3.28 82533" 8%

 

 

 

 

 

 

 

 

 

 

 

 

 

 

. ,
.

-Lué'.

43L;

\ ”11"” (”-‘V'm

T

C‘
so

A '15:":
"noL‘Au

”-

J...

o o 0
H n "n. p"flflfln..h u.. .Mvnflflfiflu u do Hflflflflflflflfl
.. rm .
2.
o o. c o I O o a n o o a o a O o O
o o o I O o — a n I o 9 n . a a n o a 0
n a a o W“ m n . I ..m 7’
o o o o O I a . 97L.“ .IU n.-
. . .7/ “fiflflflflfl n. wrflnflnu" u ..Cfli nuuuuflunflu
a n a A» o o a o «H ..M
. . . n. a". flu. . a: A4 A...
o o . 1L 0 . o a . o a o o . a o o p o n . 5“ oh»
- a a I.“ o . 0 o o a 9 o 0 n a a o a 0 a n . WM“ my" " fl " u "n u ”H
a o a . . n . 0 ~ g o . n c o o o O a c . j o r“
o v . in c n a o o o - .. o o o o . o . o o c «U +9
. . a v . . o o o . a a . o g . o a a a . ...O ...M ".0
. . . 7.) . . . . . . . . . . . . . . . . . . E C +
n I . AV - . a a o o u c o a a u c a a a a n ....V “V Ida
. . . n. . . . . . . . . . . . . . . U. . . I o n
c . 0 3v - u a a o o u o o c O n a o 04.. a 0 *1: .F .U 1“
. . . .. . . . . o . . . . . . . . . “a . v: .... 1.". H M nu
. . c o o . g o o a o o 0 . c o a . WU; . n a...» “U M
. . . g: . . . o . o . .rV fig o . . . . . o «L o o ...“
o . 0 ..fi 0 o a o o o o 3.4 A.“ c . n o a a 0 ¢ 0 n w. r01 1.. )
o o o «h . . o o o . WA Aw o o . . o . . 8L . . _. F..— .“ Cu
«O u o ofl‘ o o o o o o . 01 .I.; o o o . o o .I.. u I 01* (
44 o n ”ma ...V o o o a 0 PM o o O ‘1; o “:9 +u
0.. L 0 n H.“ a...“ o — H J l/ a 0 01¢ . n s .% I“ a“.
1 o o NL by n 3‘ I; ha“ 2’ u. 71'1”." U oflH TA 1 HQ
. S ..n T. a... .....u C 3 DJ 1.. ..J. nvmuw..".un...Avn. . t C C «J 8
S .1 . ....CP.F v“: u 1. 1.. "LG: 0.9.35 . C . C E 3 ft n
.1 .4, C ... ..u .1 ..1 ... .. 7.1 3 S .3
C 1.. . r. .... u .T 11 ..l C L L. a m... .1. S 3 I
l 3 . L .I.. ,3 1 3 X 2 +.. A .1 a; B e a
1 ...» . .l C .m ...M C O C C v a. C 3 E n” H
& . n.“ .u .1 _ Lu ”.7. me u \ In “\J .n n... «C. ‘1
.o 1 . C ... S .1 n “.... "a: d n..II.u.. E I I e
I 3 2 r V X C .... D m .... n h C C )5 C a t.
C t C T. .. .... .1 ; «...... .... . C n O C (BIK U... T U... U. a
C .l I I ... .... n... A. In. +. (5 n
d n... 3.1 .1 r I u C .1 a C 3 6 3 .1. . .... a L n: NW C C
e A.» ..L 1M 5 C an ...... m C n ...L ...... a.“ .t ...... «u .... L n av +.. “I. «3. n .I +9 b
A. 3 V H Hurt—p.31; V D asl..¢&C+. rv afi CC... 8 $.12.“ r
n a s 1 n 1 53 ....M f 1 ... n i ...." h t a ... I: if vi: K CD 8 n a
C L C C .... .1. 9 i... e u. 3 : “..-. C I 3 ”...! (a v.“ C C C .1. C r ... .n .1 .m ...w «..v
P .1 d s .. g : ... z r. i s a .2 a .4 .2 I :. ... c .... c fix). a m. a... n
....w .... .... S n- 1 3 Ci to: Q S C 1.1: C t 14‘ .m WW ...“ n“ ..m. K .h v. nu a ..Q Q
1 : _ .- . . .. .. .. . . . __ a .... .. . ... s. ... .. ..J m . . .. Yu‘
ND HMMIV 9.“ ”MR,“ u‘ sL 5.“ .u u i 1‘ ”ammonium; 1* . s» ‘ ~T Y.H&P&CI

I I H M S 3 D E C n P N 3 S T: . ...... S C:

V

._’

‘ "733.4 . .
a, ‘éw- V‘O‘V~~ '

A‘
v

m
.L

“unnuA-p“ “I A’h'

W.
hMfl-Ifivt‘ ~ av- v-

 

Q
I
' ‘ ._ .1‘ v.“
. ‘ ‘
"‘I‘ “‘ b~d
‘ \
II ....»
n
U“-0u~‘ . . ‘ '
‘ I
,‘ u,
II§O~ .‘ . ‘ ‘
" I
. o . I ‘I .- I|-,‘.
. I
unn'y.”k“'
I_‘ .
‘ 'll‘
lava...“ .. ‘
\ \
.uh“' rt.
‘
. \vg".‘.‘. \ '
. - ‘
‘ ‘l
«.l_ .
' k1
? K
t ‘.. u
n h‘ ‘ ‘IA\

80.
v
\
o
c . .
. ‘~
‘ . ..
|
~
u
' o
—\
v o

M! "\q -‘ g
10.24.; 9
HA“"“’::~?{~'° 170 Ampfifi 1H 'v-ma f-‘j I‘TVY VA}? ma -- v7. -
v- \ .Lru$..s‘ -‘AVAvuO rét.--9 Pa.» mJ-u'u...‘.~' .1; ALAJILJ.‘
v‘nnfyvx';v -.~\'m-¢
“wk. ‘ V “boa-v.1 . U
" . ‘ ,0 ’- _ ‘. ‘ _ A W I — n -.11 . ,— .
u , __. A ' ‘5 ~ ;.lf‘ 1‘ t P. -,_ - . I. .... . .
t‘ , v v . ..J “\- A-v ULJ‘ L.‘ C1 Lyon-«(‘1‘- LIA '-~ “‘55 J» A- Lg -4 V (.41 ;..
:4. Al. 1 '3 (I. -. . ‘Q‘ ."“." -o‘ ’1 ,Q \ «I‘ l n”..-
A.-."“A\l "LZICQ’U RBI-4.. U—V iuv‘ '1 ”5.5-t-L‘ 4..
t"
‘ ‘ 1...-..“ fl< A, A 1A,
MM‘.‘¥J~A“O l. o I o I o o I o LVIJ‘ 3 U0} Av;
17':- "--. 1‘2," '1" " " *‘fi‘m’.
Uu*¢~w ‘. O O I I I I I O O O 0‘1‘.’-‘ ‘— vov‘l-i‘vl
{iflr ' .. ‘- 61 Aflflt h A1!“
E‘vurvfiliaVLOOOOIIOO Jovvv.) 1 yoy.~~.L"
fl-‘ ,_ 4 ..__ ”A n r} f‘ fiJnr.
VG-I\'¢\-‘¢A‘IC I o 0 o o o o o o o I 1V."‘ L UIV ’7
A,— Q_ ‘. f4 (R A P fl ‘w
r—‘ ‘1 ‘ | - '- "- ‘l "' I p’ "
9“" L‘V'AAUL' L'o I I I I I I I I I VEQV ‘- UQV'223
“TI-~44“. 7"? "V” 3 n Fania
~“d-\-~L¢v.\—. o u o o o o o I O o I]. J. b V'IVF-K-J‘.
t7--fi~_' ....‘q 1 AA"! 1 n --.-r‘-1
‘°d’ -*-L\LL‘&O I I c o o - c 0 c I *OVV“ U.;jl—
.-
577‘17 .31-7“ ”A?! n "f'd"
“J \-"-L CJ'th-‘t'| I o I I O o I I 1—7OV’V 1 VOUJ-udu)
-fll_ _ -“‘y~w~' Ff- If“ 7 A r.f—-'~-q
‘55..--, $2-;L‘.-. I I o o I O [/0 ._...1. / VIV/l'
.._‘- " a “Y‘\!“ ... -'- H“ 0 A f‘u—vr—ri
'* ~-—¢-, LO 4.“..1- 009 CI J'JOV—‘h " V."/I/'J
a. _‘ ‘ P‘I qP‘ f: A hrJ'afi
‘uo--§'~-".‘. O O I I c o . o - L-Ioib ‘- VIle—L
if - (’3 Ah” 1 n I”: (a
‘L’-‘§UCI I. I v I I I I U - I VSOH'UV ‘- V.b~¥&
ERA“ 1. t” PP fin” '7. A fi-r-uf
"“~£5.a nggooIOoII [’0' . / 'Vou'IA-w
:‘—.-3 _- (5" r- -, 1 f‘ A‘I—vr-
U--~‘- -‘.L- I I I I I ‘ - I I I I Lb. ' .. ‘- V .V’vr - "
all //
3““. . ,_+,_‘ AK A," "‘ F A"-"‘ fl
“*r;o‘§vc’o . o o o o a o v I leU'h-‘f ‘- VOV'LVQ
A q
-0\ LI- ' .V‘ . f‘ q-
‘ ‘ . ‘ ‘ ' ‘ .. : . , .o a ', a I— c .. . A o J “A . .' v _ ' ‘ ' .‘l ' I. I" 1" J
“.I.-5&1 Abaws‘VQr-bio' Q “' lucr'odoo v.5 val ’w“ “U v A‘ t’
_. -.. .-.- ‘- _‘.
&V‘-. 5‘ “a . Il‘ .
m‘“ t N '\ . . ‘ ‘ 0 c .“ 1. r: 'I + '_ l . ," . +L _. -'. ‘ " ‘6 L f’ ..- -. f" F r + k ‘
‘IIU -'- &‘uv~J-Q~ ‘vl “L uVAgu-aofi.—D -..v v.1“ £‘V'..5\, b.) ‘ . “V
,.
u" ‘ -.- 3 : .
.,.__ .. «an —:‘;
tic-1:- -" "v“’ r‘ ‘
p: In:
\ - - ~ - P 0“ '. w - 1 .‘u-‘-
L c - s “1‘;— C ‘ “.L +3 V - ‘g i h ‘ \— h. L q u‘ U u.- ‘u fin l 0‘
‘I— ~ AC! n: - +.- g - ,-—--. r . -'.-,‘ "-.r+ .
...; - 9.... ...- n:r.—...I...,-.11.u, & L4 cq...vQ..--....,
‘- —. ---3 ~,- .._+- A" *" ‘1 ." ~“ ' P' ""L '1- 1"“ a 99-51» ’7' + - In.‘
+ ~‘-b‘ «Ah-:Lu- $¢uv L4x..vv- ./ y‘r‘ wvbs- VG.....C.D ...»L Nu yr 'v‘a.“
\‘ “I -. ‘— 3 .. 1 ”A ‘ ‘A+ ‘ - a. ,_ . 1 N. A ‘1
Qi-‘*“b va Cr J‘QAC ;M&-\: GA I“-J-J'-*\r do

 

-3u-

 

1

4.

b

‘

-- V.

ran: 7
uiscznunoua morons

Alkaliniti'oa and hardnau in term of oaloiua carbonata

Bioarbonato ion (3003) p.p.a. 1 0.8197 2 (3003) alkalin-
ity as 0.003 p.p.a.

mbonata ion (003) p.p.a. x 1.667 8 003 alkalinity as

0.003 p.p.a.

Hydroxide ion (03) p.p.a. x 2.9% = (OH) alkalinity aa

0‘00} p.p.m.

Oaloiun ion (0a) p.p.m. x 2A9? = (Ca) hardness aa

“003 p.p.a.

lagoon. ion (lg) p.p.m. 1 .£115 3 (lg) hardnoaa aa

“003 p.p.a.

lulphato - alkalinity ratio
Total alkalinity aa OaOO; X 1.06 = alkalinity as sodium

m‘bonata p.p.a.
Sulphate ion (30)..) x l.l&79 = «dim aulphato, p.p.a.
Grain. per gallon. x 17.1 8 parts per aillion
M'aolyad Oxygen
9.1:... by night 1 0.6975 8 0.0. per liter
O.c. per liter 1 1&3}? = p.p.m. by night.

-35..

'0‘

J—
Q._.&.L-J U "

1'1““ v; ... O
‘

'l

. .t
«.5;

Aim.
Ap *1.— ).
.- b

\- u? ‘r-VC'».
._,-

.10

ii “any;

w-f-vq-A'
J-‘ubtus

1‘7““
A. ox 51“
p

; .‘ag‘

‘ '. --
inn..- u
m—n‘vg-v
an-u-un.&~uy
-&' L‘n

v4 U
"\,‘.
lg“

---,'
VUL’
. r‘.

an

IN - T nvw
lClilZ

P“:—

‘
.- . <,r--‘-'%- ‘~
x-‘vbvsaaat -

T

V.a\&‘uu.ll.-v.n
.

Ah"—TTAM l‘-~'.“

1

i

3 Av .
.1 1i ... t
m Av v“ II 8
. g . .1 C .6 Y“ 8 3. hu. 2 2 3 7| 7:. 1 7/. C .1 .

_ u C u I .... C . C . 3 r) l E 7,, 1.1." 1 o. 3/: ... Ln 3
..C v » 1qu n7. r. ...m — a o a a o a o o m u 1 .u ...a (Gar/Q]
vi liv ,. any . i 7-7/flg 1.1iiu 22/0 . r) "a . anal

“a "J n.» .G ...v LL .0 a, I an. 0’ A7 7 1+ I3 VA an” O n
.1 .u ... u C ... u C I C 71 n.) 3 1 3 Pic 3 . a

z 3.. "r «5 .PL .....3 1i 1.. 1 C159 . t. p...“
I an .... t a: i I. 3 d ...b u
”a 5 .v 5 .u L t . 1 E L 9 u
SC .u.. Tu a: 3 roar— AV ..u:.. o..v ....
flan}. S C fly 2 E). unqli.i C
.c u ”7...... ant "JC7IIXf
wt- i J i G a a : 2 : : z : : a z : z I 17.3 ...».

m it .u +» ,u it, .1. a VA VJ

at “LU +9 ~a W“ :U «(U “H "y 5?“
a1‘Q.wuiu .awfi uufi»

.n .1 t o n . up. D 1 o

.A 6 L C .V ...... +9 .L 7.. V... n t

I 3.5.1; .... n 2 n, r3 2 ,a n
at... i k... L .1 t 9 ”a C 7. C; C) 6 a A v 8 7: . T 1.
.... a :fi mi. v“ av .Ua n.» o . a a o a o o o o .9 b l 5 my

:21 l f C C C r. C . 3 O ...) C 5.1 2 8/ r.) 1 O f b .i 2

”h. ; .... C C 1.1 L .o :6 c2 :70 3/ 71.1 7. 7. . O u ....nl .

3.: u ”.i +. I .5 7/ 1.. ..b in Z L . To

a... c c C V c C 6 d C k .... h l 3

C a“ .L C .l .... I U .L. r“ .3 0 1L .1 C 3 d
«a; ..v «... fiu VA. #4 PHI \ .I \II ) \il ‘1 \./ \Jl \’ \I ) u. Av rd 4... fiv .vv
2 a v w G .u. 3 3; u .D a C a ...u a C «L S r). .L C .l I a:
$1. o+vi Ta :7. ((((\((I\((!\ 2 11.1.3.3 1‘;

L1,..Cflun nvkh+o ...i ....mECS
.... a s . u t w a X X "A X X X X X K v“ .3 cm 6 E i. m
...“ v. 3 2.1 n a H 1.1. ‘31 3 3
a .l . u. C PV .3 we. 2.. T.
&.&d:.:1. n c n .5 f
m. C .a S C .1 i :1 n ,u
.a . v a» mu V +. .1 7/3 win n; :1 O! 40 (V L o i a:
i t h _. a J .1. _ L1. 81/... 7/ 2 f3 ML. .2. d v Q .1 so u. T. 6
h om..1..lw. .1 3... a 2 3/5 711 r, 7. 3 . C .9 Gdlt
..v 9 Inf. 0.. 1+ 1. .a‘ a a o o a a a o a . .“ ..¢ 9 .L in
C i... .. i E .l d w.“ a 1 Ad 7) 1.. :2 7.) Lu. nu _ . .... h h .l 1..

.1 . .v .1 V ...) 1 l P i C in .a

C .... 3 .c G Am .... T. . c o . . . . . m0 «id .1 C
.... R a 2.2 J .a . . . . . . . o . . ..L a. ,1 n .1.
.I C "..." 3 +.. q ..U. . . . . . . . . . . .1; r .1 x... ‘F. .u
.... S C E . . . . . . . . . . p mi u 3 C
CL n e .o . . . . . . . . . . n a. End
8 Pu 0 Av V." v“ a a a o o . o o a a Cu 8 1i. «.0

win... it... . . 3w . E 8 . . __ . t J. 6 C )6
w 1 at 8 3 n t . t d e e t . u v uk L7.

-a d a .r .1. nJi .v .. . l . . .1 a», ....» a e 1.. a: e 1.” a.“ q... 1
C mi -i ..C. .L S b H S H“ a.“ X nu .l .D .T a 01; a1 .a
.n... ., _,J C c A... o .J 3 .l C u . . C .3 I ..E a V. U“ flv V T; "V
_ L ‘ . . .. .
T m a at: Km. 91. r C .3. i ... I 2. C s I
C .3 V 1. a _,.v I. m «.1 1‘ lb Ad I 3..“ W; 1 C ab ) )
.3 Ab .m 8 av "a S U Ea v» I\ (

-36..

"7””:

cuticn

.I.-.A.

0

q
H

‘1‘
an,

fi

......

......

u
.......

1129:.
be cc:
21m
mlit
brine

is not
Pi u:

a! the

Zeolites

in the baee exchange method of water conditioning
eeolite ie need. zeolite has the preperty of exchanging
its eodim for the caloim, nagneeiu and iron in the
water. Thie proceee ie eleo revereable. The zeolite can
be completely regenerated by the addition of a eodiun
chloride eolutiongr the calcium and nagneeiun that the
eeolite hae taken up ie exchanged for the eodiun in the
brine solution. The life and ueefulneee of the xeolite
ie not affected by the regeneration proceee. The life
and ueefulneee ie determined by the phyeical propertiee

01’ the zeolite.

There are three principal olaeeificatione in which
'0": zeolite ralle, vix., glauocnite (greeneand), eyn-
“101: 1c and natural olaye. Glauoonite ie round in the raw
"ate in narl depoeite in lee Jereey. Thie ran aaterial
1' proceeeed by the nee of a hot alkali for cleaneing ad
'°°uring. The aaterial ie then treated with eodiun eili-
°ue and elm. The reeulte oi' thie treatment ie to nuke
“‘9 material durable, clean and hard. Thie eeolite ie
duh green, eiee of grain ie from .30 to .35 n. The
”ight dry ie 90 to 95 pounde oer cubic i'oot. Glauconite
h“ an exchange value of 2,800 graine of hardneee ea
0‘00} per cubic foot and the ealt required for regenera-
‘1on at thie oapaoi ty ie 1.15 pounde per cubic foot.
09‘1“: 15 ehoee the relation of exchange value and ealt

-3'7-

 

 

 

 

 

. - 4 - t -I . 1
. . . .
. . .
i . _
III I. III OIII'.’.05L.IQIIIIL IIIIII .. II I! I
m. . ... .
.. . . ..
. . . . . . 4
i V v o
i _ _ _.. u
. p . F L
. J _ .. q 4
. .. . . .
o. . . _ . _.
- .I J In- - .. f . . . -
I. 4 . .
_ . r J _ h . J .
, .
_ . 4 .
T‘IIIFIIII’,. . Illl ITIvIcIODIII..-r..IIIIII I..~I I O I II I UIIL I'olIiI..IAYII L‘III .IA I I «In’flilelktlII4T9' 0' III |f§la|ttll-L-OI- II
, . . . . . I I .
I . 4 . h u v A.“ m u _
IIIJI..III‘ lull 0-4.II 1‘ I|-P I Oily ‘ II 0|! I I41: I
. . . . . _ .
_ . . ..
. v .

I
l
a
a

'-.

 

 

 

 

  

 

 

4 - ..-...— -

 

3

 
    

X

   
  

..

.
.
... ~P—-'

4

..
.
+ .
.I
6
i

.

o

.

I

A

I

.

-..--

I

.

.

D

I

.

.

.

