299
CHAPTER
X
MANUFACTURE OF MAGNESIUM SILICATES AND
HEAVY BASIC MAGNESIUM CARBONATE
In this chapter it is intended to describe the
manufacture of magnesium trisilicate and heavy basic
magnesium carbonate for.which the processes have been
developed and the cost calculations for the above
products are presented'based on bench pilot plant
studies.
10,1 Pharmaceutical Magnesium Trisilicate (by double decom­
position process)
•.Magnesium Trisilicate is used as an antacid,
in the treatment of gastric hyperacidity and peptic ulcer
because this compound becomes gelatinous in the presence
of gastric juice owing to the formation of hydrated silica.
The latter substances serves as an adsorbent, for toxins
and is said to be valuable in coating, the crater of ulcer,
thus protecting
the irritated mucosa from the digestive
action of pepsin and hydrochloric acid.
Table 31
Specificstion of Magnesium Trisilicate.
U.S.P. XVI
•CD
MgO
(2)
B.P* 1958
(3)
Not less than between 30 20$
32.5$ in
ignited
material
Table contd...
I. P. 1955
(4)
between 30 32.5$ in
ignited
material
.
Table contd...
(D
300
(2)
(3)
(4)
SiOg
Not less than
45%
between 66 69.5% in
ignited
material
between 66 69.5% in
igni ted
material
acid •
consuming
capacity
140 ml-160 ml
.1N HCl/g of
ignited
material
250 ml. .055
HCl/g of
ignited
material
250 ml. .05H
HCl/g of
ignited
material
I<oss on
ignition
Should not
exceed 3456
between 203056
between 2030%
Ratio on
wt.%
2.1 to 2.3
^mmmmm
SiOg/MgO
ts s s z m
From the specifications, it is clear that the
pharmaceutical magnesium trisilicate must not only have
a fixed proportion of MgO and SiOg but should also have
an acid consuming capacity between 140 ml - 160 ml. .1H
HC1 per g of the ignited material.
Such a product can
be prepared from a soluble magnesium salt and sodium
silicate wherein the NagO : SiOg ratio is such as to give
magnesium trisilicate having two molecules of MgO for
every three molecules of SiOg.
It is not always easy to
get sodium silicate with this ratio.
Process worked out
is for the preparation of pharmaceutical grade magnesium
trisilicate by using sodium silicate having NagO;SiOg
(molar ratio (varying from 1*1 to 1:4.
There are two
possible ways in which magnesium trisilicate of correct
composition and required specifications can be obtained.
301
One method is to use two different kinds ef
sodium silicates in (which the molar ratio NagOsSiOg .vary
from Is 1 to 1 :4.
In the present investigation sodium
metasilicate NagO: SiOg : : 1:1
NagOjSiOg : : 1:4,097$B)
(A) and sodium silicate
were used.
The two silicates
were mixed in various proportions by weight.
The mixture
of silicates so prepared was added to a clarified and
diluted sea bittern under constant agitation.
Acid
consuming capacity of the product obtained was determined
and presented in the Table 32.
Table 32
Effect of NagO : SiOg ratio of the mixture
of silicates on the acid consuming capacity
Exp *
No,
Sodium silicate
(A)
sSodium silicate :Mol,ratio
(B)
of Na^Ot
SiOg
^of
Mol*Ilag0sSi0g1 s 1 Mol.NagOsSiOg
the mix.
1s4,097
Acid
consu­
ming
capa­
city
1
1
:
1(by wt)
1:2.17
118
2
1
;
5( "
")
1:1.405
127
3
1
:
")
1:1.45
149
4.3(
"
It is evident from the results shown above that
if the mol ratio of NagOsSiOg in the mixture of silicates
is adjusted to about 1s 1.5, the acid consuming capacity
of magnesium silicate lies between 140-160 ml .1N HCl per
g of the ignited material.