I

 

 

I f
E .
I #44441: ;

    

 

  
 

 

 
     

 

  

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

._ ... a .3.
.. .I I1
> . _
j . . N . . n . 4 a 4 . I» I I m .. e . .
. . I a . e .. v .. I. . I. _ I L . I I! e u I u
. . . . n I w . I. . _ .. . ... w . . . . o a . ~ 6.4 e . k
. ..I . c . q . o .J. H . . u . . n .. . . w ._ . . v . .. ... .. w
II I OI I . I V a .1... ol I .41! L I 9 I I04 e D e O II¢I . I! II iv .‘II. V. Itlfl eI I .e... oti 0.. III. 4 u..1i-et4‘l‘lfiibleii {In ItIIQeNI‘,
.. . . I. _ .. . — a I. . ‘ u . . I v. .e .. I .. I a M
4. .. . J .. . . . . . . :L . . 4 . 4 ..... . .. . .. ..
.~ . . .. . . . «. w . . I4 H a e H I :fIv .- ._ 4 ... ‘9
I . . . . . . . . {I4 . ... . . . . . .... a ..I .. o._ . . . .. .
YIIIIiIo. I’b‘ ..... ki'niflt IKDI! IIOI Ottllr0.4tee‘|0|lI-!\I ‘l OIIOI IIIOII. . ' 0‘ VI‘IV;OIII?JI,..:IQI‘ FOI't’I ’t’O-W’-I £1 1!! s‘.lv. till I... if
_ _ . ....I _ .. m . .fi ... I4. ..-?1..- . a...-~
. p . I . I. A I I . . I u e e ~ ~ 0 . 9 raci . o I I - .atq.
. _ . M _ e .H . q . ..... .. ... e _ w a I . .
. . _ e . . . p u . I. _ o ..v 1e4. o I. ..... . O ....
W'I \ 'e . u .0 e v 4 I | GI I'IJ ‘I I I I I toI |% I .5 I t O u I e . y . I. v] 41% 1I' .v I A e . LT I v I e I. 04 I I '1 <0 ‘i..t I ‘IIL' VI IIOIV .‘4 unri”. IOI. I II ...Ile .III .I..
I, I . . .a.. . . . — W- .~ . . ... .a 0“ L. . t ... 1e.- .. ~ .I .. 9....
. .. * . . o . . . ,Ie ... .. v . I. . . a I" . or ..m |.. . . .0... I
. , . . .. . . ... .. 4 I . ... . . . . . .- I I I ..
. . . * .. ._ . ... H.. .. .. ....I a I . .. ...» I.H, “ H
I _ J - F Ir ‘ 4“ L l h F
_ .. . .. . . . . i fitQ. J .- 1 . ...Jl ..I i : :J . I _..
. . . . p i . . i . _ .. > . . I. e 4 .A .I .- I .I _ . .. I I
. . . — . . e . «a . n. ... I Q. I. . e. _ I .. _ o .4 a .. ... a H _.. . .
_ . - . u . . v v ... e . - . . r . .e I . a. . . . . I .
l . .I.? o .I - Y<In.k. I I IIILIeIoIOLeuhHIrH I .. W. I P.1I. II... I“ .I-?” I I.. m 1.1.II ..HIIIV 9-.-»? -.9 . .... 4.I..I. .INII .“...l6 .9. I. I..O. I. . .. .1... i
.. . . . , . _. _ i . . . . _ w o . . . . I. . .n . . . . a I . . d. . .
tn .. . n m . I ~ . I a, < v . . . I .. . . . . a I . I .. .. o . M .v . 4 — e
. .o _ . L I .I _ .I . I . . V. I . 4 I . I . . _ .
-4. . H 4 r H . 4 . . M .. . I %. i. .. . . _ . . a -4? h . I. n . . . $0 . . .
Ii'il'lvelo 0...... I I "lelvnl. . I L V II I I‘LWIIIIOIFII‘III
. . i. : u» - .a. .... . . . . T I: .I. a ..
. .o I o _ .... _ . . . m we” a uI o . .m. . H
. . . e , o . . .e o e a . u 9.. . . .. I . ... .A. .
. . ._ .w. _ It . g . .. y r v H.». . .I.. ..I ,. .,.... I ..
II. .tcu. II .0|.IIOI 'IDIIAI I. I 09" u: . lv<iIa he. I tu‘q’Vv‘ )5! 9| gift? on. .IIIIIII , a .w.AII
fin. .. .a . .. . . ..H .l.. . ..._ . I.. .. .. . ...... . ..... . ..
<I I so. I ’ n V H . _ . . . v . h 4e .1. I. . . a
. o ..I u . . 4. e a . I. .e . I v * 9’ —u.. e I ..
.o .« . . ~ . . I. ._ e .4 w. . .. H .e be no. 1 .. u ..
'4 L r . LT . v .
v .~.. . . . I .*__ _.AI. .J. I ‘e... ow. . ... . .. ‘
e.w. . w. . .~ . c . . a . . . .... Ola... ..... ‘ . ._,
I a'l Il’... o . . a. . . . a I . d .4 w o ‘.a . . a . H
V .L lube: e . . ... t. x u k ,.~‘ . ‘. . l . \.. as. .\e‘ .
. _ e I. I e eve . I .t'. I e 1.!“ 0|?- l ‘IP . nal YI . . . Q a
. .
. .

'--.-..

 

.
a
O
‘
‘a
‘0
V
x.
Y‘«
-
l
A
‘g
\
4
\

l.lI.‘I|Ivll _
I I 1”; '.

 

 

..
L .L
1
l
l
t
, . ;.
—-.—a-—.——1—.n«---
,. .
I .

 

 

 

 

I
I
.7
J
F
!
I '_§ .:
. ii
I. '
' 'i
i
"fibfiiwfl
l
I

 

 

. J. . a i . .
* I. . e
.. . .P 4. . 4 .I‘ . o I . ‘ I.I' II'HIIII
I'd I I.vev . . .J _ _ , .c a. .‘ ‘ ~. .~. . . t u
.. . Ia. . l .el. I. * v: . . . ~ .. . ... . .
. . - .-. . I .... I I . .
g e . . . i
. . .fi - . . . _
4 I 00 1 ... I . “q . K II. ll
4%.: I I 'l IIIII

 

 

 

1
!
I
1
1
I
1
I

I
I
I
1
I
I
I
I
1
I
I

. I.
l
H—
1
I
‘w

v
-...-4-_
l

 

 

-.-. J

I f.
1

1

I

I
v I

4

I
._-§.__..—.—.—

HART’ 16

 

 

F
2,:
I
1
1
.‘
1

 

 

I
I
1

‘.

ERN§TEI

IABLE,2

....

 

15¢oié .600

.' ' - .
.-.-.. 1.-.”.1.
1F .
I .
0 - -‘ < I ..
. .

I . . ,. .
A.
I -'
, . L— .
¢-r'r--—“~w-JI ‘-
I I
-..—m~.).¢.—— »-

 

l
-__‘-- -‘- 0’--
I
1
h-.... - ...-

I
I

 

J
I .
|
I

 

PERATUR.

pm I'M-"WATER;

i
1-1
g__1

'fi
I

I
I
L
I
“I
I
I
.L-

...-

.1: -I.

i

 

 

I
I

    

RISI

- o

l .
, . . . I I
0 ' ‘

... _- 4....4 4-44.4...
?‘ . I . 1
i- I

POHWT

      
 

I
I
I
- —»— WM ”“ QM ...”. *1»... M
f
I
1
I
l
1
I
I

. I 1:54w LAINDQLT. 32...?

 

Accapfreo
; 'fiig‘ _
' ALCULATIED FROM

I...

1.11); :

 

 

13539.53

-.. ..— ..

1
I
1
if.
ETHECHAN

WITH
E

. --M +_-. —..
I
I

I
I
7
I

 

. I

.
-....-»

I

    

  

‘ COMMO

.q

{3420. Q4!

.. .
...+--. .... . ...

 

’.4

 

I

TEIIPERA‘TU

 

 

 

 

 

NEUTR

 

1H MIDQH IONIS ;

1 MI

 

I
I
I
g ' .ETRUILIIE
H

 

 

1
I
...

 

 

 

 

 

required for regeneration. In relation to other aeolitee,
glanconite has a low pcroeity and has etrong reeietance

to aggreeeiye watere.

Synthetic aeolitee are nanufactured tron eodiua
eilioate, eodiu alminate and elm. Theee chemicals
are mixed and torn a jelly (gel). ‘i‘hie gel is dried at
a temperature of 100°C. for 2h houre and dropped into
water. Thie ehattere the gel and (one the correct eize
particlee. The character or the tiniehed eynthetic aeo-
ltte ac to poroeity and reeietance to attack by aggreae—
in water ie deterained hy the proportion of eodiun Ill-
inate Ind alt- that are added to the eodiun eilioate. To
obtain a eynthetic aeolite that hae a high exchange value,
a low CiOa ie required, ec eodiu alminate only is added‘
to the ecdim eilioate. Ihie product will have very
little reeietance to attack by aggreeeiye water, and will
not be ac poroua ae aaolitee wade with eodim eilioate
end alna. Theee aeolitee have a lower exchange value, not
eo eeneative to attack and are acre porone. The water
Inet not have a p8 of leee than 6.8 or he leee than 10
can. hardneee or low in e102 to ‘be auitable for condi-
tioning with a eynthetic aeolite. The reeulte of thie
‘reataent ie to aate a uhite colored aaterial which ie
clean and porcne. The grain eiae in larger than the
Elauccnite, neually about .65 an. ‘l'he weight dry wariee

-35-

Iron 30 to 50 pounds per cubic foot. Synthetic zeolite
has an exchange value of 6,000 to 16,000 grains hardneee
as Oa003 per cubic foot and the salt required for regeap
oration will vary from 2.5 to 6.5 pounds per cubic foot.
This aeolits is relatively porous and has not much re-
eietance to attack tron aggressive water. The principal
advantage of this type of zeolite is that due to the high
exchange value per unit of volume, a.smaller quantity is
required to do the same work as compared to glauconite.
Due to the porous characterietic this aeolite will clog
readily if suspended matter is present in the water.

CYnthetio aeolite will not remove iron to the same ex-

tent as glauconite.

The natural or clay aeolites are manufactured
Iron a clay deposit round in both lorth and South Dakota.
it is dried, granulated and baked and then treated with
alkali similar to glauconite. The results of this treat-
Ient is to make a cream colored material. The grain size
1| larger than the synthetic, usually about .75 mm. The
'eight dry is 50 pounds per cubic foot. Iatural aeolite
5‘8 an exchange value of 4,000 to 8,000 grains hardness
‘0 0a003 per cubic foot and the salt required for regens
“rition will be I pounds per cubic foot. This material
has not the high exchange value of the synthetic zeolite
“DI the high resistance to attack by aggressive water as
‘50 glauconite material.
- 39 -

TABLE 9
mam Losers In poms PER scum iron THROUGH mourn:
Unidcrmity coefficient: 1.50
Appearance of raw water: clear

rxcwsivr or GRAVEL, srmxna are“): up EXTERIOR
Effective siae: 0.33 m.m.

2222.245 22.2.2456 23.24568
I W I
0 0257.545 692 7.557 O 9.27.5560 I .
n 9 eeeeeee n 9 eeeeeee n 9 eeeeeee O
. 2222.245 22.2.2456 25.24568 n 8 OkufiJun/wd
1122222
n 02 57545 W 6927.557. m 9.275.760 W8 h
o 8 eeeeeee m 8 eeeeeee o 8 eeeeeee o
D 2222.245 n 22.2.2456 D 25.24568 m
) ,
a m a .... a m u . m
n .I.. 7 0.2.0754...) n in 763.4557. M ..u 73755.60 m we 8JJJJA$7H
..............
r 2222.245 ... 22.2.2456 r 22.24568 .... r1122222
f e f I e. o 37.0
O m 0 n 0 a I P
e 8 02 5754 5 I u. 6 92 7.557. e 8 9.27.556 0 I I
m meaaaai..&m ”6.22.13... ..2... m m6hh}t..56..a 2mm
r . r r a 8 01.“ I euhtunlbewlel
e e e I e I 0 P1122222
t t 8257545 t .- 6927557. t t 8.275560 F 6
u u 5 eeeeeee u u 5 eeeeeee u n 5 e e e e m
m 1222.245 m 22.2.2456 n 23.24568 0
u . u u n . w e u
r u 7.257545 r n 5927.557. r u 7.21.5560 an I2624578
O on. eeeeeee O on. eeeeeee o 0‘- eeeeeee g'eeeeeee
P H 1222.245 P H 22.2.2456 P H 23.24568 5 “1122222_
..“ a m .... h a . a
0 50 5754 5 o .48 2 7.557 0 51 7556 0 P m
I I’m-undeandmeephe/r ”39H?“ eeeee ' razxe/eeoa.ea
e W e. b ..n e m _._ n mmu479wcurw78
. r1122222
w I 9957545 M. h 14.61755? W I 417.5560 M 4 P
a. 2 eeeeeee 2 eeeeeee 2 eeeeeee
8 122.245 8 22.2.2456 23.24568 1..
r
. .. .. a h
P 7.8 57.545 P 7507.557. P 307.5500 n w.
.1. e e e e e e 1 eeeeeee 1 eeeeeee
I 122.245 I 12.2.2456 m 2.2.2428 f D ....ttht...»
.m m m t h t 0 d 1.1.1.11...
1 n 5580075 m flu 77.55077 tu 010700.) II R 2.245678
m ...e ooooooo ...e eeeeeee m ‘ae eeeeeee
8 1123.24 0 12.2445 8 123.2567 M
.2 .I. 5

u ...............t.... h .......t. .fit. h . . .... . . .

Chart 17 shows the reagent adjustment necessary for
lime-soda ash water treatment. The usual tests for the
alkalinities in the conditioned water are made by neutral-
laing a 100 c.o. sample of sater with l/zo sulphuric acid
to both the phenolphthalein (Pht.) and methyl-ornge (li.0.)
and points. The rate of decrease or increase of both the
lime and soda ash can be read directly off the chart sith—
out calculations. The area marked “Degree of Tolerance“
should be located by experiment. The location will depend
upon the hardness that it is desired to maintain in the
tater. The area should be located so there will be some
hydroxide alkalinity present with respect to lime. Iag-
nesiu should be removed as magnesium hydroxide. This re—
quires a slight excess of lime. The chart is based on ?0
Percent available caloim hydroxide. The following example
illustrates the use of this chart:

deeming that titration gave the following results:

Pht. with l/ao 3280., was 2.2 cc.

me. with l/zo 3230., m 3A cc.
The coordinates of these readings intersect on both a 27
degree diagonal ad a 45 degree diagonal. follow the 27
“Ceres diagonal to the right and a decrease of 22.2 pounds
01 lime per million pounds of water is indicated. Follow
th. 45 degree diagonal to the left and a decrease of 19.2
pounds of soda ash is indicated. By making these adjust.
lento the condition of the resultant water will fall with.

13 the “degree of tolerance'.

-h1-

 

 

 

02_0<mm Fri
O.

6%: 03.2 .00
O.

 

 

50
, 5.0

CHART I7 .

 

 

 

 

 

 

 

 

 

 

7%
4%//5 ’9
j? .

é
//
7
/

 

 

 

 

 

 

V
j
g
V
W j
? f.
/ If
//
40
MO READING

 

 

 

 

 

 

 

 

 

 

 

G .-
m ,. .- . /
.t d
T. m T. - .... j w /
Iv A _ .
.... T...T-.. / / / z. /
F ”FT ......L 7
\JTth L.
W m .n“ ....n .1 .
r s L ... h .4 04
u .1... .-
J _R_ In a 5
om... . . . ..
AFA 1w . H
w H o
m A mefi . 2
E D -.HT...AS m N
G O .-:.-.....i,.. L .
M S F.x..\llwl A C
_ ..., .T . ..
R CM. 37m. ..
I q_m.A\.C.LWH .fi
L LBMU ...
Pb?
g.
CA
..me

 

 

 

Chart 18 shows the relations between hydroxide,
carbonate and bicarbonate alkalinities as determined by
titration on a 100 c.c. sample with I/20 sulphuric acid.
The following method of testing and use of Chart is de-
scribed in a l.l.L..A. publication, 10.289414. method
of Test. leasure 100 c.c. of the water to be tested in
a volumetric flask and empty into a 200 c.c. casserole.
Add. four or five drops of phenolphthalein (Pht.) indica-
tor and titrate the sample with [/20 sulphuric acid un-
til the pink color Just disappears.

'The masher of c.c. used is the Pht. reading. lext
add. two or three drops of methyl-orange (11.0.) indicator
to the same sample and continue the titration until the
color changes from yellow to orange. The first definite
tinge of orange which does not fade on stirring is the and
Paint. The total ntmber of c.c. of acid used starting
tro- the beginning of the Pht. titration to the end of the
.“hrl-orange titration is the: 1.0. reading.

“The various alkalinities may be read directly from
“10 chart, eliminating calculations.

'The alert is divided into two areas by three data
111;... :2. the x-axis along which the carbonate alkalinity is
"to, a heavy 21 degree diagonal along Ihich bicarbonate
ind hydroxide alkalinities are zero, and a heavy 45 degree

-112-

 

diagonal along which carbonate alkalinity is zero. (All
alkalinities are expressed in parts per million of cal-

cium carbonate).

'The area included between the x-axis and the heavy
27 degree diagonal denotes amounts of carbonate and bi.
carbonate alkalinity, carbonate alkalinity being indicated
by lines parallel to the x-axis, and the bicarbonate a1-
kt]. inity being indicated by lines parallel to the 27 de-
groe diagonal.

“The area included between the heavy 27 degree di-
agonal and the heavy 45 degree diagonal denotes various
amounts of carbonate and hydroxide alkalinities, carbon-
at. alkalinity being indicated by lines parallel to the
heavy 45 degree diagonal, and the hydroxide alkalinity
being indicated by lines parallel to the heavy 27 degree
di‘zonal.

'Dse of mart. The readings. obtained on a sample
of uter were:
l'ht. reading 1.0 c.c. [/20 82601,
5411.0. reading 2.8 c.c. [/20 Bacon
Ind on another water
Pht. reading 1.6 c.c. l/20 112801.,
b {11.0. reading'2.4 c.c. 11/20 32801;

-15)...

“By reference to Chart 18 using the results of test
s; the coordinates 1.0 and 2.8 intersect in the area of
biocrbcnates and carbonate alkalinities, on the horizontal
line (read right) showing 50 p.p.m. carbonate alkalinity
and on a 27 degree diagonal, (read obliquely left) showing
20 p.p.m. bicarbonate alkalinity. Using the results of
test b; the coordinates 1.6 and 2.4 intersect in the area
of carbonate and hydroxide alkalinity; on a 27 degree di-
agonal (read obliquely left) showing 20 p.p.m. hydroxide
alkalinity, and on a 45 degree diagonal (read obliquely
right) showing 40 p.p.m. carbonate alkal-inity.‘|

 

 

 

 

 

 

 

  

    

 

           
   
 

02.931 ...02 0%.: 08.2 ..0 0.
u. m_ N. I O. . m r
o - 1 - T - 4 +4.- - 1
4. . coo . ooh. were man. . on... 009. on, on, on, on.
. om; . . . W . . H . Mia... ......zflinaq mh<20mm<9m .
o... . m r r . . m
_ v. 1-. .T ”e 91.31 .+ . t .v T . e t m T . v . . H T . i . .fl . t . . m
9 00 . V. W m . W . . m
V T . . w M . .« . 4 . a. .
N 484-1.“. -+.-v WY-.. .TT‘ ,1“. i .
em. , .3. n, . l _ 9 m .
f . - . .w ~ . . . a. w .
?m 03” w. 5 .M r w r
. e ..u.-. - v. . 0 .WII - a r . . 1 0 + t t v
. .. m. n . W - . r
N ,0? .+ . .. . .
+4 . ..OON . T T . .t - - - . . T w. .
O . . . H d .. . H . h M
CNN H d . . r . . ..
H . . w . _ m .
Or. MEWWTx--+ T W
h. W. . ... . a H . .
A.” new “ u
v * «
E . . w . a
3 . . m .
V . . n . .., .
m. .. - 2 ...-2...: -..---c,
N . . . . H . . m .o
9 .. H . M . . 29.203221... n 38.0 x in...
o . . . _ . . . . . . 592$ 00 oo. 9 904 023138 om\z 0263
m H two... Wt- 1- t T- «Tr-1a.. ...-It)...- woo. . .. .- 30.:th A029 002.20 :1me a fire,
. 9. . . r . 2.341.150sz zoannmnkzommg 5.20.20
on m H . a. .5. 29.3.2 awn wens... as. $122.35..
. a - e) \ .
m _ .09... 1......» ... .._ .. . T .99. . $428.35 . 2.2.33 .920qu
e
.a,le%%%
.9 an 9.9 o 83.3 20.2%. 20m...
91 -.- Try)!" MW. mm..§23<xn_< uO 20.2.6.2.qu 10.2 .5?an

—v -\]|\./.\/\/

I

 

 

 

 

 

CHART l8

 

>\‘ ~_"——-

Ahk. ......

Chapter III

'1“ fi 7" '71? "a '“f‘fi fltfn'Tfi' .5 TAM-n 1 "‘a w-ua
ST ‘\ “‘13 SP‘C IfI 93$$$C¢IJ 2v“ v--a.‘...Lv:J..-v 14an' I1: haTL.
fiancnvm#r\‘Y-fx'(\
VV;.~.L~AV&¢*¢‘J
w - 3 H; "‘
Swp11ng and Test 1? 0
-~ ' 0 -“. < -= of, - -
1.. The COmpCSlticn 01 the chem1oais sh all dete rn1nei

by euaalyzinr seaplee taken protp

al at the point of

materi

£2. Whe. chehicals are

ly upon the

shipped in bul k,

I

arrival of the

consumption.

(0
b
H
H

the sample

be 530 taken that it will repr eser at an average of all parts
Of tlie shipment fr om top to bottom, and shall not contain

a diSp‘oportionate share of the top and bottom levers. It

(in
shall be crushed if

911611 tered" to provide two l-lb.

Shiilgl be 1'ept carefully sealed for use in a possible

99
CD
Ti
H
9-“
(—1;
(D
Q;
31’
O
H
O
p.
U
CD
f.”
d'
(D
H
O

in packages a
f 330:2: various
Sr».

‘*“l;7led as in the above

Ll‘. When Sampling qllic’iime

Siblfi,

in order to avoid undue ex

necessary,

the case of lump lime 100 lb. ,

mixed thoroughly and

samples, one of which

4.
0

1*all be 5311:2131.

.. that the operation he oeniuctei as

to the labora

c+

tored

rfin‘fi

least 3 per cent of the

parts of the shipment, dumped, mixed and

tory Shel
iéut container in which

until the shipment hae

'5'
U)

('0

H

o

Resainplin?

1. Notice of dissatisfaction with a shipment based on
these specificationsm ust be in the hands of the consignor
Within 13 days after the receipt of the shipment at the point
Of destination. If the oonsignor desires a retest, he shall

notify the consignee within 5 days of receipt of the notice

0

f comp1aint. The duplicate sample shall then be forwarded

H)

or a test to some laboratory agreed upon by both parties.
This retest shall be made at the expense of the consignor.

The results of the retest all be acce ptcd as final.

Lime (Cat?)
81:11" ing
Ellen luuzps of quicklihe are immersed in water, they

shall readily disintegrate into a sac pension of finely di-

Vii e :1 material .

Cheiniical Requirements

1 - For quicklime the standard of composition shall be a
9011 ent of 65 per cent available calcium oxide (CaO), but
quickl 1me of less CaO con ent may be accepted where condi-
“-0113 of service permit and the price of the less pure pro-
duct is such as to give increased economy considering the

additional quantity of both lime and sludge to be handled

3 - For hydrated lime the standard sh all be a content of

90 percent available calciun'. hy roxide (Ca(OH)2). The mag

Hes-inn salt content shall be less than 3 per cent.

-146...

Ecnus and Reduction
Where large quantities of lime are to be purchased it is

recommended that the contract be drawn to include a bonus

("

or a reduction of 1.5 per cent in payment for each 1 er e=nt
by Which the available CaO or Ca(0’:i)2 exceeds or falls below

““3 standard percentage. In case of small purchases the con—-

“-va

97nd...

tract should permit rejection for failure to reach the etc-...

ai-d.

Packing and Shipment
Quicklime may be shipped in bulk, in wooden barrels, in
metal drums or in waterproof bags, packages of each kind to

be of uniform weight. Hydrated line is usually shipped in

Paper bags holding 50 lb. net each.

So a. Ash (Nagoo3)
Cheillical Requirements

3 58 per cent light

9)

The soda ash shall be that known
soda sh and shall contain not less than 98 per cent of sodium
Cart, onate (135.2303). The material shall be in a dry po'v'zdered
form, stall contain no large lwnps or large crystals, and

Shall be free from chips and other foreign patter.

Alum (Sulphate of Alumina) (A12(SCh)3 4» Water 0" Crystal—
lization)

Ch em 1 cal Requirement 3

1 . The material diall be basic, shall contain not less than

.1”.

17 per c2 nt available tater- soluble aluzeina (A1203) and

shall not contain more than 0.75 per cent iron (Fe303).

Insoluble Matter

1. Sulphate of alumina from which the in soluble mate al
has been reao'ed shall contain not more than 0.5 per cent
of material insol his in istilled water.

2. Sulphate of alumina from which the insoluble material
has not been removed shall contain not more than 7.5 per

cent of material insoluble in distilled water.

f Lumps or Grains

0

Sizes
1. Lunp sulphate of alumina shall range in size from B/H
o} in
2. Ground sulphate of alumi afor use in dry-feeding

machines shall be of such size that not less than 95 pe

cent shall pass a woven sieve havir -g 13 meshes per linea

in.,a nd 130 per cent shall pass a sieve having 4 meshes

per linear in.

Packing and Sh ipmen
l. Sulphate of alumina may be shipped in bulk, in bags

of uniform weight or in barrels of uniform weight.

Sulphate of Iron (FeSOh7H2 0)
Chemical Requirements
1. Sulphate of iron shall be what is connonly kno n as

ugar sulphate of iron theoretical formula, Fe Soh7H20.

.. us.

17 per cent available water-soluble alumina (A1203) and

shall not co r1tain mer e than 0 .75 per cent iron (F6303).

Insoluble Matter
1. Sulphate of alumina from which the insolue le mater a1
has been removed shall contain not more t.

l insoluble in distilled water.

..Jo
w

of mater
2. Sulphate of alumina from which the insoluole material
has not been removed shall contain not here than 7.5 per

cent of material insoluble in distilled water.

Sizes of Lumps er Grains

1. Ln1p sulphate of 1111111 8.111 r1 ge in size from 3/u
to 3 in.

2. Ground sulphate of alumina for use in dry-feedin
machines shall be of such size that not less than 95 per
cent shall pass a woven sieve having 13 mesheh oer linear
11., and 130 per cent sh all pass a sieve having 4 meshes

per linear in.

Packing and Shipment
l. Sulphate of alu.mi .a may be shipped in bulk, in bags

of uniform weight or in barrels of uniform weight.

Sulphate of Iron (FeSCh7H20 )
Chemical Requirements
1. Sulphate of iron shall be what is connonly known as

Sugar sulphate of ire n theeret ical formula, Fe Soh7320.

5 46—

2. It shall contain not less than 9
ferrous sulphate (Fe30n7320)
per cent of free acid and shall be clean and free fron all

dirt and particles of foreign hatter.

Packing and Shipment

Sulphate of iron may be shipped in bulk in pap er-lined

(1‘
1.14
to

tight box cars, in bass, in arrc or in casters, packages

of each kind to be of uniform weight.

Caustic Soda HaC1V)
Chemical Requirehents

e caustic soda shall be that kncv a'n as 76 per cent actual

0

test sodium oxide and shall contain not less t1an ,3 per cent

sod ium hydroxide (haOH). The dry material is manufactured in
three forms, viz. 1 1d, ground 'nd flaked.
Packing and Snipnent

Solid CEJSt ic soda is ustenarily shipped in steel drums
containine approrimately 700 lb. net weight. The ground and

flake material is commonly shioeed in steel hr ms or in

5
C‘
O
{J
(,1
D
(’0
{11
H
m
H
(D
O
U
:3
(1'
fit
Lb
15
5)-
{J
C 1
93
r
”O
H
0
:4
PJ-
E
(if:
d
H
4:
Q
3
H
0'

Barium Carbonate, (Withe rite), BaCCE
Chemical Peq1iremer1ts

This material shall consist of not less than 93 per cer 1t
barium ear hcnate (Bude). The hydrochloric acid insoluble

matter shall be less than 1/2 ofl per cent.

-19..

7“",
“LA -

3

¢7'r\"‘\

1")

,-
\r

(F
U\ 'v-fii .- 0 u..“_V,~

1: ..
, d-J
'3

to

Fr?“

.i‘ N 00

.1...
.1...
a;
.-.1.
C

*1.

n5

7qfi1“11"'

--11“-

HAOtaJ u... .- ~l~¥.‘

’\

a

fi
J'.‘

,-

more th

~_

t

scluhle in warm '

+9
‘

_. .. w
h u

C
..., v
.v u
‘3
1‘

3

1a..“

.5.

5"“

kc 1‘3

,. 3.41" -

‘qu‘d‘- ‘-
Triscdium pho

hm,"

Q

I‘-

a:

AL

L
LL

‘
L

4;

Disodim Phosphate, (laZHPOulZHZO)
Gheaical Requirements
Dieodim phosphate for water treatment shall contain not

less than 25 per cent of available water-soluble POh. The

water-insoluble matter shall not exceed 1/2 of 1 per cent.

Packing and Shipment
Dieodim phosphate say be chipped in bulk, in bags of

unifora weight or in barrels of unifora weight.

Bodim Gloride, (laOl)
Ghenical Requirenente

The sodim chloride shall contain not leee than 98 per
cent sodim chloride with a mini-m of calcium and nagne-
sin. The aaterial may be either rock salt or evaporated
salt. The color shall be white to grayish white; indicap
tive of cleanliness. The phenolphthalein alkalinity shall
be zero. The salt shall contain no grease, fat or oil con-
tent. lt shall be free fron chips and other foreign natter.
The fineness shall be between 8 and 50 aesh. The salt ehall
dissolve rapidly without packing, farming a clear solution.

-51..

Chapter IV

nrrrmunrros or ovum! or cannons sequins

Lime on be obtained in two forms for water soften-
ing. Both forms are widely used. These are the calcium
oxide (OaO) or quick lime and caloim hydrate (Oa(03)2 or
slahedv lime. Commercial an contains 85% available OaO
and the cost is 811.00 per ton. The calcium hydrate
(hydrated lime) contains 90$ available «(03);, I36. the
cost is 81km per too. On the basis of available OaO
the quick lime can be evaluated at 312.90 while the hy-
drated lime is 820.50. The quick lime is difficult to
handle and store; extreme care and caution must be exer-
cised to keep moisture away. considerable heat is evolv-
ed s... it is slaked. lo such danger exists with the
hydrated form. As a general rule call plants use the
hydrated form and larger plants the oalodm oxide. The
oxide is considerably cheaper in not only the cost of
the lime, but requires a lesser quantity in cubic feet
to soften a given amount of water. The storage space
required is consequently less. If it is desired to con-
vert calculations of chemical quantities in terms of
M to the equivalent «(08);: the quantity of mo must
be multiplied by 1.25.

The calculations for the quntity of chemicals re-

quired will be based on the molecular reactions of the

-52..

'—

      

 

—9~._..
s

 

 

AIS.

   

l

 

 

 

 

   

 

 

 

 

 

 

 

- [I ...s y- 1.. 1...: ill- -I ...... Ail: _1 111.111.111.11I..I--.|.-.I.In11.il t l t- - .... -- - - u
a M _ ” ... . . l . u M
_ . . . .
. H m I.“ .. M . . ¢ .. _
- .. .- ..-. . - - - - i -. -.I I-.- ,- ---. a
_ w a W. $0.127...§H_zj<§<z_20%d:oum . . ....mH
. w a - 1.1.-.. L - .....1. -. .. . _ .n .i A.
. _ _ 2 . . .. a. . . . .
m U % W . .71.! u H _ .. ... H om H
-- --1~...-:i-..-----.--..-..- - 1 7.11 1 71. .. - ...- 1- -.--tic...
_ .. .. ~ . _ .. . ls _
l w . . M... .. w 5.... * a w _ l . H.
w u . 1 .... w . a . i m _
-w. - -- l l . --.»..-I-iT-irsl2 :41---- “ - f: -- s
m n l w _ . H: . . W l
. a . s s . ... ~ . .
m _ . _. W M M . H . i
o 1.3 .-.fo?i|0.s~ .m _ .UF II . 111.1.--110lll tilithlx.’ .
. _ w. H .M a .. M m .
n U i a a u _ ..l
. H- - ...- .. I 3-.. 7- It 9 1 gr, 1 -- - .... - -11}: I - -. 1 -- - . i
w m a. . . 1 W .... _ :1 m .. M a . M .
m 1 a... l A... - H. a; l-.. w- a ..Pn
. 1 b M a . . . .. _ . .a ; .P .
-..... ..-- ....- -. .. _ ...--... ms:-
. . .. . . . _ _ . .
a U . . a . . a. . . . . . _
. _ fl ... r- H; - ..rr . l J ...... I w 1- . I. .
H . .m .1. ,. . H .. .H H. _ . . . W
-1 1 -. s .- ---.r..1...-.l.....-T .111----T:tit-....ii-1l.--..----- ....M--.i
. .. ..H . . m h a E
. 1. . .L t.
..M . ”In .
M
a:

 

 

 

 

 

 

 

J."°‘Y""“"' .--._ --4 -J.-._s_.-0--—_.1—.o
e O s a f s

 

 

. t _ . _ .. .l
w m C- a U a U H H
H. at “- n . .w . .l .._
7....-.S-.. .TR--...--.:-- .-- l- -- - - ..J. --. --.: ....
a . P O _ l _ a ..

c n. -o .... ..-..1. . - w .. in u .-
..N. .F ..H _. w . . a .7
EP . a . .u L
_ VA! 4 I... . l fl . ..[Lf
“Z.” ._ .m ... m m . .l a.
+A . .. f- -.2 - . .7 i- ...... .-3 34.5.

M a . . .g. M 3.. ...
1! --H ... ...-12......3... .. .- 111.2...-
_ . . a 1 _ T . . l
i 1 -m .27 . . l H. . .. a -m -- -,..-.-..+-.-.-
H .... .. .. _ . ...
. .r .r....: + J... _ .L. ._ ..r “.....th...
. H 1 .M w . 4. .4 A..1.TW JJ ..|WI14
v ,. .. ...... a e . ..
......

 

 

Isl '.

 

 

l'lte‘ eltl

- .__- e

_.. Ear z. era-Lima?

 

. m p
. . a
. s . V s
u s .

‘1 ‘llllf‘,

 

 

 

.17-:- Vu *.Ix It

 

lone in the Inter Iith the added chemicals.

The quantity of coagulant anet be determined ex.
periaentally. The quantity varies with the temperature,
change in chemical composition, pH and reaction tip.
for the typical liichigan deep Iell Inter, the quantity
will he on the order of 10 p.p.m.

The addition of 10 p.p.n. of alun (alminun eul-
phate, £15801”le 320) will decreaae the alkalinity
3.5 p.p.n. and increaee the eulphate content 11.33 p.p.a.
Alkalinity ae calcium carbonate in equal to the bicarbon-
ate divided by 11122. The decrease in bicarbonatee will
then be 5.5 p.p.m. The water analysis in ionic torn and
parte per nillion ie:
Carbon dioxide 002 10.3 Bicarbonate 3003 337.5 (31113-535)

Oalcim 0a 108.0 Sulphate e01. 73.9 (69.6 +£1.13)
Iagneeit- lg 32. l chloride 01 6h». 9
Sodim la 7.8 Iron Fe 1.0

the reactione applied and factors need are for:
002 Reaction h i‘able 3 , 'rable fl 6-0

lg Reaction n " 3 3 " # lit-c
BOO} Reaction d " 3 ; " 1|» 3-6
0a Reaction e " 3 3 " # 11-1.

i'he line (an) require-cute, producte formed and the colu-

ble ione introduced are as follow:

-53..

a. 10.3 002 x 1.28 0a0 = 13.2 0a0 required
b. 10.3 002 r 2.27 0a003 8 23.“ 0a003 precipitated
product.
c. 32.1 Hg. 1 2.31 0a0 = 7M.2 0&0 required
a. 32.1 lg. x 2.110 13403)... a 77.0 ng.(oa)2 pre-
cipitated product.
e. ,32.l Mg. 1 1.65 Ga '8 53.0 0a eoluble ion intro-
duced.
1. 337.5 3003 x 0.h6 0a0 == 155.3 0a0 required
5. 337.5 3003 x 0.82 0a003 = 277.0 0a003 precipi-
tated product.
h. 337.5 3003 r 0.k9 003 t 165.H 003 eoluble ion
introduced.
1. 1.0 to. x 1.51 0a0 '3 1.51 0a0 required.
1. 1.0 to. x 1.91 re(03)3 a 1.91 re(03)3 precipi-
tated product.
h. 1.0 re. a 1.08 0a. 3 1.08 0a eoluble ion intro-
duced.
The eoda.alh (812003) requiremente, producte formed and
the eoluble iona introduced are ac iollcwe:
0a to be conditioned includee 108 p.p.n. in original
water plus 53 p.p.n. introduced in item e, and 1.1
p.p.m. introduced in iten k, total 162.1 p.p.m. It
in deeired to have the reeultant water contain 85 p.p.n.
- hardneee. Thin will reduce the 0a to be conditioned to
162.1 - 31.1 = 131 p.p.n.

-511-

1. 131 0a 1 2.65 11.2003 = 3% ”zoo; required
I. 131 0a 1 2.50 0a003 8 327 0a003 precipitated
product. .

n. 131 0a 1 1.15 la ‘8 151 Na eoluble ion introduced
it '111 be noted that in item 11, 165A p.p.m. 003 ion woe
introduced, and thie amount then calculated to the eoda
aah equivalent 106 la2003/60003 = 1.767 will reduce the
amount of la2003 required for the conditioning of the Ga
ion.

c. 165.1; co; 1: 1.767 = 292 [0.2003 equivalent

p. 396 la2003 - 292 [@003 I 51!» “2003 actually re-

quired.

q. 185 u - 156 la = 29 la ecluble ion actually in-
tnoduced.

r. 327 0a003 - 276 0a003 = 51 0a003 precipitated pro-
duct.

The total lime required will ho the sum of iteme a. (13.2),
c.(7u.2), f.(155.3), i.(1.51) and.an exceea of 10 p.p.m.
The total ie 250.2 pounde of pure 0a0 per million pcunde

of water treated. The commercial chemical ccntaine 85$
0&0 co the total number of pounde of commercial chemical
I111 he 25“.2/.85 = 300 pcunde.

The total acda aeh required will be 5“ p.p.m. plue an ex-
ceae cf 25 p.p.m.; a.tctal or 79 p.p.m. The commercial
chemical containe 98$ lm2003 co the total number of pounde
or commercial chemical will be 50.6 pcunde per million

pounds of water treated.

-88..

The next step is to determine the probable analysis
of the water after treatment with alum, lime and soda ash.

The chemicals added are 25h.2 p.p.m. 0a0 and 79 p.p.m.
la2003. it is assumed that the impurities in the commercial
chemicals are insoluble. The soluble ions found in the con-
ditioned water before recarbonation are:

002 none

0a 12 p.p.m. (solubility at 51°F.)

Iagnesium 13.5 p.p.m. (solubility at 51°F.)

Sodium 18.9 raw water + 29 4 10.9 Excess - 58.8 p.p.m.

Bicarbonate none

Sulphate 69.6 raw water +*4.3 p.p.m. = 73.9 p.p.m.

Chloridss 6h.9 p.p.m.

Iron .8 p.p.m. (residual)

Oarbcnate lu~p.p.m. (calculated from excess la2003)

Hydroxide 6 p.p.m. (calculated from excess 0a0)

pH 9.0

The quantity of 002 necessary for recaarbcnaticn to
fix the carbonate remaining in the water after the clari-
fier is calculated as follows:

003 4 002 «I» 820 .9 28003 lach p.p.m. 003 requires

60 4 M + 18 ...122 .733 p.p.m. 002

also
on + 002 -'H 003 Each p.p.m. OH requires
17 4- 1m 4 61 2.59 p.p.m. 002

- 56 -

Ids .

Good operating practice dictates that a residual
002 in the water should be on the order of 5 p.p.m. The
total 002 required then will be:

lit p.p.m. 003 x .733

10.3 p.p.m.

6 p.p.m. OH x 2.59 = 15.5 '
Residual .542 "
Total 30.8 p.p.m.

The E1003 remaining in the finished water will be:
lit p.p.m. 003 x 2.03 = 28.1} p.p.m.
6 p.p.m. OH x 3.59 - _21_._6, '
50.0 p.p.m.
One pound of coke will produce three pounds of 002.
The quantity of coke necessary per million pounds of water
'111 be‘30.8'-p.3 .-1o.3.po\mdc.

The total solids remaining in the water is calculat-
0'1 as follows:

0:100) precipitated item b (23.1%), g(277.0),r(51) - 351.5 p.p.m.

lz(on)2 Precipitated item d (77.0) s 77.0. '
hWon); precipitated item a (1.91) =__l..3 I
Total 430.3 p.p.m.
Total chemicals added are:
0.0 254.2 p.p.m.

182003 ..19... '_
Tat“ 333e2 pope's

-57..

The reduction of total solids will then be 150.3 -
333.2 8 97.1 p.p.m. The raw original water contained
.#33 p.p.m. total solids so the conditioned water will
contmin 335.9 p.p.m.

The finished water after leaving the filter will
have the following characteristics:

Total Solids 335.9 p.p.m.
8102 3.5 "
Dissolved metallic ions

Calcium 12 '
iron .2 '
Iagnesium 13.5 '

Bcdim 58.8 "

Dissolved Ion-metallic ions‘

Bicarbonate 50 "
Carbonate none

mloride 61+.9 "
Hydroxide none

Sulphate 73.9 "
Dissolved oxygen 6.8 '
l'ree Carbon dioxide 5.0 "
pH 8.2 '
Alkalinity as 011003 #1 '
Hardness as 0a003 85 '

-53..

The calculation for the salt requirments when using
the zeolite method of conditioning water are as follows:

From 0hart15,0.ll1 pounds of salt are required to
remove 1,000 grains hardness, calculated as 0a003 when
operating the greensand zeolite at an exchange value of
2,800 grains per cubic foot. From this relation, one part
par million hardness calculated as 0a003 will require 2.87
Pounds of salt. All the water passing thru the seolite
beds will be softened to zero hardness. To maintain 85
P-Pomi. hardness in the finished water it will be necessary
to bypass some of the water by the zeolite beds. The amount
of seat required per million pounds of treated water will
thin be (300—85) x 2.87 1- 90* pounds of salt.

The percentage of water that must go thru seolite

0019 '11], be 315/1500 ' 78.8 percent.

The quantity of 0a and lig in the finished water can
b0 determined as follows:

108. p.p.m. 0a x 21.2% = 22.9 p.p.m. 0a

32.1 p.p.m. Hg x 21.2% a 6.8 p.p.m. Hg

The increase in sodim due to the exchange of is for
“2 catand lg is:
103 - 22.9 0a 3 85.1 0a removed x 1.15 = 98.0 p.p.m. la
32.1 - 5,3 [g a 25.3 ilg removed x 1.89 é 31.1 p.p.m. la
1%.7 p.p.m. la
la in original water __;§_,_9_ p.p.m.

168.6 p.p.m. la
- 59 ..

The increase in total solids is:
185.7 p.p.m. wt.cf la added
85.1 4 25.3 = _119Ԥ ' 1 ' Ca and Hg removed

35.3 p.p.m. net increase

The finished water after leaving the seclite filters
will have the following chemical characteristics:

Total solids u68.3 p.p.m.

lilica 3-5 '

Dissolved lstallic ions

Calcium 22.9 '
Iron .2 '
Iagnesium 6.8 '
Sodium 16h.6 '
Dissolved Ion-Metallic ions
Bicarbonate 393.0 '
Carbonate none
Chloride ‘ ou.9 '
Hydroxide none
Sulphate 69.6 '
.Dissolved Oxygen 6.8 '
. free Carbon dioxide 10.3 '
‘pH 7.6 '
Alkalinity as coco} 281 '
Hardness as 00.003 85 "

To the finished water, after the zeolite treatment,
must be added 0.3-p.p.m. liquid chlorine to obtain ster-

ilised water. This is not necessary when lime is used.

The calculations for the amount of chemicals re-
quired when conditioning water by a combination of lime
and zeolite treatment are as follows:

The total lime requirement will be the same as for
the lime sodasash method of treatment, visa 250.2 pounds
of pure CaO which in commercial chemical is equivalent
to 300 pounds.

it will be noted that in item n, i65.uip.p.n. 003
ion was introduced. ..This amount when calculated to the
soda ash equivalent amounts to 292 p.p.m. la2003. This
will remove:

s. 2 2 111 p.p.m. Ca ion treated

2.6%
t. 111 Ca x 2.50 Ca003

277.5 Ca003 precipitated.produot.

The soluble ions found in the conditioned water be-
fore recarbcnation are: ’

Dissolved letsllic ions

Calcium 108 4 53 - D11 4 8 (Excess) = 5M p.p.m.
iron .2 p.p.m. residual

lagnesium 13.5 p.p.m. (solubility at 51°!.)
Sodium 18.9

- 61 -

Dissolved lon-Istallic ions

Bicarbonate none

Carbonate 18 p.p.n. (solubility at 51°12)
mlorids 68.9 p.p.m.

Hydroxide 6 p.p.m. (calculated from excess CaO)
Culphate 69.6 in raw 4 8.3 p.p.m. - 73.9 p.p.m.
Dissolved Oxygen . 6.8 p.p.m.

Free Carbon dioxide none

The 002 required for recarbaiaticn will be the some
as for the lime soda ash treatment.

The hardness of the water from the recarbonating
basins will be:
58 Ca x 2.897 = 135 p.p.m.
13.5 Hg x 8.115 = ___55_._5, p.p.m.
190.5 p.p.m. as Ca003

To reduce this hardness to 85 p.p.m., 105.5 p.p.m.
must be removed by the seelite treatment. 2. 87 pounds of
salt will be required per pound of hardness removed. 105.5
x 2.87 = 303 pounds of salt. Due to the nature of zeolite
treated water having zero hardness, part of the water must
be filtered thru sand and part thru zeolite beds. The
percentage of water that must go thru zeolite beds is

105.5/190.5 s 55.3 percent.

-62-

The total solids remaining in the water is calculat-

ed as follows:

Ca003 precipitated item b(23.8), g(277.0) 300.8 p.p.mt
ug(cn)2 precipitated item d(77.0) 77.0 '
Tb(CH)3 precipitated item J(l.9) ___;,9, '

Total 379.3 p.p.m.
one added _g5§,g_ '

Total reduction 125.1 p.p.m.

58‘— 28 Ca. = 30 p.p.m. Ca.exmhanged for Us
13.5 - 6 lg I 7.5 p.p.m. lg exchanged for Is
gel. wt. Ca 80
' ' lg 28
' ', Na 86
The additional solids due to exchange of Ca
(86/80 x 30) - 30 - 8.5 p.p.a.
The additional solids due to exchange of Hg
(86/28 x 7.5) - 7.5 = 6.7 p.p.m.
Cross addition due to aeolite 11.2 p.p.m.
let reduction in total solids is 125.1 - 11.2 = 113.9 p.p.m.

833 p.p.m. in raw water - 113.9 removed = 319.1 p.p.m. in
finished water.

The quantity of la remaining in the finished water
will be:

I!
W
.p
0
0"
i
a

58 0a:p 28 ‘= 30 p.p.m. removed x 1.15

13.5 Ig- 6 I 7.5 ' - x 1.39 = 1,5,2 ~
Total 88.7 In
Original water 18,9

67.6 p.p.m. la.

The quantity of Ca.and Hg in the conditioned water
can be determined as follows:
58 Ca x 88.71. = 28 p.p.m. 0a remaining in water
13.5 Mg x 88.7“ - 6 p.p.m. lg. remainingninfwater

The finished water after leaving the sand filter and
zeolite beds will hare the following chemical characteristics:

Total Solids 319.1 p.p.m.

Silica 3-5 '

Dissolved Istallio ions

Calcium 28.0 '
iron .2 '
Isgnesium 6.0 '

Bcdium 67.6 '

Dissolved lon-Ietallic ions

Bicarbonate 50 '
Carbonate none
Chlorides 68.9 '
Bydrcxide none
lulphate ' 73.9 '

-51..

Dissolved Oxygen 6.8 p.p.m.

Tree Carbon dioxide 5.0 '
pH 8.0 '
Alkalinity as 00.003 81 '
Hardness as CaCO3 85 '

- 65 -

TABLE 10

00142131301! or rinisarn WATER

Total Solids

Silica 8102

Dissolved letallic ions
011011- Ca 'H’
Iron Fe """"
hgmmium lg"*
Bodiun ra *

[Dissolved Non-Istallio ions

lmgnmmats 3003'
Outmude 003-
Ohlcride Cl-
HMroxide OH”
Whhlhl lOu”

Dissolved Oxygen

’1'” Carbon dioxide
PH

“minty as CaCO3
We” as CaCO3

Raw
Inter
Before

Treatment

p.p.m.
833
3~5

108.0
1.0
32.1
18.9

383.0
none
68.9

none

69.6

6.8
10.3
706

281
800

- 66 _

Lime

Soda. Ash
lethod of
Treatment

p.p.m.

335.9
3-5

12
.2

13.5
58. 8

50.0
none
68.9
none
73-9
6.8
5.0
8.2
81
55

Zeolite
Method of
Treatment

p.p.m.

868.3
3.5

22.9
.2
6.8
168.6

383.0
none
68.9

none

69.6

6.8

10.3

7.6
231
65

Lime
Zeolite
Method of
Treatment

p.p.m.
319.1
35

28
.2
6.0
67.6

50.0

none
5m
none
73-9
5.3
5.0
3.0
In
35

Culinary of chemical requirements for the three meth-

ods of treating the water to a hardness of 85 p.p.m.

TABLE 11

021111011. nroursrururs in 2.2.1.

Chemical

Alus

Lime (CaO)
Bods Ash

81 t

Coke

Liquid chlorine

Line and
Soda Ash
Treatment
10
300

573

5.6

TABLE 12

Zeolite
Treatment

Lime mid
Bods. Ash
Treatment

10
300

_ .
-
D

303
5.6

osmium. ucmamsrs Ill POUNDS m union GALLOIS

memical

Alias

Limo (Can)

Coda Ash

Cit

Coke

Liquid Chlorine

Lime mid
Bods Ash
Treatment
lb.
83.8
2502
673

86.7

-67..

Zeolits
Treatment
lb.

7539

2.58

Lime and
Bode. Ash
Treatment
lb.
33 . 8

2502

2527
86.7

Chapter V

m nmwsi'cni. sonocrnrrrr AND minim. smiiisirr or
acorns

There are many parts of a water conditioning plant
that are dependent upOn experimental data for their de-
termination. A few of the factors that must be determin-
ed by tests and models are:

1. rlhat is the proper length of time for mixing?

2. what is the optimum velocity of mixing?

3. Ihat is the proper period of retention in the

clarifiers?
8. lhat is the optimum velocity in the clarifiers?

The hydraulic action of the water may be determin-
ed from scale models. The data from model tests may be

used with confidence if certain fundamental relations are

considered.

For dimensional homogeneity (assuming that the ratio
of the prototype and the model is n) the following relap
tions exist:

1. The volume of the prototype will be n3 times

. that of the model.

2. The length will be n times the length of the model.

3. 1f the retention time is the same for both the

prototype and model, then the velocity in the

- 68 -

prototype will be n timesthat in the model.

8. 1f the velocity is made the same in the model
and prototype, then.the retention time is n
times greater in the prototype.

for dynamical similarity the following relations
exist:
1. The velocity in the prototype must be the square
root of n times the velocity in the model.
I. The retention period in the prototype is also
the square root of n times that in the model.

As an example, assume that it is desired to check
operation of a clarifying basin 30 feet wide, 100 feet
long and 16 feet deep. If tectonic ratio; (n) is 10, the
model will be 3 feet wide, 10 feet long and.l.6 feet deep.
Tor a 2 hour retention period in the prototype, that used
in the model should be 2 e 105*:= .633 hours or, 38 minutes.
The average velocity thru the prototype will be .833 feet
per minute and should be .833 divided by 101} - .268 feet
Der minute in the model.

Two factors which are troublesome and sometimes fatal
to test models are surface tension and viscosity. These
troubles do not appear unless a- large scale ratio is used.
ratio. up to 20 to 1 will give satisfactory results. chels
'1th ratios above 20 should be checked by using tube floats.

.. 69 -

1f surface tension is excessive, the tubes will not move
with the water but remain stationary as if frozen in -ice.
Surface tension is usually disproportionately large in

the model but will hare little effect on the test results

unless excessive.

- 7o -

Chapter VI

CALCULATIONS FOR THE DESIGN OF A LIMIPSODA ASH TREATMENT
PLANT

The sire of the mixing tank necessary is determined
from experimental data. The time necessary for mixing will
vary from 15 to 60 minutes. Assume that tests made on a
small model indicates that the optimum of best mixing was
20 minutes. To insure adequate mixing, 30 minutes will be
used as a basis of design. The initial conditioning OdplP
city of the plant will be 15 million gallons per day; the
plant being designed so the capacity can be expanded to an
ultimate of 30 million gallons per day. The arrangement
of the various steps in the conditioning process may be
such that it would be desirable to install all the mixing
tanks with the initial installation. This is the case
with the layout as determined by the ground space available
for this plant. Two mixing tanks should be provided for
the ultimate capacity. Agitators need be placed in only
one at the present time. For a mixing period of 30 minutes
the capacity of the mixing tank for 15.million gallons per
day would be:

_l§,QQQ.OQQ ; 39 = 312,500 gallons which is equivalent
2
u ‘ 6° to 81,800 cubic feet.

The depth of water in the mixing tank will be approximately
the same as that in the clarifiers. This factor is a.matter

of Judgment and good practice indicates a depth of 15 feet.

- 71 -

The arc of the airing tank will then be 81,800 4 15 a 2,500
square feet. The length of the mixing tank can be approxi-
mately the same as the clarifier tanks to simplify construc-
tion. Assuming a length of 100 feet, the width of the mix-
ing tank for 15 million gallons per day would be 28 feet.
The future mixing tank would be of the same dimensions.

The cross section of the mixing tank should be such
that the velocity of water does not exceed 1.5 feet per
second. The velocity of water in the mixing tank as de-
termined would be:

W13... : 23.1 cu.ft. per sec.
30 x 60

velocity 3 $153 -_- 5.5 feet per second.
x

The size of the clarifying tanks must also be deter-
mined.frcm.experimental data. The time necessary for clari-
fying will vary from one to six hours. Assume that tests
made on the water to be conditioned indicate that the re—
tenticn should be approthately two and one half hours.

The total capacity of the clarifying tanks will then be:
0 2 r = 1,560,000 gallons which
hr. is equivalent to 208,000

cubic feet.

Good design practice indicates a depth of water in
the clarifying tank from 12 to 20 feet, depending upon
ground space available, type of water and kind of coagulant

-72..

used. Assume a depth of 15 feet. Due to the desirability
of installating continuous sludge removal equipment; the
last three feet of tank depth should be considered as in-
effective as clarifying capacity. The equipment installed
in the bottom of the tank would be continuously moving aid
this will render this part of the tank ineffective for sub-
sidence. The effective depth is then 12 feet. The total
area of the clarifying tanks would then be 208,000 cubic
feet for 2.5 hours retention 4 12 feet - 17,350 square feet.
The length of a rectangular tank should not be less than 80
feet; water requiring this leish of travel for the floc to
entirely settle. To provide a factor of safety, the length
of the clarifying tanks will be determined at 100 feet.

The total width of the tanks will then be 173.5 feet. Good
practice dictates that the ratio of length of tank to width
should be approximately 3. To comply with this factor the
width of the tanks should be 30 feet and the number of tanks
would then necessarily be 6 to provide for the necessary

total width.

The area of clarifier tanks should be such that the
settling rate is approximately 900 gallons per square foot
per day. The size of tanks as determined will have a set-

tling rate of_%5‘QQQJQQQ__: 833 gallons per sq.ft. per day.
x 30 x 100

-73..

~ The width of the distributing conduit to the clari-
fiers should be calculated so that the floc formed in the
mixing chamber will not be destroyed by high velocity nor
will it settle out in the conduit due to too low a velo-
city. The velocity necessary to properly transport this
floc should be not less than 0.2 feet per second and not
over 1.5 feet per second. Assuming a value of 0.75 feet

per second as a basis of calculation the width as determinp

ed for the ultimate capacity will be:

IQE%QQ,QOQ g.p,q,
(m x 60W 7. x l ft.depth x .75 ft.eec.velccd ty 7-

3.85 feet wide.

 

 

To maintain a.high degree of settling efficiency, the
exit velocity should be as low as practical. lxit velocity
should not exceed 0.8 feet per second. The clarifier tanks
as calculated will each have a horizontal weir of 30 feet
width. The height of water over the weir and the exit vel-
ccity is calculated as follows:

a = 3.33 bug
where Q = cu.ft. per sec.

H 3 head in feet

b 8 width of weir in feet
Q per tank will be 23.1 cu.ft. per sec./6 = 3.85 cu.ft.per see.

b = 30 feet.

-7u-

2

_ 2 .2. 3
3.. $3.? ‘3'. i .;§8§ 30;} = .0386 3 .11# ft. = 1.37 indies.

V g Q 4 A g 3.85 + .11“ x 30 .-. 1.13 ft. per sec.

Thisrout1et design would result in a high velocity
when the treatment plant is operating at rated capacity.
The difficulty can readily be overcome by the installation
of auxiliary weirs. An additional 80 feet of weir can be
installed across the width of the tank, six feet from the
end and connecting same to the end weir by two troughs.
The height of water flowing over the weir and the exit
velocity would then be: 2

2 .2. 3'
s : $379763: 2%? z .0105 . .one ft...576 inches.

V .-..- Q 4 A a 3.85 4 .0“ x 110 . 0.73 ft. per second.

The capacity of the recarbonation basin should be
sufficient for a ten.minute retention period. The capacity

can be calculated as follows:

lfigggg‘ggfl_§_1§_wa 156,500 gallons which is equivalent to
x

21,000 cubic feet.

The length of the recarbonating basin can be the same
as the total width of the clarifying basin; the width of

the recarbonating basin would then be:

2 : 7e} {'0‘
185 x 1% depth

-75-

The calculation of the filters is the next logical
step in design. The standard filtration rate is 2 gallons
per minute per square foot of filter area. The area of

the filters will be:

.ISlggngQg_. : 5,200 square feet.
1, x

The filter structure for plants of this size is de-
signed with a central Operating bay, filters being built
on both sides. Operating tables and instruments are mount—
ed opposite the filter they serve. The qpase below the
operating floor is used for pipe gallery and operating
valves for the filters.

The.maxinum desirable length of filter bed is 30
feet. Lengths over this figure may have trouble with back-
washing due to difficulty in the distribution of the back-
wash water. lith filters on both sides of the operating
floor and the length determined, the total width of each
set of filters can be calculated:

Wow. feet = 86.7 feet.
x 30

The smaller number of filter units installed the less as
mount of piping, valves and fittings will be required.

The larger the filter units, the higher the rate of flow
of water necessary for backwashing. Good practice dio-
tates filter units 30 feet wide. Using this factor, three
filters will be necessary in each side of the cperathng

-76..

floor, a total of six for the 15,000,000 gallons per day
plant. lach filter will have a rating of 2,500,000 mil-
lion gallons per day. This is the same rating as each
clarifier unit. These sises are adaptable for future ex-
tensions tc the plant. The extensions can be made in

5,000,000 gallon step or multiple thereof.

To limit the rate of flow of backwash water, each
filter is designed in two equal sections; one section be-
ing washed at a time. During backwashing the complete
filter unit is out of service. The time required for
backwashing a filter unit is doubled by the arrangement
but the advantage of reduced backwash rate more than com-
pensates for the disadvantage. The dimensions of each
section will be 15 feet wide with a length of 30 feet,
the area is #50 square feet.

Backwash rates are expressed in terms of inches
vertical rise per minute or in terms of gallons per square
foot per minute. “Present day practice is high backwash
rate. A rate of an inches vertical rise will be used in
the design of the backwash requirements. This is equivap
lent to 15 gallons per square foot per minute. The rate
of flow will be #50 x 15 : 6,750 gallons per minute. The
time necessary to backwash each section will be from h to

8 minutes, depending upon the efficiency of mixing, clari-

-77..

floor, a total of six for the 15,000,000 gallons per day
plant. lash filter will have a rating of 2,500,000 mil-
lion gallons per day. This is the same rating as each
clarifier unit. These sises are adaptable for future ex-
tensions to the plant. The extensions can.be made in

5,000,000 gallon step or multiple thereof.

To limit the rate of flow of backwash water, each
filter is designed in two equal sections; one section be-
ing washed at a time. During backwashing the complete
filter unit is out of service. The time required for
backwashing a filter unit is doubled by the arrangement
but the advantage of reduced backwash rate more than com-
pensates for the disadvantage. The dimensions of each
section will be 15 feet wide with a length of 30 feet,
the area is 450 square feet.

Backwash rates are expressed in terms of inches
vertical rise per minute or in terms of gallons per square
foot per minute. “Present day practice is high backwash
rate. A rate of 2& inches vertical rise will be used in
the design of the backwash requirements. This is equivap
lent to 15 gallons per square foot per minute. The rate
of flow will be #50 x 15 = 6,750 gallons per minute. The
time necessary to backwash each section will be free k to
8 minutes, depending upon the efficiency of mixing, clari-

-v

-77..

fication and recarbonaticn. Five minutes would be good
operation. The total quantity of water per section would
be 6,750 x 5 3 33,750 gallons and per filter unit 33,750 x
2 - 67,500 gallons.

From Chart 10 , with the size of filter sand from
.R5 to .55 mm. diameter, the rate of increase of loss of
head in feet per hour is 0.3 feet. Loss thru the filter
when clean will be 2 feet and the filter may be operated
until the loss is 10 feet. The number of hours between
backwashing when operating the filter at capacity is
(10 - 2) e .3 g 26.6 hours. The quantity of water pass-
ing thru will be 2,500,000 x 26.6/2% 8 2,780,000 gallons.
The percentage of water required for backwash will be
67,500/2,780,000 - 2.83 percent.

There are two methods of providing the backwash
water. One method would be the installation of an over-
head tank of sufficient capacity for backwashing twc fil-
ters. This tank could be filled by a small centrifugal
pump operating constantly. The size of this pump would
MW a 951i g.p.m. To provide a fac-
tor of safetg the also of pump should be on the order of
300 g.p.m. The other method would be the installation of
a large centrifugal pump sufficient to furnish the back-
wash water as required. The capacity of this pump would

-73..

he 6,750 g.p.m. It will be noted that this rate is 65 per-
cent of the capacity of the treatment plant. This plan is
the most economical in first cost, the operating cost of
the two plans are the same. Unless there is sufficient
overhead storage or clear well reservoirs already provided
this last plan is not practical due to the high rate of
flow required. It will be assumed that sufficient reser-
voir capacity is already installed so advantage may be
taken of the more economical installation. The pressure

of the backwash water must be such that 1% feet head is main-
tained at the filter manifold during backwashing.

The depth of the filter bed necessary for a filtra-
tion rate of 2 gallons per minute per square foot will be
#2 inches. This bed will be made up 15' of gravel graded
from 2' to 1/16' and 27' of filter sand. Before raking the
final determination of the depth of filter bed and the sire
of the filter sand, experiments should be made and various
sizes of sand and depths of beds toeietermine the optimum
of size and depth. The filtration rate can be increased
with larger sand but the quality of water may not be sat-
isfactory. The higher the filtration rate, the lower the
loss of head at which flocculated.matter will pass the bed.
Prom Chart 10 the maximum aims of sand with average floc-
culation which at a loss of head thru the filters ofilo ft.

- 79 -

will pass flocculated matter is .60 mm. in diameter. It

is well to provide a factor of safety so the size of sand
for this plant will be determined at .50 mm. in diameter.
The underdrainage of the filters may be of many designs.
The simpliest and most satisfactory for all purposes cone
slate of a central manifold from.shich laterals are tapped
on 6' centers. Strainer heads are placed on top of the
laterals on 6' centers. The size of the orifices in the
strainer heads should be within the limits of .07“ to .123
square inch per head, which is equivalent to .3 tc.5
square inches per square foot of filter surface. .h square
inches will be used in this design. The outlet of the fil-
ter should be 125 percent of the total area of the filter
heads. The sise of outlet will be #50 x h x 1.25 a 225
sq.in. The area of an 18' o.d. pipe is 232 sq.in. The
else of the laterals are determined in a.similar manner.
Each lateral will drain from (15 t 2) x .5 = 3.75 square
feet of filter. 3.75 x I: x 1.25 . 1.375 sq. in. The are
of a 2' pipe is 3.1 sq.in.

The wash water troughs (or gutters) are placed 30'
above the sand bed. The normal height of water while
filtering will be 6" above the wash water troughs. The
maximum allowable spacing of the wash water troughs is 7
.feet, so that the travel of wash water will not be over

3.5‘feet to any trough. The width of the troughs will be

- go -

lZflinches. The length of the filter is 30 feet so the pro-
per spacing of the troughs will be 7.5 feet on centers, the
distance between troughs will be 7.5 - 1.0 a 6.5 feet. The
center of the and troughs will be placed 3.75 feet from the
ends of the filters. The top edges of the westwater troughs
must be placed level so each trough will carry off the same
amount of water. The height of water flowing over the edge

of the trough can be determined as follows:

Design of lash later Trough for Rapid Sand Filters

it is important that this part of the filter be given
considerable thought. If these troughs are too small, they
will be inadequate to properly carry away the wash water
and if they are too large, they will interfere with the dis-
tribution of the wash water. The discharge capacity of any
trough can be calculated from:

Q = 2.38 AV
where Q 3 Total flow in cu.ft. per sec.

A.= Total available cross-sectional area

b=- The width between parallel sides.

Bach trough in the sand filters of the lime soda ash
plant will drain an area of 7.5 feet wide by 15 feet long;
112.5 square feet. The quantity of water will be 112.5 x
15 ga1./min./sq.ft. - 1687.5 g.p.m., which is equivalent

tce3.76 cubic feet per second.

-81...

- Assuae a trough with a width between the parallel

sides of 12', a length of the parallel side of 12' and
the bottom semi-circular with a radius of 6".

1 un equal 12 x 112 t 62 1112 . 1.39

b = 1.0
Mb . 1.39

 

The quantity of water which this trough will dis-

charge will be:
Q a 2.38 x 1.39 r (1.39)% = 3.9 cu.ft.per sec. 3 1750 g.p.m.

This design will provide for a slight excess in car

paoity. This excess amounts to:
1 159 - J 6§1,5 : 3.7 percent.
1. 7-5

Rate of flow for each filter section 6,750 g.p.m. =
15.05 cu.ft. per second.

The total length of weir will be 15 feet width of
filters 3 ll- groughs x 2 edge; a 120 fest. Q 8 3.33 M! g
a: "’g 15.95 ’=.o 6 =.11 ft.=1. 10h .
3+3.3 133 33.33 x 12033 37 3 3 35 n °°

The height of the wash water troughs above the strain-
er heads in the manifold and laterals will be:
15' Gravel .
27' filter sand
__3_9_: Above sand

72' Total
- 32 -

The gravel below the filter sand serves two defin-
ite purposes; viz. a support for the sand and a.media for
distributing the wash water uniformly through the filter

316! .

The sire of equipment necessary for recarbonation
should next be determined. The quantity of 002 gas nec-
essary was determined as 16.8 pounds per million pounds
of water. This is equivalent to 130 pounds per million
gallons. The quantity of carbon dioxide gas necessary
per hour when operating the plant at the ultimate capacity
of 30 million gallons per day 3 30,000,000/2M x 140 =
175 pounds per hour. One pound of coke will produce three
pounds of 002. The quantity of coke required per hour
will be 175/} = 58.3 pounds. A factor of safety should
be provided if equipment is operated under the most econ-
cmical point, so 75 pounds will be used in the sire de-
termination. The sire of grate necessary to burn this
coke will be 75/37.5 lb. coke per sqmne feet of grate =

2 square feet of grate surface required.

Assuming that the gas leaving the scrubber contains
”12$.002 and the weight of a cubic foot of gas to be approx.
iaately .08 1b., the total volume of gas to be handled by
the compressor will be 375 cubic feet per minute. Due to
the submergence cf the diffusing orifice in the recarbon-

ating basin of 10 feet, the compressed gas pressure will

- g3 -

be thisfihead.plus the head necessary to transmit the gas
.frcm the producer to the reoarbonating basin. The 002

piping laterals should be 3/lt inches in diameter, speed
24 inches on centers and have 1/16 inch holes on the un-

derside spaced 6 inches on centers.

The capacity of the chemical storage bins and pro-
portioning equipment will next be determined. The aver-
age daily output of treated water will be 9,000,000 gal-
lons with the original installation. The average daily
output of the ultimate plant will be 18,000,000 gallons.
The quantity of chemicals required per million gallons
as determined on page 67 is:

Alum 83.1!» pounds
Lime (09.0) .2502 '
Soda Ash 673 I

The quantity of chemicals used per average day of
9,000,000 gallons will be:

nu- 750.6 pounds = 0.375 tons
Lime (cao) 22,513 ' = 11.259 I
30d! “h 6,057 ' . 2 3.029 s

Assuming that it will be desirable and economically
justifiable to have storage for a 90 day supply of chemi~
cals, the storage should be designed for the following

quantities:

A1“- -375 x 90 = 33.75 tone
Lime (an) 11.259 x 90 = 1013.31 tons
soda Ash 3.029 x 90 . 272.61

The chemicals can be stored either in concrete bins
built integral with the structure or in steel bins. Due
to the hasard that exists when storaging quick lime it is
deemed advisable to store all chemicals in steel bins.

The storage would occupy the same area as the mixing tanks.
The maximum reasonable diameter that would fit into this
space is 13 feet. If the bins are made 18 feet high, the
total capacity of each bin will be 2,H00 cubic feet. The
volume of storage required for each chemical is:

11:- W = 1,925 cubic feet

Mu W = 33.800 cubic feet
soda Ash W = 9,100 cubic feet
The number of bins required for each chemical will be:
nil : e8 “0 bin. .
"$45, 05‘
Lime : 15.1 Fourteen bins
1% 0L

Ioda Ash ..gfi. : 3.8 Four bins
8

1t should.be noted here that this chemical storage is
calculated on the basis of 90 days for the present plant.
lhen the capacity of the plant is ultimately doubled, the

- 35 -

storage capacity will be for “5 days which is ample.

The chemicals will be received in box cars in bulk.
They will be unloaded by pneumatic conveyor system, the
motive power being installed with the storage bins. The
capacity of the pneumatic conveyor will be 25 tons per

hour. This will permit a carload to be unloaded in an

hour.

The chemical feeders or proportioners should be
installed in duplicate, each feeder being capable of sup-
plying sufficient chemical when the plant is Operated at
the full capacity of 15,000,000 gallons per day. Ihen
the cmacity of the plant is doubled an additional feeder
would be installed sothat two feeders would be required
to supply the chemical demand, one feeder would then be

in reserve. The capacity of each feeder would be:

Alum feeders 50 pounds per hour
Lime feeders 1,000 pounds per hour
Soda Ash feeders 300 pounds per hour.

The sizes of miscellaneous equipment can readily be
determined from manufacturer's catalogs. Miscellaneous
equipment includes:

1. Continuous sludge removal equipment,

. Iixing equipment,
Chemical proportioners,

43'le

filter sand and gravel,

-36..

5. Rate of flow controllers,
. Hydraulically operated valves,

Pneumatic chemical conveyor,

Gages and instruments,

\OGNO‘

Back wash pump.

The cost of constructing the initial 15,000,000
gallons per day capacity plant is estimated as follows:
Building

Mixing tanks, chemical proportioning, offices,
laboratory and chemical storage

336,000 cu. ft. at $.20 s 67,200
Clarifying basins

578,000 cu. ft. at 8.18 104,100
filter building

238,000 cu. It. at 0.19 35,200 $216,500
fixing equipment 0,000
Chemical fbeding equipment 8,000
Clarifier equipment (sludge removal) 1h,000
filters, sand, gravel and underdrains 18,000
Rate of flow controllers 10,000
Gages and Meters 3,000
Control Tables 1,000
Chamical Conveyors (Pneumatic) 8,000
002, Stoker, Boiler, Scrubber and Compressor 3,000
Backwash Pumps 5,000

-87..

llectrical fork 8 3 ,000

Plumbing ' 1,000
Piping and Valves in Building 211,000
Piping outside Building £5000
Miscellaneous 10 ,000
lngineering and Supervision 11.599

Total ”50,000

The cost of constructing the second 15,000,000 gal-
lens of capacity is estimated as follows:
Building
Clarifying Basins
578,000 cu. ft. at 8.18 810M»,100
filter Building extension

238,000 cu. ft. at s.19 £5,200 011:9,300
Chemical feeding equipment l5000
Clarifier equipment lu,000
filters, Said, Gravel and Underdrains 18,000
Rate of flow Controllers 10,000
Gages and [stern 3,000
Control Tables 1,000 .
llectrical fork 1,000
Plumbing . 1,000
Piping and Valves in building 20,000
Miscellaneous 8,000
Engineering and Supervision ___l_2_,19_o_

Total $212,000

1': the extension is made in three steps of 5,000,000
gallons each, the cost per step would be 252,000/3 - 880,700.
The actual cost would be slightly higher due to spreading
the construction over a longer period of time and this fig-
ure should.be increased to 88h,000.

Summary:
Isthmated cost of initial 15,000,000 capacity $350,000
Estimated cost of second 15,000,000 capacity _g§g,ggg
Total cost of plant $592,000

-39..

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

    
   
  
 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

_ a M“ r, - i._r-_.l_.. _ .--...'._,-.__,-__,4
2% J :, :2»-ng _. _£fii.
. , 1 1 3.1L
.9, T
fl—W“ E) A S ) N i ‘(0 l
m . _ — .m- — — — — |:‘¥—— !
Q E ‘J— i
!
*TEt-L ' g
E i
: l
B A s 1 N s ; E
.9:
.3 29'
E -0 Fm. TIER FxL. Tap. FM. HER
% mu ;
z ? ; .
a :OT 1“ .
“ _"‘l'__
”4' 1 " 3:: l
Zflk
S E
L—___—_ ---_______ 8
L H3313" 7 *4
F ”v “1.1,---“ ‘ “’1
I
i TST e u
fi_‘_ =—-= -——-=-—- = —._=.—_ ...—... ,
i u '
i ' H
g “ rm. TEK FIL Tap. FIL flak
{ u . q I 1" I I
a L j , c; L A K \ P V x N C: B A g l N s. '
_ u [:1 E: ' I 1 .
03 || ' F \ LT E K CONT Rot. FLoom LABORATDKY fi <I II I I N}
_. 7 \9:
K") II :7
(13 1:3 [:3 [:1] . =L1ME-soDA AsH
1 w y 7 .
ll 7 0mm: 7 I t . 7 _ TREATMENT
E? '
II 1:11. TER FM. TEFL Fm. :TEK CONTROL. : PLAN? .
' ‘ i Room SCALE. 1 = 30
O
i 'l : d ‘I I I '(
El: :0 w A L. K w AY
OPERATING FLOOR. “ " ’ q PLATE 1.

 

 

 

 

CLEAR WELL
OVERFLOW

 

  

 

GRADE

  

F iLTE PL House

WATEK L t NE "
k9

'0»

 

  
 
    
   

C. HE M I CAL ITO RAG E
EszQPOfiHCAHNQ

  
 
  

   

 

CLARIFYING BASINS

      
     
  

WATER LXNC 2

‘3

  
  
 

mxxme
TANK.

MIXING
TANK,

   

GRADE \.

  

W

     
 

 
 
  

L 53EC"
.1

.. . v
3‘ 3394 ” (’3

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

   

LONGWUDWAL SECWON

      

‘
-
'

    
 

...——-
--b

  

  

 

 

 

 

 

 

FELONT ELEVATION

LIME- SODA ASH TREATMENT PLANT

ScAL; I": 3:: FT.

PLATE 2.

 

 

 

F1-)

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

i PLPEEfEhE" Y1“...

 

 

 

 

 

 

 

 

 

 

 

 

 

 

FILTER CONTROL (ZOOM FLOOR)

TYPLCAL

 

 

 

 

 

 

 

 

 

 

 

    
 

WATER LmE ?

  

[u

WATER LANE 2

 

 

 

 

 

 

.. H, CLAR\FIED WATER

 

' SAND LKNC \

 

- _'_—

 

 

 

 

 

 

 

 

 

KAV'ELI'ganxE"-

 

WASH WAT: r; “mar

 

 

 

 
 

UN‘DER' (Samba:

 

 

WAT GR To

 

 

 

 

 

 

 

 

 

  
 

  

 

 

:v- cpEA K

 

<———J-——- -

sEcTIo-N A-A

 

 

-
”—'-

  
  

  

 

 

 

 

RATE. 0F FLOW
CONTROLLER

 

 

TYPlCAL ELEVATION

 

 

 

 

 

 

 

 

 

 

 

 

 

 

FILTER PJPlNG
§CAL.E, y4.“lFT_

DLATE 3

 

 

 

.__—_.__~_ ...—.....- -_—_

 

 

LOSS or: HEAD RATE 0: FLOW

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

  

 

 

 

 

 

 

 

  

 

 

GAGE GAGf:
::ETHEY:\ QBVEEK - I - A J -—--*—~- WASH WATER
D PUMP MOTOR
$TART 0 are p

CLOSED O O 0 O

I / / /
OPEN

0 O 3 E,

n

d & F d d

g I» d '3} u)

4 k m J ‘1 d I"

b 3 3 s E g 3

o

‘9 u 3 g 3 2 f,

if d at V “J

a! w n) P . I 4

4 P r 3 W W 3

.J :5 .1 3 <1 4 u]

U u [C u. 3 1 d

PLAN or mum common. BOARD

 

 

 

 

 

 

 

 

 

 

 

 

 

VALVE OPERATING SCHEDULE

POS)TION OF VALVE

NORMAL BAGKWASH RE‘WASH
CLAQIHED WATEK To FILTEJL. OPEN amass-.1: opsH
FILTERED WATER.‘ SOUTH OPEN 0 arc. OPEN
FILTERED WATEQ- NORTH 095M C. orO opsH
RATE OF FLOW CONTROLLER open CLOSE» CLOSED
WA‘STE. WATER. 0.0559 OPEN egos-.51:
WASH WATER- CLD$ED ope-5n; CLOSED
RE. WASH WA‘TEV- cgossv CLoseo OPEN

 

 

PLATE

 

 

 

Chapter VII

automatons roe m DESlGN or A mourn: murmur pun

All water passing thru the zeolite beds will be sof-
tened to zero hardness. it is desired to maintain a hard-
ness of 85‘p.p.n. To obtain this result part of the water
can be by-psssed the zeolite beds. This results in a say-

ing in operation. The amount of water byapassed can be de-

tennined as follows:

WW. : 21.2 percent
p.p.a. original hardness as 0a00

bypass.
Zeolite bede need be provided for only 78.8 percent of the

total capacity of the plant.
15,000,000 1 .788 *- 11,820,000 gallons per day.

The factor that influences the original cost of con-
structicn of a zeolite conditioning plant is the period of
regeneration. the zeolite mineral will cost nearly 50$.o:
the total cost of the plant. if a short period of regener-
ation is taken as the design basis, the beds lust be out of
service a large percentage of the time. Regardless of size
of the bed, the period of regeneration is 30 minutes. if 4
hours is used as the period betteen regeneration, each bed
will be out of service a total of 3 hours during the day,
with a 6 hour period this is reduced to 2 hours and sith an
8 hour period to 1.5 hours. The total capacity of the plant

must be increased the following amounts for varying periods

- 90 -

of regeneration:

Regeneration Total time Percent decrease
Period for regeneration in capacity
h-hours 3 hours 12.5 i
6 hours 2 hohre 8.3 $
8 hours 1.5 hours 6.25 f

The most economical period will be 8 hours between
regeneraticns. Periods longer than this increase the cost

of plant out of proportion to saving in operation.

The quantity of water for which the plant must be
designed will he 11,820,000 1 1.0625 s 12,600,000 gallons.
per day. With an 8 hour period of regeneration, the plant
lust soften between regenerations:

1g,600,000/3 = n,200,000 gallons.

One cubic foot of greensand zeolite will remove 2,000
grains hardness as 0a003. The quantity of zeolite necessary

will be:

0 a 35,000 cubic feet of greensand
' x 1 . zeolite required.
lhen operated as a gravity filter, a bed of seolite should
be operated with a filtration rate of 2 gallons per square

foot per minute. The area of filter bed necessary will be:

W ; “,370 square feet required.
1, x 2

The depth of zeolite bed will be:

45.999. : 8 feet
“.370

_ o1 -

15 inches of graded gravel should be placed above the col-
lecting strainers for a supporting bed for the zeolite.

The arrangement of the filter beds used for the lime
soda ash method of treatment to reduce the rate of flow of
the backwash required, will not be suitable for the zeolite
installation due to the leryh of time necessary to back-
wash, brine and rebackwash, which requires a total of 30
minutes. When using the previous arrangement, the whole
unit is out of service, although one half is backwashed at
a time. For the sand filter the time necessary for back-
washing is only five minutes and this would not affectiihe
total capacity any appreciable anount. The length of time
necessary for regeneration of the aeolite is the controll-
ing factor in the determination of the number of beds. A
total of ten beds would seem desirable, five on each side
of the operating floor. Each bed would have an area of
h,37o/1o : It}? square feet. If the controlling dimension
of each bed was taken as the width, with 15 feet only one
central collecting manifold would be required; the length
would then be l87/15 - 29 feet. The sire and spacing of
the manifold, laterals and strainers would be the sme as
to: the sand filters used in the lime soda ash method of
treatment. The freeboard, 1.0. the distance that the top
of the wash water troughs are above the zeolite can be
calculated the same as for a sand filter. The distance

. .

-92..

is,the backwash rate in inches of vertical rise per minute
plus 6 inches. The rate of backwashing for zeolite is 12
gallons per square foot per minute and the equivalent is

19 inches vertical rise. The freeboard will then be 19
plus 6‘! 25 inches. The normal height of water while sof-
tening will be 6 inches above the wash water troughs.
Opening of the wash water troughs have the same limitations
as sand filters. Two troughs will be required each spaced
so the center line of the trough will be 3 feet 9 inches
from theeside cf the zeolite bed.

The height of the wash water troughs above the strainer heads
in the manifold and laterals will be:
15' Grasel
96' Greensand Zeolite
.35" Above Zeolite (freeboard)
136'l Total - 12 feet, h inches.

The gravel below the seclite serves a twofold purpose,
a support for the zeolite which has a diameter of only .35
am. and for distributing the wash water uniformly throughout
the zeolite bed.

The rate and quantity of backwash water required can
next be determined. The rate is:
29' length x 15' width x 12 gallons/ sq.ft.! min.- 5,220

gallons per minute.
This rate is 50% of the total capacity of the conditioning

-93-

plant. Untreated water will be suitable for backwash
water. Due to the large quantity of water required for
backwashing it will be economy to build a storage reser-
voir for raw water and pump direct from this Itorage thru
the seolite. This water will be highly contaminated with
calcium and magnesium chloride and must be put to waste.
The pump must develops a head of 1% feet at the manifold
of the zeolite bed. The zeolite bed must first be back-
washed.for 5 minutes to loosen the bed and remove the
suspended.matter deposited by the raw water, the bed is
next flooded with the required amount of saturated brine ‘
solution and it is allowed to be in contact with the sec-

lite bed for five minutes, and then rewash (downflow) for

20 minutes.

The salt necessary per regeneration per zeolite bed
is: #,200,000 gallon.plant capacity between regmneration/
10 beds = h20,000 gallon per bed. Each p.p.m. hardness
as 0a003 removed will require 2.87 pounds of salt which
is equivalent to 0.hl pounds of salt per 1,000 grains
hardness.

#205990 3 £99 3 9,4; : “,030 pounds of salt.
1, 00 x 17.1

The solubility of salt at 50°F. is 36 pounds of salt
per 100 pounds of water. The brine solution will be 90
percent saturated so each 100 pounds of water will con-
tain'32.fl pounds of salt. Each pound of salt will require

- 9n.—

100/32.4-= 3.1 pounds of water or .37 gallons.
h,030 pounds salt x .37 = 1,491 gallons per regener-
ation for brining.
The rewash water will be used at the same rate as soften-
ing, 1.0., 2 gallons per minute per square foot. The pur-

pose of the rewash is to remove the excess chlorides.

The total quantity of water required for regenerap

tion Will be:
'For backwash, 5,220 g.p.m. x 5 minutes = 26,100 gallons

l'or brining, _ = 1,500 "
For rewash, “35 sq.ft. x 2 x 20 min. 8 11,009 '
Total h5,000 gallons

in terms of million gallons passing thru the zeolite
beds, 107,000 gallons of water are required for regenerat-
ing purposes; this is 10.7 percent of the water softened.
in terms of million gallons of 85 p.p.m. hardness water,

8.fl3 percent is required for regeneration.

The capacity of raw water storage for backwashing
zeolite should be of sufficient capacity for two succes-
sive regenerations. One regeneration requires 26,100

gallons so the capacity of the reservoir should be 60,000
gallons.

The capacity of the salt storage bins will next is
determined. The quantity of salt required per million

-95..

gallons of 85 p.p.m. hardness water is 7,539 pounds as
calculated on page 59 . salt is native to Michigan and
can be economically trucked if necessary. It will there-
fore not be necessary to provide storage for such a long
.period as for the chemicals in the lime soda.ash method
of treatment. Then the demand on the zeolite plant is
nine million gallons of 85 p.p.m. water per day, 67,850
pounds of salt will be required daily. For a 28 day sup-
ply the sise of storage would be:

6 2 2 31,600 cu.ft.
0 lb. cu.ft.

lith a depth of 10 feet and a width of 20 feet the stor-
age pit will be 31,600/10 x 20 a 158 feet long. The salt
can.be unloaded from box cars direct into the storage a,
long the side track. The salt will be covered by water
and the brine pumped to the zeolite beds as required.

This storage capacity will be sufficient for 2 weeks op-
eration when the size of the conditioning plant is doubled.

The cost of constructing the initial 15,000,000 gal-
lons per day capacity’plant is estimated as follows:

Buildings
zeolite Beds and main operating Building
2115000 cu. ft. at 8.20 t ua,eoo
Salt storage and brine pits '
7h,000 cu. ft. at 8.20 lh,800
Brine pumps, piping and meters 2,u00

- 96 -

_Grasel and underdralns for seolite bed. 8 10,000

Rate of flow controllers 17,000
zeolite mineral luo,ooo
1,628 tone at $86 per ton

Gages and Hetero 6,000
Gontrol tables 2,000
Backwash pump 5,000
- Electrical work 3,000
Plumbing 500
Piping and valves in building 29,000
Piping outside building “,000
liscellaneoue 8,000
lngineering and supervision 15,599
Total 8300 ,000

The cost of constructing the second 15,000,000 gallons
of capacity is estimated as follows:

Building
Extension for seelite beds-
180,000 cu.ft. at 8.20 S 36,000
Grasel and underdrain for zeolite beds 10,000
Rate of flow controllers 17,000
Zeolite mineral ino,ooo
Gages and meters 6,000
Gontrol tables 2,000
Electrical work 1,000
Plumbing 500

-97..

Piping and valves in building 25,000

liscellaneous 6,000
Engineering and supervision 12,599
Total $256,000

If the extension is made in five steps of 3,000,000
gallons each, the cost per step would be 256,000/5 =
051,200. The actual cost would be slightly higher due to
spreading the construction over a longer period of time
and this figure should be increased to .5#,000.

Summary:
Esthsated cost of initial 15,000,000 capacity 0300,000
lstimated cost of second 15,000,000 capacity ,_z§§‘999,
Total $556,000

- 93 -

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

I ' -'
hill- 4“ 979HH_W ,1 1
SI ‘ (2' ' ‘ . ,. ‘ , ”k " r
. ’dh_o-t5____yd.l§ ‘7 45,111,579: ._';1., all“
m, 2; ’i a! ‘71 g‘ f '
_ , .7 5 ~. 1 3 H
A; -~>
V I. 1' L. i T E. BEDS
f :53 23 FT U BE. P
I I
3 i
' .
f t"
; ”f71.-.;1
1 ~.t _
:O* i :
CL? 9‘; P)PE GALLERY
m! N;
i o:
3 Li___
I ""4 _
T d:— 4“:
} 13* a F‘ bcié P
a “
“—55 _

SECTION THRU ZEOLlTE BEDS

GRADE. '

 

 

STORAG E

GALLOHS

WATER

WASH

)OOO

60

 

 

 

 

 

 

 

 

 

FRONT

ELEVATION

 

 

 

3T0 RAG E

 

ELEVATION

z EOLITE WATER TREATMENT

SCALE. Y: 306‘:

 

PLATE 5

 

 

 

Chapter VIII

011.001.1110“ roe m DESIGN or l mu ZEOLITE reruns:
PLANT

This method of treatment involves a combination of
the two previous methods in that lime is used to remove
the temporary (carbonate) hardness and zeolite to remove
the permanent (non-carbonate) hardness. The conditioning
plant will be substantially the same as for treatment with
lime and soda ash except that zeolite beds will be substi-
tuted for some of the sand filter beds. The mixing tanks,
clarifying basins and reoarbonating basins will be the
seas. The water leasing the recarbonating basins will con-
tain 190.5 p.p.m. hardness as 0a003 as compared to the “00
p.p.m. entering the mixing tank. Instead of using soda
ash, seelite can be used to lower the hardness to any lim-
it desirable. The limit of 85 p.p.m. has been.previous1y
determined. All water passing thru seelite beds will be
softened to sero hardness. To obtain a residual hardness
of 85 p.p.m. some of the water from the recarbcnating bas-
ins must be filtered thru sand filters. The proportion of
water that must go thru seelite beds can be determined as

follows:

M r 55.3 percent.
190.5

The remainder, hh.7 percent, must be passed thru.sand filters.

—- The filtration rates for zeolite and sand are the
same. The layout of the filter structure is subh that the
total filter area is divided with one half of each side of
the operating floor. The proportions of filtered to aeo-
lite treated water is close enough to 50-50 that one side
of the filter structure can be used for zeolite beds and
the other half for sand filters. The filtration rate for

the sand filters will MW .-.- 1.725
1, x 3 x 30 x 3

gallons per square foot per minute.

The rate of backwashing will be the same as for the
lime soda ash filters, vis. 6,750 g.p.mt Total quantity
of water per filter will be 6,750 x 5 x 2 = 67,500 gallons.
The same percentage of water will be required for back-

sashing, 2.u3 percent of the water passing thru filters.

The quantity of water that must pass thru.the seelite
units will be 15,000,000 x .553 8 8,300,000 gallons per day.

The filtration rate will be___m§_.6399,99_9_‘____ g 2.13
1, x 30 x 30 x 3

gallons per square foot per minute.

Assuming the same period of regeneration as in the
cal culaticn for seolite treatment (8 hours) the quantity

of zeolite necessary will be:

. 0° .00 1 a s - .062 ..ste 0 ts t 96 e r;:-n; .
3 regenerations per day x 2,800 gr. per cu. ft.seolite

1 a 11,700 cubic feet of green—

x 17.1 .p.m. to g.p.s.
sand zeolite required.

- 100 -

For a symetrical design of filter structure, the same
area for the zeolite beds will be assumed as for the sand
filters and the filtration rate will be calculated instead
of assuming a filtration rate and calculating the area of
the zeolite bed. The filtration rate will be:

9,39%,992 I 1,9925 3 2.27 gallon per square ft. per
1, x ,700 sq.ft.
minute.
This is not excessive and represents good operation. The

depth of the zeolite bed will be:

f e : n.33 feet 3 52 inches deep.
2,700 square feet

The sand filters should be arranged the same as for
the lime soda ash method of treatment. They will consist
of three filters, of two sections each. Each section will
be 15 x 30 feet in area. Only one rate of flow controller
need be installed per filter and by dividing the filter in
two sections the rate at which wash water is required will
be halved. Due to the length of time necessary for regen-
eration, this arrangement is not practicable for the sec-
lite beds. By installing six zeolite beds; each 15,: 30
feet in area, extensions to the filter building can be
made by installing one sand filter 30 x 30 and two seolite
filters 15 x 30 feet. Extensions could then be made to
the treatment plant in 5,000,000 gallon steps.

The same centrifugal pump that is used for‘backwasb-

- 101 -

ing theflsand filters can be used for backwashing the zeo-
lites. The rate of flow necessary for backwashing the
seelite beds is 30 x 15 x 12 g.p.m. per square feet =
5,u00 g.p.m. The rate for the sand filters is 6,750 g.p.m.
The pump discharge must be throttled to the 5,uoo g.p.m.
rate when used for backwashing the zeolites.

The height of the wash water troughs above the
strainer heads in the manifold and laterals will be:
15' Gravel
52' Zeolite Bed
_2_5" Freeboard
92' Total = 8 feet, 8 inches.

The quantity of water passing thru each zeolite bed

between regenerations will be:

8,192,999 3 1,9625 3 H90,000 gallons per bed.
3 x zeolite beds

Each p.p.m. hardness as 0a003 removed will require
2.87 pounds of salt which is equivalent to 0.Ml pound of
salt per 1,000 grains removed.
W = 2,240 pounds salt.

1,000 x 17.1

To obtain a 90% saturated solution of brine 0.3?
gallons of water are required per pound of salt.
2,2“0 pounds salt 1 0.37 3 838 gallons per regeneration
for brining.

- 102 -

_ The total quantity of water required per regenerar
tion will be:
For backwash, 5,h00 g.p.m. x 5 minutes 3 27,000 gallons

For brining : 350 s
For rewash, l$50 sq.ft. 1 2 x 20 minutes = M '
Total 45,850 gallons

In terms of million gallons passing thru.the zeolite
beds, 93,500 gallons of water are required for regenerating
purposes; this is 9.35 percent of the water softened to more

by the aeolite.

The capacity of the slum and lime storage bins will
be the same as for the lime soda ash method of treatment.
Ialt may be stored in the same capacity bins as for the
lune; 2,n00 cubic feet each. For a 28 day supply of salt
there will be required:

2,32% 1b, 151; fier milligg gal, ; 3 g 28 day; . 4.h3, 5 bins.
, cu.ft. x 0 lb. per cu. ft.

The same pneumatic conveyor equipment that unloads the lime
and alum can be adapted to unload the salt.

The chemical feeders for soda ash will be omitted. A
concrete tank 6.5 feet x 30 feet can be installed at one
end of the aeolite beds for making the brine. A‘brine pump
should be installed.near this tank and brine piped to all
the zeolite beds.

- 103 -

The siae and number of chemical feeders or propor-
tioners should be the same as for the lime soda ash method.
The capacity of the feeders are:

Two Alum feeders, 50 pounds per hour eadh.

Two Lime feeders, 1,000 pounds per hour each.

The cost of constructing the initial 15,000,000
gallons per day capacity plant is estimated as follows:
Building
Hiring tanks, chemical proportioners, offices,
laboratory and chemical storage

336,000 cu.ft. at 0.20 3 67,200
Clarifying basins
578,000 cu.ft. at 8.18 10H,100
Filter and Zeolite building
233,000 cu.ft. at $.19 H5,200 $216,500
Mixing equipment “.000
‘ Chemical feeding equipment 6,500
Olarifier equipment (sludge removal) 1h,000
Filters, sand, gravel and underdrains 9,000
Brine pump and piping 1,000
Gravel and underdrain for zeolite beds 5,000
lbolite mineral
5H5 tone at 886 per ton “6,800
Rate of flow controllers ߴ,000
_0ages and meters “,500

— lons-

Control tables 3 1,500

Chemical conveyors, pneumatic 8,000
002, stoker, boiler, scrubber and compressor ' 3,000
Backwash pump 5,000
Electrical work 3,000
Plumbing 1,000
Piping and valves in building 26,000
Piping outside building “,000
Miscellaneous 11,200
Engineering and supervision __;34QQQ,

Total 3&03,000

The cost of constructing the second 15,000,000 gal-
lons of capacity is esthmated as follows:

Building
Clarifying basins
578,000 cu. ft. at 8.18 $10M,100
Filter and aeolite building
238,000 cu. ft. at 8.19 l$5,200 “#9500
Chemical feeding equipment ' 3,000
Clarifying equipment (sludge removal) 1n,000
Filters, sand, gravel and underdrains 9,000
Gravel and underdrains for zeolite beds 5,000
Zeolite mineral h6,goo
Rate of flow controllers 1h,000
Gages and meters “,500

-105-

Control tables 3 1.500

Electrical work 1,000
Plumbing . 1,000
Piping and valves in building 22,000
Eisoellaneous 13,900
Engineering and supervision 15,999

Total , $300,000

if the extension is made in three steps of 5,000,000
gallon each, the cost per step would be 300,000/3 8 $100,000.
The actual cost would be slightly higher due to spreading
the construction over a longer period of time and this fig—
ure should be increased to 810h,000.

Summary:
Estimated cost of initial 15,000,000 capacity 8H03,000

Estimated cost of second 15,000 ,000 capacity 100,999,
Total cost $703,000

- 106 -

Chapter 1x

.. 0010131301! or Iuvrsmcsr um cum Inc cosrs

mprgcigt 193
The equipment and structures of each of the three

methods of conditioning water will have different depre-
ciation rates. The following tabulations indicate the

probable life and depreciation rate of the component parts.

Lime and Coda Ash Method of Treatment - Initial Installation
Assumed Deprecia- Annual

, A Life tion Deprecia-

Item Rate ticm
Buildings 6215.500 50 2 P 0 “.330
Equipment 70,000 25 ll» $ 2,800
Filter sand 8,000 12% 8 $ 6M
Piping and valves 28,000 25 it $ 1,120
lisc. , Engr. and Cup. 31,599, 25 J 1. M

Total #350,000 2.85 7. 0 9,990

Second Installation

Buildings $115,300 50 2 i» 3 2,986
Equipment H.000 25 It at 1,760
Filter sand ' . 8,000 129 8 $ 6110
Piping and valves 20,000 25 n.9, 800
lliso., Engr. and Cup. M 25 Jj £9

Total 321:2,000 2.90 1. a 7,011:

Annual depreciation charge per unit extension of 5 ,000,000
gallons: 381$,000 at 2.90% a $2,186.

-107-

Zeolite Method of Treatment
Initial Installation

Deprecia- Annual

Item ‘33:“ 333 ”$33“.
Buildings 8 57.600 50 2 1. 6 1,152
Equipment 345,900 25 It $ 1,836
Zeolite Hineral 1140,000 129 8 $ 11,200
Piping and valves 33,000 25 4 $ 1,320
liec., Engr. and cup. __2_3_,_509, 25 __L$ 959

Total $300,000 5.50 at $16,018.

Second Installation

suudings 8 36,000 50 2 i t 720
Equipment 36,500 25 it 1. 13160
Zeolite lineral $0,000 121} 8 $ 11,200
Piping and Valves 25,000 25 h 1» 1,000
111-0.. her. and Sup. M 25 ..Lfiv .__1&Q

Total 3256, 000 5.90 ‘5 015,120

Annual depreciation charge per unit extension of 3,000,000 gal-
lons: 850,000 at 5.90% = 03,186.

— 108-

Lime and Zeolite lethod of Treatment
Initial Installation

Deprecia- Annual

1'... ‘2???“ £122 “233’”
Buildings $216,500 50 2 i 0 9,330
Equipment 75,500 25 u at 3,020
Filter sand £1,000 12} a at 320
Zeolite lineral 46,800 121} 8 1. 3,710:
Piping and Valves 30,000 25 ll» $ 1,200
Ilse. , Engr. and Sup. M 25 J1 ___1...§.Q§.

Total $03,000 , 3.112 5 813,822

Second Installation

Buildings 01119500 50 2 1. 0 2,936
Equipment 119,000 25 I: 7. 1 ,960
Filter sand l1.,000 12% 8 $ 320
xcciits Mineral 166,800 125 a 71. 3,7111;
Piping and Valves 22,000 25 ll» ‘5 880
liec. , Engr. and Cup. M 25 Jj 49159

Total $300,000 3.63 at 1311,0116

Annual depreciation per unit extension of 5,000,000 gallons:
0109.000 at 3.6% . 03,827.

- 109..

gapita; gharge
The charge on the fixed capital invested in condi-

tioning plant will be uniform for all methods; “5 percent.

ELM

The unit costs of chemicals, water for backwashing

and labor will be assumed as follows:

Alum .25 per ton, f.o.b. plant
Lime (00.0) 811 per ton, f.o.b. plant
Bods Ash ‘33 Per ton

Belt 8 7 per ton

Liquid Chlorine 8 8 per cwt.

Coke ‘10 per ton

Electric Power 1.25 cents per kwbhr.

Cost of untreated water will be $12 per million gal—

lons.

Labor Cost, . Chemist $2,n00 per year
Operators $1,600 per year
Labor 50 cents per hour.

Utilisation by customers, 80% of pumpage to distribup

tion system.

3222.1211
The additional pumping head due to friction losses

thru.the various process in treatment will be as follows:

Lime soda ash plant, 8 feet for all water

- 110 -

zeolite plant, 9 feet for 78.8% of water
no loss on 21.2%. Weighted
loss on all water 7.1 feet.

Lime zeolite plant, 8 feet for all water.

Assuming that the work done on the untreated water
was a lift of 150 feet, which cost 812 per million gallons,
the cost per foot would be 312/150 - $0.08 per million gal-

lons.

MW

The quantity of water required for backwashing in
the lime soda ash method of treatment was as determined
on page 78 , 2.03 percent of the softened water. The sludge
from the clarifier will contain 80 percent moisture. Each
million gallons of water softened will produce #30.3 p.p.m. x
8.3h'= 3,590 pounds of sludge (calculated dry). hoisture
contained in the sludge will increase the actual weight of
the sludge and moisture to 17,950 pounds, of which lu,360
pounds is water. This is equivalent to 1,720 gallons per
million gallons of water treated. All water used for back-
washing in this method of treatment will be water to which
chemicals have been added so the unit cost of this water

will be the cost of the raw water plus the chemicals re-

quired.

- 111 -

The total water required per million gallons of
treated water will be:

For backwashing, 2%,300 gallons
For desludging, 1,129 gallons
Total 26,020 gallons per million gallons

of water softened.

The quantity of water required for backwashing in
the seolite method of treatment was determined on page 95 ,
e.n3 percent of the water conditioned. The backwash can
be untreated water. The total quantity per million gal-
lens of water conditioned (85 p.p.m.) is 8n,300 gallons.

The quantity of water required for backwashing in
the lime aeolite method of treatment is calculated as
follows:
later passing thru zeolite, 553,000 gallons per million gal.
Cater passing thru sand, h47,000 gallons per million gallons.
Fbr backwashing seclite units, 553,000 x 9.35 a 51,750 gallons
For backwashing sand units, “£7,000 x 2.h3 - 10,870 gallons
For desludging, 379.3 p.p.m. x 8.3“ x,1%%,-
15,800 lb. sludge,
lees solids 1%:6g8' lb. water - 1,529 gallcns

Total 6#,1fl0 gallons

per million gallons of water softened.

The backwash in this method of treatment mist be conditioned
water.

- 112 -

Ilecgrig figwgr figggiggmeptg
The line soda ash method of treatment will require:
Kw—hr.per day.

1 .. '2 hp. for mixing, operating 21!» hours per day - 35.8
6- 1 hp. for clarifying, operating 2% hours per day - 107.11
1 .. 37 hp. for backwashing, operating 1 hour per day - 27.6

1 - 20 hp. for chem. conveyor, operating 2 hours per day - 29.8
3 - 1} hp. for chem. feeders, operating 24 hours per day - 26.8
Lights, 20 kw. load, operating 6 hours per day 499.9
Total 11117.11

“#7.“ x 365 II 163,000 kw—hr. per year at 1.25¢ I 2,037.

The seclite method of treatment will require:

2 - 5 hp. for brine pumps, operating 6 hours per day - 45.0
1 - 30 hp. backwashing, operating 3 hours per day - 67.3
1 - 15 hp. salt conveyor, operating 2 hours per day - 22.“
Lights, 6 kw-hr. load, operating 6 hours per d” - 1g Q

Total 170.7

170.7 x 365 = 62,300 kw-hr. per year at 1.254: = $779.

The lime aeolite method of treatment will require the
same as for lime soda ash except that 20 kw-hr additional per day
will be required for backwashing zeolite.

“7o“ x 365 = 170,500 mm. per year at 1.25¢ = $2,131.

-113-

bo t
The lime soda ash plant will require:

1 Chemist at $2,h00 per year - 6 2,900
k Operators at 1,600 per year - 6,u00
1 Laborer at 1,200 per year - 1,200
Allocated share of superintendence - m

Total 311,000

The zeolite plant will require:

h Operators at $1,600 per year - 3 6,000
1 Laborer at 1,200 per year - 1,200
Allocated share of superintendence - _1.999

Total 8 8,600

The lime zeolite plant will require the same labor
as the lime soda ash plant.

- 11h -

The time when extensions to the water conditioning

plant will be required can be determined from the fellows

ing data:

Per Capita Average Max. Ratio of

Pumpage gal. Daily Daily 7 Max.to Avg.
Year Population per day Pumpage Pumpage Pumpage
1910- . 31,000 96 2.8 5.9 1.75
1920' 57.237 83 “-75 8.5 1.79
1925- 68,000 10h 7.07 11.2 1.58
1930- 78,105 -109 8.52 11.95 1.75
1932- 75,800 at 6.37 10.78 1.69
1936 (a) 98,000 lou' 10.2 18.0 1.76
1910 (b) 115,000 115‘ 13.2 22.6 1.71
1945 (c) 135,000 118 16.0 27.1 1.71
1950 155,000 121 18.8 32.2 1.71

' Actual data.
(a) Add 5,000,000 gallons per day capacity.

(b)

Add 5,000,000 gallons per day capacity.

(c) Add 5,000,000 gallons per day capacity.

- 115 -

-Igriaple Charge; - Lime ggda Agh Irggtgegg

The charges that vary with the quantity of water con-
ditioned for the lime soda ash plant will be:

1'1er 13
Chemicals
Alus 83.0 lb. at 825 per ton - \. 3.4-1.0".
Lime (CaO) 2,502 lb.at 811 per ton - 13.76
Coda Ash 673 1b. at .33 per ton - 11.10
Coke l+6.7 lb. at $10 per ton - ____,_23_
Total ' " ' $26.13 per mil-
ion gal.
lash Water
Raw water 812 per million gallons
Chemicals £6.13, per million gallons
Total $38.13 per million gallons
26,020.gallone at 838.13 per million 0.99 per mil-
ion gal.
Additional pumping head
8 feet at $0.08 0.61!- per mile-
_______ lion gal.
Total variable costs $27 .76 per mil-
lion gal.

-116..

ar e 1 r e - 2e lite T eatme

The charges that vary with the quantity of water

conditioned for the zeolite plant will be:

TABLE 1“
Chemicals.
salt 7,539 lb. at 87 per ton 826.39
Liquid chlorine 2.5h lb. at $160 per tggggg,
Total per million gallons
lash Water
Raw water 8h,300 gal. at $12 per mil.
Additional pumping head
7.1 ft at $0.08
Total variable costs per million gallcns

- 117 -

826.59

1.01

823417

a b 8 ar - i e e 1 e Tre t e

The charges that vary with the quantity of water
conditioned for the lime seelite plant will be :

TABLE 15
Chemicals
Alum 83.4 lb. at .25 per ton 8 1.08
Lime (CaO) 2,502 lb. at 811 per ton 13.76
Celt 2,527 at 87 per ton 8.8%
Coke 96.7 lb. at 810 per ton ___923
Total per million gallons $23a87
ween Water '

Raw water $12.00 per mil.ga1.
Chemicals i33.§1,per mil.gal.
Total 835.87 per mi1.ga1.

64,1HO gallons at $35.87 per mil. 2.30
Additional pumping head 5 '
8 feet at 80.08 4,95;

Total variable costs per million gallons $26.81

- 118‘-

 

Average 99119 9691 9
9111109 9911919v

Maximum 9911? 99919 9
9111109 99113 9

Tfifial 999991 pump9g9
9111199 9911999

Sap9oity 91 91991 '
9111199 g9119n9 99? 999

Total le99 3991191
Or1g1nal 199191191109
990111099

Total
Total 199991 $991999

Variable op999119b 99919
$27.76 999 9111191 99119

99 91
Sperating 19991

Water for operafiing hy9199119 991999
Electric Power

Maintenance, 1% 11199 9 g

Loss in £1119: 9999 19 9999911y
Depreciation

Ori ginal plant

Additions

Total 099191199

Capital ohargea, 99% on £1199 capital
Total annual 00909

Operating 90919 991 9111199 gallon

Capital charge per 911110n gallon
Total annual Costs per m1llion
gallon to distribution system

Coat cente,p99 100 cu.ftadelivered
to customer

Cost cents, per 1,000 gallons delivered
to customer

 

GQST SF

A 3"»
<3 1

“r; c’"; :fj
2111.” 0 £2

9,191¢§

99
91

£717 )2; 4‘ 33"”: {‘F9
VJ 1‘49." ‘9:wa

, 997-1799: “ii-1 M T"?

91990
9 $12§§§

99

1 40.01
9 47.20
M.4l¢

5.90¢

TABLE 16

GPEEATING LIME SODA ASH TREATMENT PLANT

99

H
\95
9
CN

1E,g;0

3 2 .

3 37.02

1.1119

1 42.90
3.96¢

5.30¢

$101,393
12,000
600

2.237

4 ,340
160

292
93799
11137218
9 36.50
5.35
$ #1.85
3-91¢

5.22¢

" 119 a.

12

20.#
4,383.0

20

$350 000
fin 000

3933:005

$121,672
12,000
600
2,237

14 .

23.8
5,113.5

25

$350 000
l68 coo

$513, 000.

3141,9517.

13,000
700
2.437

.$_34.00
;_2_2§.

16
.27.2
5,844.0

25

$350 000.

168 000

$518, 000

$162,229
13,000

..700 .
2.“37’

5,160

200.

990

9,”

_ 2 10
$2»

.13  37 96
 3 52¢ I

u.74¢ .-

18
-30.6

6,574.5
30'

$350,000

a 2 000
16651000”

$182,508
19,000
80°
2,673
6,020

240 _

9 990‘

$2

$ 2E:030

'fi 33. 98 '

4.12

$;39.10 1

.3.56¢

4.76¢

 

'\

‘
.‘A 0 h”;

«K.

IfiIOT
1d

nticteqc
.txvss

£531?

azaqo 101 1533?
Iflwcq

Imfifil S

1?;

!

M
r.“

’T‘

orxr
“AA

“WV" ‘3'

't
v

'. "1..
;~,§

«“s ‘2'”!
...
\d-

5

.. '
. .

52.1.

'9»

....4 n

5 Q I i ,U
.3 a... 5 .... up.“ a;

.3 a «L

3 £8.99 ...u
out. Siffi
Jfl +ufl0rx.

....v I 3

.5 a... ....»I a.
«In

9‘ J.

g
It,
ans!

I, . fix

a... .. .. A. C. .
”s; u ...-«M M! y\
....u A...» mw
. u flux.

0. 4‘

I. —.l .a
if;

1C?

9

F

‘1 téq.sinéo Ja-

UV

0?

.3

Vrhl‘. i
¢ “*{Jhm

t4.
\

Ismoieuo
IsmciaLn o:

7261!?

.1

q 83900

'T :1
~
I“. _

...Po‘ '1‘?“

v a‘

.
--l' -'v- .
9"". W? ,
D - ‘
‘ P

-..
r

‘ _ .
' ",—"’W4j.

QQEE 00 Q.£R&TI§$ ZEQLITE TREATMENT PLANT

 

Avsraga 80110

' a c - ' ,1 $5. 37: .<:..-. .3
170.11. £001.»; *0:
a. , V

million 3011000 6 5 10 12 14 16 18
Maximum 1011? pumgag0 ,
million gallong 10.2 13.0 17.0 20.4 23.8 27.2 30.6
Total annual pumpagg _
million gallono 2,191.5 2,922.0 3,652.5 4,383.0 5,113.5 5,844.0' 6,574.5
030001 ty 0f gloat _
million $011000 p00 day 15 15 18 '21 24 27 30
$0tal Fixed 0301001 .
gig-1:11 12130311252102: $300,000 $300,000 $300,308 030:,000 $320,000 $302,000 $300,000
'r;1fi.0na _& w_4w 4 10 000 1 2 000 21 000 2 0 000
To tal 53003.0 $m300“1,0“00 $3 , 0 $W‘”,000 0m $316‘”,000 $317L‘“0,ooo
Total Annual 0harg00
Variable opofafiing 0001500 00 , 1 ~ ' '
$28.17 per m11110n $011000. 3 61,735 $ 8;,313 $102,891 $123,469 $144,047 $164,625 $185,204
Operating labor 8,600 8,600 9,000 9,400 - 9,800 -10,200 10,600
Water for Oparatimg hyifaulio 001000 500 500 600 .700 I 800 l 900 1,000
Electric pg... 719 779 879 979 1.079“ 1.179 1.279
Maintenance, 1% $1100 0001101 3,000 3,000 3,540 4,080 4,620 4,160 5.700
Loss in 2001100, due 10 010210100 .
ani wasto $0 1%% amnually 2,100 2,100 2,520 2,940 '3,360 3,780 , 4,200
Depreciation , ,1 0
Original plant 10,448 16,448 16,448 16,448 16,448 16,448 16,448
Additions ... - 186 6 2' reg-fig 12' 44 11%;2?
Total Operation $93,102 $i199?35 4 3 . $ . $ . $2 . 3 $2 ..3
Capital charges, 1.53; on 11:03. oapi'tal 1%,?"00 1 “‘00 1 0 18 6o Eggkggg 2 220 ' 2 6
Total Annual Costs $1 .0 3 $I§$f5 $ .9 4 ’. 3 . 0 3 3 .2 N 353215;?
Operating costs per million gallons 8 42.50 0 38.80 $ 38.16 $ 37.50 $ 37.10 $ 36.80 $ 36.55
Capital charge per million gallons 2.126.231, 4.61 ___4_._3_§_ __4_._l_9_ _____lg_._o_§ __3_._3_7_ ____3_._39_
Total annual @1008 per milliom / _ _ . -.
gallons to distribution system $ 48.60 8 43.41 $ 42.52 $ 41.69 -$ 41.16 $ 40.77 $ 40.45
Cost per 100 cu.ft. dolivered to . ‘ "- _" _. , .'
customers 4.550 4°05¢ 3.98¢ 3-89¢ 3.84¢ 3-31¢ 3~77¢ '
Cost per 1,000 gallons delivered to . . ‘ '
customers 6.08¢ 5-42¢ 5-32¢ 5-21¢ 5.14¢ _ '5-09¢ 5-05¢

 

-120~

 

b'!

K‘.

. {,1

I
n'r H- ,\ t- _ . , .1
(‘1 o:~"~'~‘r. 19.5.?- r .. cur.
\ .‘ ~.. i :1 ". ‘ . ' ' b n . j- ..., I,
‘- ‘3 - ' {fi- .— u. _’.. " ‘ 3.. 4
I ‘1’ .. n .a ..., .3 ' 0" —‘ ‘1 ¢L ~45
. P n 1
'~ «1 "~.' "- V‘ 5 V- 1......“ f ,2!
:‘.‘,,_ «‘1 .... '0 1' -a ‘5. ‘uk' éJqu ...(," 0‘—
. ‘ 'Q. P " v ‘ ‘4
- - - . . x t’ .' f-
t . f .o. ~/fi ‘ . o
d . V J” 0 .« 1 .. 5 no._" .‘. . ., ‘d 3, a. .t. J, )1

t . (1. ‘e | III ' n {5' -, ‘I b" r ‘1" " Mn
\‘ h it. .' fi .\)J 5. '4. - b M);-
’H r r ~ ..
\i ' I d a
' . V 0" ': ‘5‘ ‘y '. ". ’ I . "
. . Ar 1. a. w‘ .- . ‘5 ’ '~ 0 ' 3' A 1’4.-»|
u ' '? ,r '. "Q " V“
'1' I . . e i. 0 " c‘ M i
to An I ‘L- x. V - ..., .Y ."‘ v
«r ‘:»-n*I""
. ’1: . ' , ' ‘ ‘
.‘ .. ‘4‘, x a J\; S;Iq.' ;m~ L‘ly.‘ 51;. 3‘
I .1
Ice”? -"v'<..-"‘.‘ "3"."1 I‘Nj’r
0‘; w. _‘.. .. 'w .m. ' .0. J ‘ .4 v' '-
(. ‘a 9' .‘z” .. o . q .. .. \
I r .‘ .4 I ~ * ‘} -, V ‘v - r' I ,v. ‘ v I
. ’I V‘ 1. ‘3' . '__ - 1‘s ‘ I. I '3 ‘o A: l C' 15-31 .. I , ..A 4.‘.‘~ if- ‘9-
.‘
~ ' ’ ‘ ‘r ‘ u I
i A I-da vl~ - a G' - .. u“ $l. J, :1
r ‘ . r .. . g“.
4 1.. v' a V» ~. 3‘_ 'p' O- I b! t
Q v- .0, v a 3 a -:\ a .I. a. - 5...,
E... t. C " i .. .n'J $0 .8 .‘~.‘A-L-A 0‘3:- '~‘ ' ‘
‘ {o > . ' l ‘ 3' I: J'
' ' .fia “ l ' 0' I ‘q ' n ' :7 :‘u ( Q I r - t .- o: ‘
9 A.’ ‘l" 'w s ' z." ~ I 4.) ‘9“ l. s Q! . -‘ ‘ I; ‘j ’l ‘ Q'- -’ a: .- ‘ "
s .- K. - ‘ ‘ r ‘ h . I' t t 5' n ~1~
; ‘, v ', ; } ' r1 " ' ‘- _ l' V O" Q ;' ‘ ' J‘ o '
5, 321* ' -¥~ .1 1.11..-.23 1.. 1-«1151 c... 5.5 ow”

~. ‘ i ,-

.. ' . u I )z a. .y- u '3' a r - ‘

‘1 V ~'t \J lJLa e z .! +I! $ '; o"
- ‘1 o .

I...“ ’1. ,1 7.1. ‘Qr ‘ L." ’l. r .. 5...?! ' q a 4 l.- . ¢ :- H a. -f ~ ," 1 ~ -. . .

s. 21‘.“ t. 0. w .4. .f u I 4 ...;'.. -I.! '1; 32;: .E -- .F 10.10 ..2 ' A 3 0 If!

.' 3" f , - rm"

« xv. .. f‘ I! ' if n I

22‘ ' . L5 :JJ* v 3.5: u .4.“-

h ..

V. '.'g

, )
.-o

n .‘ (Iv ls

{'- .'~. h‘ ..o g. N fl ‘3‘! «.I. Q
V9“ ex, ewe; Fe‘JYK...

f
r- . _ .0 '0 .v v. " 3 a V“ o . 7
10 9...: Aft-‘31..£.;~';u it: {.Lf‘QCU
" : r ' ' .‘
r... .1 , ‘(1 .. ”m a. i.

. 7f
. .
‘s
M ...
301-
H
t
C..
9"

,W,
‘ I
3:
Q
g u
13’
1“
b.
r.)
U:

3

~‘-- #- ,- =.'.~.r- N to?
lab .‘ 3:1.» .‘ Y ..‘--

’
.7. [1" i l. A.
,, ...}... .... .. ~~
‘ V { --'-r~ 3.1,: ~«.: .5 ~11: ‘ L l.‘.-
4

L
‘ -\ '. t. - ' I l .
' - ‘ ' ‘ 1' + "'- in" 'f i. ' ." "‘ v“ r ' n- -3 I 4'4. ‘1 v"
._‘,_ ,2, . ., . . ...? .1 is.) :. t.§t ‘.,_‘:,.,,§fl,3 ”5:,,_.,.,,;
~ n, -\ ‘5 .‘q- :- .pf ‘ ‘ - - v
. - m r "1
a ‘t at '- Q I , ’uqy T . 3.3 \- '
" g " "' ‘ * 8‘... V, {3‘ L15" 4 b Elsi .' 0f; 4' J. {J J-
I‘ " f, h r p f ,- (...
'- M a h'*f‘t.‘ ' *“- 1 ‘- ._- 4 " .. W * .- ..-a-,- . I
v ' l --d-' v {10 \-o‘; u 3" ‘3 (I... .. a ) I )4 3 1‘ E: 0‘ ET 1“ 7:; .t .53 .1 1.;
"W ’1 ‘4 If. 1‘ '\ : I '3 q'. Jo l~ :4 3F ’ 5- 'p I- -.a (J. 'Y A 1 J .' r 0‘ " ' r',’
' .f O .. 0/31‘_J A. . ~.' 3 . 5&1“. :'. -L 4. .11 '. :3~4 H; ‘11 I“ .J ) ‘L“;, .g 3‘ '.)
~-.¢.‘.-..-, -..—.g ‘.
. I‘ ‘ § ‘ 0‘ , '-
“V ' ‘ n .-, .' 4', 4 0’. - , A p-Ar'w a\" . "
A ‘., I .I.: A g a: .2 2' .1 if. CC! ..~'._.';..‘, ;_;,,.2- I 1;”, C1 a
I.‘_ , ,n
. v ‘ ,' I . ~ . v' ... ‘ . , . ‘ A -. ‘. 3 .,» , t ' ... ..., " . _.
- ‘. ‘1 u, PI 1' .f . a , A. . ! \ I .
u. an“? 1' .‘s‘v- 2 .C- L- Ju. .1 .. ~.'¢..lui_‘-, 1.... Cu {ii-LC.) 11:33
A . I" ’. "‘ I Hi f
. , } r r . v. t o (M . , I. u A .
0'- Av125£dbt3 ‘ Ou‘io. ' ‘x'..-- 1"q J'<-")
* "s
" ‘1 ~‘ r (I - - ., 'v
T" 2" ' ' c.¢~tt¥\t:d :9

g
, 1 , .4 ‘f g..- /~. l' -, -..,
’v ' ' 1" ‘..u.su " £ v

4‘- :
fl»!

 

Average daily gumpagg

“‘1- E HWY“ 6‘
bflfii ’

TABLE 18

SPERATING LIME ZEOLITE TREATMENT PLANT

millien gallsma 6 8 10 12 14 16 18
Maximum fiallyigumpggg
million ga110m0 10.2 13.6 17.0 20.4 23.8 27.2 30.6
Tetal annual gumyaga A ’ m
millicn gall0n0 2 191.5 2,922.0 3,652.5 4,383.0 5,113.5 5,844.0_ 6,574.5
Cayacity of plant 5 ' , '
million g0110n0 00: 10y 15 15 20 20 25 25 30
Tatal Fixeé Capital -
giggtgal 100001100100 $403, 00 $403,000 $483,288 $403,000 $403,000 $403,000 $403,000
0H0 ,, 1* ,.7 5 10 000 20 000 208 000 12 000
Total .20.?” 00 $103,000 1W0 ,0 03W , 0 W $€ITf600 457151000
Total Annual 0hafg03
Variable operating chargea at 3 ,
$26.81 m11110n gallama, p01. $ 58,754 $ 78,339 $ 97,924 $117,508 $137,093 $156,678 $176,202
Operating 1.00: 11,000 11,000 12,000 12,000 _ 113,000 13,000 14,000
Water for operatigg hydraulig 001003 500 500 600 600 ' 700 700 800
Electric Powe? 2,131 2,131 2,331 2,331 2,531 2,531 2,731
Maintenanca, % fixed cagital 4,030 4,030 5,070 5,070 '6,110 6,110 7,150
Logs in £11000 sand 1&1 annually 60 60 so so 100 100 120
Loss in 2001100 15% annually 702 702 936 936 1,170 1,170 1,404
Depreciat1on ' ’ ~
Original planfi 13,822 13,822 13,822‘ 13,822 13,822 13,822 13,822
Add1t10ne " ~,fl= ~,, __;,§g1 82 6 4 . -6"4 11 481,
Total operat1cn §§0j§99 0:16:53E’ $130,990 $ 5 .17 0 2,1 $201, $§§7f770’
Capital chargaa, 45% cn 11201 00§1tal “ 18,175 ‘ 18 1 " 22 81 22,815 2 4 27,425 _3§,;1§
Total Annual @0832 $ 093I%E $'3 0 9 $15 0 . $17 :9 9 $ 9: $22901 0 $259394
Operating costs per millian $011000 $ 41.50 $ 37.80 $ 37.40 .$ 35.70 $35.63 $.34.50 $ 34.53
Capital chargss per million gallons 8.20 6.20 6.26 __5;§§, -__§;1§g __4;Z; l;+4g§2
Total annual 00003 per million , _ f . , '
gallons to fiistribution system $ 49.70 3 44.00 $ 43.06 $ 40.92 3 40.99 $ 39.21, 3 39.42
Cost per 100 fiu.ft.deliverad t0 ,- . .
customer 4.05¢ 4.110 4.07¢ 3.82¢V 3.83¢ 3.67¢ _3.69¢
Cost per 1,000 gall0ns delivered to ‘ I ~ . . .
customer 6.21¢ 5.50¢ 5.45¢ 5.11¢ _ 5'12¢'. 4.91¢ 4.93¢

~ 121 ~

 

«T'-
u.’ .-

.1:

If:
£113.11

. '4'?‘ “9 ”'1'“

fihAn' tulip.”-
”SW“ VA
,5 {my

.2.

p

’3‘“
i
.1-

‘¥

.J

1.. ....
f. M;
J ..
...... I.
.m. .

...;

....3

5
\...:4
..m
o...

J. 1,1

I

‘.~

' {-.fi
71.1

r
do '1‘

. .r
071.!

M.
J-

. "‘.
02." hi

3.1

-,, .4

r
.L .

Harms.
... .
w 1.
w. .u
.n A \m
u
a...
.r.. a...
u.
“..--
. ...?
1. ..
1..
. .
_ ,. r
-. .lo
. a
ha .0

i" ,5 'V‘l
4w;- 1+ O J.

‘1

|
-.r

rt" .( fl

“.1
..
w'

I

l
.

(p " #‘f *f".
3’3‘ .;.:.‘0:-

33.

..L‘
I .
.I .
‘0
0
.01;
.A.

0~
....

. .
.: -,]
n. .

9

p
'a5

v.r

J

)9

\

M!

’1 I] .-
‘1

. .1
r . .4

or. w'
-

k
\

., --1-..-._.-.1..,.
'.

f.
.1“. x...
4 . i

a .

. .0
i ., .3.
f . .. 4

-..
Y:
’1. a3...
...» rm.
.I. .0 .v
a... .3.

\
~4-—.

‘. Q. a- -.

o

‘1
"-3

1'21-

1:.-
- .

(A. l‘"
.1 a, .L

.9, r-
h).

'
~

‘A
34.0.1.

 

 

-fl-1-1..l.1.1.-...-...1111111 1.2.1..-- 1.- - “11 . 1.11-1111} 1-11..-.1111.¢nm111113 ..1.
. mzodao. .._.0 39.52 J J J . :
5m4m>m-wzo:ramzz.m 06.60 :864 .z. . .
.0Qom.J;....--J.. _ g . , . W

 

  
 

 

. | ~ .
..\...-‘-aq* H~~—. .w ,—..— - »
._ . I

 
 

 

. . . .
-.. 7.1.- -- 1-4-1.1-- ..1J11111TJ11:3
o. . . a .. . .

J . .. .J- . ; . - ....H .4
..... .. T. J --.1--. -5.-- .44.--

       
     

 

 

 

 

 

 

 

 

 

 

 

 

l
9

 

g-.. .x 326:...154 400m 2.136
. . _ w ,_

 

_.M.3.H.Jw . _...J.
.J. N ..
1.1.1.11 lmr M m H J
J _ J S . .H J. .4u.1
#611 H . .J- . .M ..J.
J , d .. ._ .. J . 4
--.. . 11.. a .11.. J1141wi. 1.11.41- 1 H 11 J111111 1N1! 1 I1J-I.¢1........111N.1111J1|1.i [1.1.1.114 . .L
..J..f..1~ . J. J. . J- ..“JH..- J.
WhanW J. . 6+ 1..
. .. .J... .. w . .N. OOIFU§4 “54.0w” Tzflw >0:

. 4 -
. 606%....mt 8T6 +1..
4,

9 0151111er
1
1
1
1
1-

“'10.
In
-Ji,

J»-_
y-

 

1
1
‘1

 

 

3.0
.Jl ..

 

M
I
L- c—w...

 

L
i
l
l
4
O
1
Q
0
V
l
O
1
I
' f
“57‘3‘7‘””“‘
!
1

i {

 

 

 

. . -
A_J
.

 

 

 

 

. .. _
VI}- 1...
_ .

 

 

 

 

 

 

' '-;0321n111n 92910711.

 

- | . . O
1-~.-r—¢—-..7- .4}- ”—1. —- A —— p“ 4 -—-.-. - -
. . . , . .1
- . . .
p

.3 i
1.--- 1
l

 

 

 

 

 

 

,1.

h

\JA‘u-Y-

h

I

~54

5

1‘1. Win. A‘ V

.I./\I

U

‘Ikfl .vha

‘w~!\l\

V‘

Inu~£

nMrfi<JJaQ

N AHINMV Lv

.._-- _.- _4A_ _U I
1

108 GALLONS T

l

. '_ _4‘

T”

Lia-IRS; PEf-‘i -'w

~ COST-Loo

LJT-ION sv $11: M

I
1

q DISTRIB
WG.‘D: '

L

l
- .- ..-‘._.A.
1

I
I
I
l
l

..- ...— ?.- -

1

ILY- fPWkAGE g a:

1?

~ AVEMGE —

‘ 1

 

I
I

 

 

 

 

 

 

 

 

co-o-dud h

T

 

 

 

 

 

 

 

 

 

 

 

 

 

I «. ju—i4fi‘
2 l ' l

I I . .
o -. ... —"o~o-~—4- ”Tn-......fi f‘

 

 

 

 

 

1 LIME

szA ‘fASH

7 _I. ...~.

I
--I. ..
1
1
1

1

.

 

 

 

 

 

_.——.~. ......

 

%

ZEbLI-re; *

LIME

, ‘ zeougrc'
METHOD OF TREATMENT ‘1 ‘

1
|
i

‘ , .

cAPI1‘AL CHARGE.
’ 1, A . #w.

__,,._-_.,. ...r.-

MIsc.§ExP

{P~--'-..-——‘ +~~~d L—x—OA—Lm- q--;‘_- o .. _
f I

1

OPERATING L

‘1- -.‘ ..1”

EA 1

I

1

1

. .. ‘mfl Ho‘p... - ..-

i I

_ 1r. ...- j
. 3 .

i

1 l

I 1 1

I I I
‘ l

Abe—ooIadu-uman—«r-un—b—r- cw... .—~¢_._-... ~. .. ., ... - ..---. ..--

‘ i

5

I

1

"MAIN1ENANCE . “ i '
ENSEI ' '

ABbR

. + (10511 OF CHEMItALs .

l

I
.-.L.. ...-.....y ..-. .---
.

- mos- .-_o— ~

‘- ”-..—..-. ..hr-_I

bumgthAmN - _ i

!

TIONAL PUMbINc HEAD]
I ’ - 1

.- ~_..¢_~...__.-..- -

CHART 2|_'

WII"

I I

‘~“

I'Z\.Jl ‘1‘

:1\ .‘I \

h‘rl‘

IV

 

 

1
1

BACKWASH WA'II’ER

 

1 , .
_ __4.~.*.-_.1...-~_T.-W
1
1
1
1
1
1
I

O1" .-QHB

1

I

1

I

1 I .
.... A- “1‘...“ .-.—......

1

1

I

L

TzIII-ITIIIIIu.
_ .

*

_

MISC. EXPENSES

.DEPRLECIATION

. ~ MMN‘TENANtEW - -
OPERATING LA 1 R
1:001-

.1
..1.
1
1
1

1
l
I
‘

5 .--~-_——--

..—~§...

._.._.-. ..-¢. .-——— ..
I
I

: CIjART 22'

.-4-

 

 

 

 

T ADMIONAE' 'PUM1’ING'HEAD'

. 4.III

 

 

 

 

 

, .
1

I

1

.IJME.
ZEOLITI'E -

 

ATMENT.

 

1
44
1
1
.7“... ..-...fs _

 

 

' -un-l p....-—— - V._4 y...
; ' , ..

- ..43
53

., j..l,6,. w”.
26

-....09 -

 

 

 

1

T‘V‘1‘.

I
1

I . I
-..... - ..."...L“.-_. - _

1

...L

zebLiTEI
“of

 

 

 

 

 

 

h-

 

 

I
1
1

 

 

 

 

 

 

 

 

 

 

 

 

 

L...
Irv-a4.
L-

IuME
METHOD"

 

 

’—

__I.. ,._. -. in $102

 

4? 9...; .. .
1.3.0 uva, K...--.+1 KI +1 1 ...,_._:.-
00.24;: ......mmmI 203V 0 2}: «Wm szuUIFnou

11II111_.I 11L1II._.1 1I1I- -..I1L11..1- .P:I.. I I1-

 

 

 

 

 

  

 

 

 

.1

s
‘

' l‘ I I

st -. , -:

‘In I . ...

.‘Mfi-W

1

SODA. ASH

.14- .»

 

Chapter x

Qanslnalmla

The comprehensive study of the different methods of
conditioning this water indicates that the most economical
method of conditioning, shen all factors are considered,
is the line soda ash method. charts 20, 21 and 22 shovrfihe
variation in unit operating costs for the three methods of
conditioning water. The increased cost of service will
averége 3.96 cents per 100 cubic feet of water utilised .
when the punpage to the distribution system is 3,000 mil-
lion gallons per year. The average annual water consump—
tion per residential consumer is 59 hundred cubic feet. ’
The annual additional cost sill be $2.31}. To offset this
additional cost the following direct economies are effect-

ed fcr the consumer:

Soap saying of 81.50 per capita.per year, assuming

3 in the family, total saving will be Ou.50
Plumbing bills per customer 2.50
Wear on cooking utensils .50
Fuel wastage due to scale 2.00
Decreased life of linens, etc. .__§,QQ,

Total $13.50

The same savings can be made by the customer by the
installation of an individual household softener. The cost
of making this installation sill be .150. ‘The operating
cost will be 03.00 annually for salt and 815.00 for fixed

-'122 -

ohargee; a total or 818.00. The installation of indivi-
dual softeners may not be justified from an economic tieva
point but the additional conveniences are 'ell worth the
added cost. The installation or a single municipal aor-

tener can be made for an average cost per ouetmner of $20.00.

- 123 -

newcomer

QEQELEL

Daytona Beach, Florida, later lorka
e. F. Tipplnl a 1.1. Stuart, 32.8%, Vol.23, Jan.l93l JAllA.

Developments in later oftsning
0. P. Hoover, p. n2, Vol.20, lov. 1928, JAllA.

Future of later Treatment a Filtration, The
J.R. Baylis, Vol.80, Jan.l933, later lorks a Beverage

Ieohanioal Developments in later Treatment Practice
0. r. Leander, p.16u9, Vol.21, JAWlA.

Hiatreatment of later, The
O. R. Knowles, p.M90, Vol.25, Apr. 1933, JAllA.

la! Fort layne later 8 1y The
R. L. Hclaaee, p?§g, Vol.23, Jan. 1932, JAllA.

'0' Hiesouri River later lorks of 8t.Louia
L. A. Day, p.985, Vol.21, JAllA.

It! later Softening Plant at leodesha, Kansas
F. I. Veatoh, p.25, Vol.79, lar.l932, later lks.& Sewerage

Operating Experiences lith a New later Softening Plant at narion, O.
I. E. Flentje a O. lhysall, p.778, Vol.22, JAWlA.

Ottawa's lea Filtration Plant
l.l. HoDoneld, Vol.79, July 1932, later lks. & Beverage

Past, Present & Future of later Treatment, The
8. 0. Johnson, June 1926, Hailsay Age

Present Status of Municipal later softening
O. P. Hoover, p.181, Vol.25, Feb. 1933, JAWlA.

Purification of Highly Turbid waters, The
J. D. Fleming, p.1559, Vol.22, JAWWA.

Recent Progress in the Art of later Treatment
A. lalman, l. Donaldson a. L.H. melow, 13.1161, Vol.22, JAllA.

Treatment of Filtered later with Line at Harrisburg Pa.
Richard H. Gould, p.355, Vol.19, Apr.l928, Jim.

- 12H -

later Hardness, its Effects and its Removal
R. E. Thompson, p.#79, Vol.20, Oct. 1928, JAVWA.

later Softening at Columbus, Ohio
0. P. Hoover, Vol.78, 0ct.l93l, Water lks. a Sewerage

later Softening 2 Purification Plant of Dundee, Mich.
0.8. Finkbeiner, p.u5, Vol.78, Feb.1931, l.l. a Sewerage

later Supply a Purification During 1931 - A.Heview
l. J. Howard, p.l, Vol.79, Jan.l932, l.l. & Sewerage

later Softening Plant at Marion, Ohio
6. lhysall, p.628, Vol.21, J.A.l.l.A.

later Softening Plant at lestern Springs, 111.
D. H. Harwell, p.105, Vol.80, lar.l933, l.l. a Sewerage

later Softening a Purification Hethod
J. A. IcGarigle, p.1609, Vol.22, JAWlAu

later Softening Plant &IPUmping Station Improvements at Foetoria, 0.
J. F. baboon, p.503, Vol.19, Hay 1928, JAllA.

later Softening Plant at lestern Springs 111.
n. Maxwell, p.5u6, Vol.25, Apr. 1933, JAWlA.

-125-

1 KLZLBE.

Alum Agitation Studies at Reading, Pa.
p.101, Vol.93, July 1924, Engineering News Record

Composition of Alum Floc in Mixing Basin
3. S. Hopkins, Vol.12, Dec. 1924, JAWlA.

Design of Mixing Basin
J. R. Baylis, Vol.78, Jan.l931, later Its. a Sewerage

Experiments on Formation of Floc for Sedimentation
I. S. Hopkins, p.204, Vol.90, Feb.1923, Ingr.News Record

Flint later Filter Improvements and Reconstruction
p.1189, Vol.84, June 1920, Engineering News Record

Flow Formation & Mining Basin Practice
0. E. lillcomb, p.1416, Sept.1932, JAWWA.

Mechanical Agitation by Motor Driven Paddles at linnetka, 111.
C. Leipold, p.103, Vol.80, Mar.l933, later lks.& Sewerage

Mixing Chamber Being Added to Hannibal Filter Plant
p.849, Vol.100, May 1928, Engineering News Record
ent
An Experimental Study of the Relation of Hydrogen-ion Concentration
to the Formation of Floc in Alum Solution
018. Public Health Report, Feb. 2, 1923

Experiments on Formation of Floc for Sedimentation
I. 0. Hopkins, p.204, Vol.90, 1923 Engineering laws Record

low Sedimentation a Coagulation Basins at Toledo
0. l. Sonoolmaker, p.443, Vol.92, Mar.1924, Engr.lews Ibcord

Optimum Hydrogen-ion Concentrations for Co ation of Various laters
0. F. Catlett, Vol.11, July 1924, JA A.

Principles of Four Kinds of Flow in Settling Basins
. Xiersted, Vol.93, 1924,Engineering News Record

Sedimentation Basin Research a Design
A. B. Merrill, p.1442, Sept.1932, JAWWA.

Settling Basins for Coagulated Water
J. R. Baylis, p.61, Vol.78, Mar.1931, later Wks.& Sewerage

- 126 -

Illlralima

Cedar Rapids later Softening & Filtration Plant
L. R. Howson, p.204, Vol.24, Feb.1932, JAWWA.

Design & Construction of Small Filtration Plants, The
H. H. Bell, p.653, Vol.19, June 1928, JAllA.

Design & Operation Data on Large Rapid Sand Filtration Plants
in the united States and Canada.
E. A. Hardin, p.1190, Vol.24, Aug. 1932, JAWWA.

Discredited Filter The
C. Hungerford, Vol.79, Apr.l932, later lks.& Sewerage

Fi1ter Sand Studies
J. R. Daylis, p.43, Vol.79, Feb.1932, later lks.& Sewerage

Filter Sand
J. l. Armstrong, p.1292, Vol.23, Sept.l931, JAllA.

Filter Problems and later Softening
C. H. Spaulding, p.1352, Sept.l932, JAllA.

Filtering Materials at St.Louis
A. G. lolte, p.13ll, Vol.23, Sept.l931, JAllA.

Filtering Materials for later lorks
l. E. Stanley, p.1283, Vol.23, Sept.l93l, JAWlA.

High Rate of Filter lash
l. 0. Lawrence, p.1358, Sept.l932, JAWWA.

Hydraulics of Rapid Filter Sand
R. Hulbert & D. Fiben, p.19, Vol.25, Jan.1933, JAWWA.

Improved Mechanical Treatment of later for Filtration
M. C. Smith, Vol.79, Apr.1932, later lks. & Sewerage

leaping Rapid Sand Filter Beds in Good Condition
J. R. Baylis, Vol.79, Apr.1932, later lks. a Sewerage

lew Rapid Sand Filter Plant, lashington, D.C.
P. 0. Macqueen, p.483, Vol.19, May 1928, JAWWA.

lew Toronto Filtration Plant and Other Extensions, The
l. Gore, p.1620, Vol.21, JAW'lA.

- 127 -

Observations on Filter Sand Shrinkage
lm.lallace, R.Hulbert a D.Feben, p.870, Vol.23, Jan.1931,JAWWA.

Operating Experiences lith a Large Filter Plant
J. 0. Keith, p.1629, Vol.21, JAWWA.

Progress Toward Filtration in Chicago
M.B.Reynolds a A.E.Gorman, p.965, Vol.24, July 1932, JAllA.

Report of Committee on Filtering Materials
p.13lb, VdL24, Sept.l932, JAWWA.

Specifications for Filter Construction
l. E. Stanley, p.105, Vol.25, Jan.1933, JAllA.

Studies on the lashing of Rapid Filters
R. Hulbert a F.l. Herring, p.1445, Vol.21, JAllA.

Trial Filtration Plant, Ottawa Canada. The
c. c. Hasmith, p.1017, Vol.22, 5mm.

Varying lash later Rates lith Changes of later Temperature
. 0. Lawrence, p.208, Vol.2 , JAllA.

later Filtration Plant at Sheboygan, lie.
0. B. Burdiok, p.1247, Vol.22, JAllA.

Year's Operation of Filter Plant at Peterborough Ont.
R. L. Dobbin, p.795, Vol.20, Deo.1928, JAllA.

- 128 -

Asralicn
Aeration ‘
J. R. Baylis, Vol.79, July 1932, Water Its. & Sewerage

Aeration of Water
l. S. Hahlie, p.692, Vol.19, June 1928, JAWlA.

Aeration - Present Practice
J. R. Baylis, p.275, Vol.79, Aug.1932, later lks.& Sewerage

Present Status of Aeration
F. E. Hale, p.1401, Sept.l932, JAWWA.

Theory a Practice of Aeration The
l. F. Langelier, p.62, Vol.24, Jan.1932, JAWWA.

63'

An Iron Removal Zeolite
p.153, Apr. 1932, later lks. & Sewerage

Hydrogen Sulfide Removal & later Softening at Bever1y Hills, Cal.
R. L. Derby, p.813, Vol.20, Deo.l928, JAWWA.

Iron a Line in Removal of Manganese
E. 0. Craig, E.L. Bean 2 R.l. Sawyer, p.1762, Vol.24, loV.

1932, JAWWA.

Manganese and Its Relation to Filters
P. Boynton a B. V. Carpenter, p.134l, Sept.l932, JAllA.

lew Iron Removal Plant at laverton, H.C. , The
n. r. Trice, p.716, Vol.24, May 1932, JAllA.

Removal of Iron from Hard Ground Waters
R. L. Molamee, p.758, Vol.21, JAWWA.

- 129 -

Activgted gggbgg

Activated Carbons & Their Use in Removing Objectionable Tastes
and Odors from later, The
J. R. Baylis, p.787, Vol.21, JAWWA.

Taste Elimination lith Powdered Activated Carbon
E. A. Sterne, Vol.78, Jan.1931, later lks.& Sewerage

Use of Charcoal a Activated Carbon in later Treatment, The
J. R. Baylis, p.14, Vol.79, Jan.1932, later lks.& Sewerage

£22111:

Chemical Exchange Reactions of Zeolite
C. J. Frankfoder a F.l. Jensen, Vol.16, 1924 Jour.Ind.Chem.Eng.

Engineering Studies of Municipal Zeolite later Softening
H. n. Jenks, p.342, Vol.22, JAWlA.

low Base Exchange Silicate for later Softening
V0.61, Apr.7, 1925, Power

Prepar tion a Comparative Performance of Base Exchange later
Soften‘ng Materials, The
r. a. Higgins & J.P. O'Callaghan, Vol.44, Sept.l925, Chem.Ind.

Softening Municipal later Supplies by Zeolite
J. T. Campbell, a D.E. Davis, p.1035, Vol.21, JAllA.

Softening Municipal later Supplies by Use of Zeolite
J. T. Campbell, a D.E. Davis, Municipal Hews & later lks.1932

Trends in Municipal Zeolite later Softening
l. J. Hughes .1. H. B. Craver, p.68, Vol.22, JAllA.

Use of Exchange Silicate (Zeolite) later Softeners in Railroad Practi:
G. L. Baxter, p.755, July 1928, Industrial a Engr.Cbemistry

later Softening by Zeolite in Municipalities
S. B. Applebaum, p.13b4, Sept.l932, JAWlA.

Zeolite Softening Plant Operating Experiences
D.E. Davis & J.T. Campbell, p.952, Vol.22, JAllA.

Zeolite later Softening Plant for Marshall, Missouri
B. l. Crenshaw, Public lorks, 1932

- 13o -

Miacillaaaaua.
Dollar a Cents Value of later Softening
A.V. Craf, Vol.79, lov.1932, later lks. a Sewerage

Laboratory Research in later Purification Control
E. S. HOpkins, P.27, Vol78, Feb.1931, l.l. a. Sewerage

Manipulation of pH at Springfield, Illinois
0. H. Spaulding, p.1190, Vol.23, Aug.l93l, JAWlA.

Observations of later Supplies of London a Paris
E. Bartow, p.267, Vol.23, Feb.1931, JAWWA.

Purifying later for the Textile Industry
S. B. Applebaum, p.47, Vol.79, Feb.1932, later l.& Sewerage

Quality of later & Soap Consumption _
H. l1 Hudson, p.645, Vol.25, May 1933, JAWlA.

Reduction of Carbonate Hardness by Lime Softening to the
Theoretical Limit
C. P. Hoover a J.M. Montgomery, p.1218, Vol.21, JAWlA.

Soap Consumption and later Quality
H.l. Hudson a AtM. Buswell, p.859, Vol.24, June 1932, JAllA.

Studies in later Purification Processes at Cleveland, Ohio
l.C. Lawrence, p.896, Vol.23, June 1931, JAWlA.

Taking Hardness Out of later
R. E. McDonnell, p.222, Vol.22, JAllA.

Tuberculation of Maine as Affected by Bacteria
H. C» Reddiok a S.E. Linderman, p.293, VcL78g Oct.1931,
later lorke and Sewerage.

later Softening Practice
C. P. Hoover, p.826, Vol.23, June 1931, JAllA.

- 131 -

Chart 1

\OGNO‘W

10

11

12

13
14

15

16

17
18

CHART INDEX

Saturation Equilibrium of Calcium Carbonate
Relation of pH and Alkalinity to the Proper
Treatment of later to Prevent Corrosion.
Relation of pH to Soluble Iron

Alignment Chart for the Evaluation of pH,
Alkalinity and 002 in later

Annual Soap Cost per Capita per p.p.m. Hardness
Grading Curves for Uniform.0ttawa Sands 10.1 to 8
leight of Sand Grains

Sand Rise for Different Velocities of lash later
Filter Bed Head Losa

Variation in the Rate at which the Loss of Head
Increases Due to Variations in the Strength of
the Flocculation

Loss of Read at which Flooculatsd Matter Begins
to Pass Filter Beds.

Pumpage Data, Daily Load Curves

later Pumpage and Population Curves

Substances in Natural laters

Effect of Varying Salt Charge on Capacity of
Greensand Zeolite

The Change in pH in later with Rising Temperature
Reagent Adjustment for Lime-Soda Ash Softening
Chart for Estimation of Alkalinities from Titrae
tion Values.

- 132 -

Chart

Plate

19

20
21

22

1

(hm-FUN

Turbidity Curve for Approximate Dosage of Alum
for Coagulation

Unit Costs of Softened later

Comparison of Costs - Dollars per Million Gallons
to Distribution System.

Comparison of Costs - Cents per Hundred Cubic

Feet Utilized by Customer.

PLATE INDEX

Plans for Lime Soda Ash Treatment Plant
Elevation for Lime Soda Ash Treatment Plant
Filter Piping for Lime Soda Ash Treatment Plant
Plan of Control Table

Plan and Elevation for zeolite Treatment Plant
Tabulation of Characteristics of Rapid Sand
Filtration Plants.

- 133 -

Table 1
2

3
u

\OGNO‘U“

10
11
12
13
1h
15
16
17
18

TABLE INDEX

Molecular Reactions for later Conditioning.
Common Chemicals used for later Conditioning.
Choice of Chemicals for later Conditiontng.
Chemical Requirements and Products of Reaction
in p.p.m. per p.p.m. of Ion in later.

later Analysis Statement. ‘

Conversion Factors, p.p.m. to Milli-equivalents.
Miscellaneous Factors.

Conductance Calculations from Ionic Analysis..
Pressure Losses in Pounds per Square Inch thru
Zeolite.

Comparison of Finished later.

Chemicals Required in Parts per Million.
Chemicals Required in Pounds per Million Gallons.
Variable Costs, Lime-Soda Ash Treatment
Variable Costs, Zeolite Treatment

Variable Costs, Lime-Zeolite Treatment

Cost of Operating Lime-Soda Ash Treatment Plant
Cost of Operating Zeolite Treatment Plant

Cost of Operating Lime-zeolite Treatment Plant.

- 13h -

SUBJECT INDEX

Activated Carbon

Additional pumping head

Adjustment of chemicals in conditioned
water

Advantages of lime-soda ash method of
treatment

Advantages of zeolite method of
treatment

Aeration of water

After precipitation

Aluminum sulphate

Alum requirements

Alum specifications

Area of clarifiers

Arrangement of filters

Arrangement of inlet to clarifying
basins

Average pumpage

Backwash rate, formula
Backwash rate for zeolite
Backwash rates

Backwash rate

Backwash supply

Backwash water
Bibliography

Brine solution

Calcium carbonate saturation

Calcium carbonate solubility
equilibrium

Calculations for the design of a
lime-soda ash treatment plant

Calculations for the design of a
lime-zeolite treatment plant

Calculations for the design of a
zeolite treatment plant

Capacity of clarifiers

Capacity of greensand zeolite

Capacity of plant

Capacity of recarbonation basin

Capital charge

Carbon dioxide requirements

Characteristics of desirable water

Character of water from zeolite

110

21

93
2O

77

13?.
94

10
10
71
99

1

WWW] NWNW
‘8 H mom 0“" NO

Chemical characteristics of
glauconite

Chemical characteristics of
synthetic zeolite

Chemical feeders

Chemical requirements

Chemical requirements, comparison

Chemical specifications

Chemical storage

Chemicals used for water
conditioning

Chemistry of water conditioning

Choice of chemicals

Classification of use for water

Classification of zeolites

Clarifiers, area

Clarifier oapaCity

Clarifier, exit velocity

Clarifying basins

Clarifying basins, design
requirements

Clarifying basins, ratio of width
and length

Comparison of backwash water
requirements

Comparison of chemical requirements

Comparison of finished waters

Cemparison of investment and
operating costs

Comparison with individual softener
units

Common reactions

Commercial purity of chemicals

Conclusion

Controlling hardness of zeolite
treated water

Conversion factora

Corrosion due to water

Costs of operating lime-soda ash
treatment plant

Costs of operating lime-zeolite
treatment plant

Costs of operating seolite
treatment plant

Cost of recarbonation

1%1
a}.
107
122
’3
122
10
31
11
119
121

120
23

Deposits in distribution system

Depreciation

Depth of filter bed

Depth of zeolite beds

Design factors

Design of lime-soda ash
treatment plant

Design of lime-zeolite
treatment plant

Design of zeolite treatment plant

Design requirements for clarifying
basins

Design requirements of a lime-soda
ash softening plant

Desirable water

Determination of quantity of
chemicals required

Diffused orifices, submergence
for 002

Dimensional homogeneity of models

Disadvantages of lime-soda ash
method of treatment

Disadvantages of zeolite method of
treatment

Dissociation of ions

Dynamical similarity of models

Economic waste due to hard water

Economy of soft water

Effective size of sand .

Effect of volume and surface area
on sedimentation

Effect of water temperature on
backwash

Electric requirements

Estimate cost of lime-soda ash
treatment plant

Estimate cost of lime-zeolite
treatment plant

Estimate cost of zeolite treatment
plant

Exit velocity in clarifiers

Factors necessary for design
Factors entering into design
Filters, arrangement

5
122
21

15

113

87
104

Filter beds, depth

Filter sand, life
Filtration

Filtration rate

Finished water comparisons
Flocoular sedimenta
Flocculation

Form of water analysis
Formula for backwash rate
Functions of aeration
Fundamental reactions

Glauconite, chemical characteristics
Glauconite, processing

Granular sediments

Grate surface required

Greensand zeolite, capacity

Heads, strainer
Hydrated lime
Hydraulic action of water

Increase in total solids
Individual softener units
Industrial water consumption
Inlet to clarifying units
Ionic reactions

Ions, dissociation

Kinds of hardness

Laterals for carbon dioxide gas
Laterals in filters

Life of filter sand

Lime, hydrated

Lime, requirements

Lime, specifications

Location of wash water troughs
Losses in distribution system
Lumps in filters

Manifold in filters
Manufacture of synthetic zeolite

Maximum pumpage
Methods of aeration

Milli-equivalents

rMiscellaneous equipment

Mixing tanks

Mixing tank, size

Models, dimensional homogeneity
Models , dynamical s imilarity
Municipal water consumption

Necessity of bybpassing Iater by zeolite 90

Number of filter units required
Outlet of clarifying basins

Packing and shipment of lime
Per capita use of water
Permanent hardness

Bhysical characteristics of glauconite

hysical characteristics of synthetic
zeolite
Precipitated particles, size of
Pressure of‘backwash water
Processing of glauconite
Purity of chemicals, commercial
Pump for backwashing filters

Quantity of chemicals required
Quantity of coagulant
Quick lime

Ratio of length and width of
clarifying basins

Ratio of maximum to average pumpage

Ratio of model and prototype

Reactions, common

Reaction tile

Recarbcnating equipment

Recarbcnation

Recarbonation basin capacity

Reduction in total solids

Red water

Regeneration period of zeolite

Relation between hydroxide, carbonate
and bicarbonate

Relation of 002, pH, alkalinity
and corrosion

Resampling chemicals

Residential water consumption

Retail soap survey

Residual carbon dioxide

Resistance of zeolite to aggressive
water

Salt required for regeneration

Salt requirements

Salt, solubility

Salt storage

Sampling and testing chemicals

Sand grains,size

Saving due to soft sater

Saving in soap

Scale dissolving water

Scrubber for carbon dioxide gas

Sediments, floccular

Sediments, granular

Sedimentation, effect of surface
and volume on

Sedimentation, velocity limit

Settling efficiency

Size of mixing tank

Size of precipitated particles

Size of sand for filters

Size of sand grains

Slaked lime

Soap saving

Soap survey

Soda ash requirements

Soda ash specifications‘

Softening by seolites

Soft water, sayings due to

Solubility of salt.

Sources of water supply

Standard specifications for chemicals
used in water conditioning

Storage of salt

Storage of water for backwashing

Strainer heads

Submergence of 002 diffusing orifices

Surface tension

Synthetic zeolite, chemical
characteristics

Taste of water

Temperature on backwash water,
effect of

Temporary hardness

Tests for alkalinity

Titration tests

Time for flocculation

Total solids, increase

Total solids reduction

Training walls

Troughs, location for wash water

Troughs, size for wash water

Typical analysis of water to be
conditioned

Underdrainage of filters
Uniformity coefficient

Unit costs

Unslaked lime

Unstable water

Use of water, classification
Use of water, per capita

Variable costs, lime-soda ash
treatment

Variable costs, lime-zeolite
treatment

Variable costs, zeolite treatment

Velocity in clarifier

Velocity limit for sedimentation

Velocity of water in clarifiers

Velocity of water in conduit from
mixing tank

Velocity of water in mixing tank

Viscosity.

Wash water troughs, size

Waste due to hard water

Water required for regeneration
Water softening by zeolite
Walls , training

Yield of carbon dioxide from
various fuels

so
no
52
22

115

Zeolite

Zeolite beds, depth

Zeolites

classification

' Zeolite deposits

wumu
N-q HN

 

 

 

 

 

 

 

 

 

“vv'w—v— m

 

 

‘East'sat