Alternate method is to reduce the mol ratio
-
302
NagO: SiOg in the sodium silicate having higher mol
ratio (more silicious) by adding required quantity of
»a2 0 in the form of sodium hydroxide.
work sodium silicate, NagO*
In the present
1 * 1*2.352 was mixed
with varying but known amount of solutions of sodium
hydroxide.
The mixture so prepared was added then to
clarify sea bittern and the acid consuming capacity
of the product obtained was determined.
The values of
acid consuming capacity are presented in T able
Table 33
33.
Effect of adding varying amount of NaOH
to sodium silicate on the acid consuming
capacity of magnesium trisilicate
Exp.
No.
Sodium
silicate
•
•
NagO
Molar rati©
(as NaOH)
of Na2 ° !Si02
in the mixture.
Acid con­
suming
capacity
1
1
•
•
0.13
(by wt)
1:1.44
125
2
1
«
•
0.117 (by wt)
1 :1 . 5 2
138
3
1
: 0.104 (by wt)
1:1.62
120
4
1
•
•
1:1.703
120
0.91
(by wt)
The results confirm that the required acid con­
suming capacity can be obtained by proper adjustment of
the molar ratio Nao 0:Si0
*
in the mixture either of the
2
two different kinds of silicates o r sodium silicate and
caustic soda.
In the experiment No. 3 o f Table 33 the
SiOg/1%0 (wt ratio) was between 2.1 to 2.3 as required
by the specifications.
303
The precipitate of magnesium silicate
obtained in the above experiments is slimy and diffi­
cult to filter and wash.
The rate of filtration
through a vacuum filter funnel is too slow.
by decantation is also
The washing
very time consuming process.
During the course of work, it has been found that
pressure filtration is quite quick though the effici­
ency of washing is lower than that obtained in rotary
vacuum filtration.
The wet cake of magnesium trisilicate contains
70-75 per cent free moisture.
Drying at low temperature
of 50-60°C is not economical.
A series of experiments
was carried out in which the wet cake was dried at
as high a temperature as 90°C without affecting the
acid consuming
capacity.
The above process was tried on a behch pilot
plant scale* And the details about the process and the
cost calculations are given in Table
34*
Larger Scale Experiment
46.7 litres of filtered sea bittern (41.11 g
Mg/1) are diluted with 18 litres of water.
19.8 kg
sodium silicate (NagO 1 5 3 . 3 and SiOg 350.02 g /kg)
are stirred up with 50 litres of water and treated
with 18 litres of clear solution of caustic soda
prepared by dissolving
to make up to 20 litres.
2.5 leg caustic soda in water
After adding caustic soda
solution, the mixture (of s dium silicate and caustic
304
soda) is diluted to make upto 81 litres.
The dilute sea bittern is taken in a reaction
vessel and stirred vigorously with a mechanical stirrer.
The mixture of sodium silicate and caustic soda is pumped
into the reaction vessel within 10 to 20 minutes. After
the addition, the precipitate is then stirred for about
30 minutes.
The precipitate is then filtered in the
filter press and dewatered.
The cake is then repulped in
about 125 litres of water, stirred thoroughly and filtered
again.
The cake is then washed in the filter press till
the filtrate is free from chloride and sulphate ions.
The wet cake is then dried in tray type drier at 90-100°C.
The dry product is then pulverised to pass through 85 B.S.S.
about 10 kg of the dry product is obtained,
Acid consum­
ing capacity of the ignited material is 140-160 ml 0.1N
HCl/g.
Table 34
Project Cost for the manufactune of Magnpainm
Trisilicate (Pharmaceutical grade)
Capital Investment for producing 100 kg/day for 300 days
Rs.
(1)
Cost of plant and accessories
50,280
(2)
Building shed
15,000
(3)
Erection and installation
charges
(4)
Working capital
(5)
Contingencies
5,030
24,500
5,030
Total
Rs
99,840
contd...
305
Particulars
Quantity
Cost per annus
(A) Haw Materials
Rs.
(1) Sea bittern 29° Be* 1,00,000 gals
0 Rs.40/1000 gals
(2) Sodium silicate
(Na20: Si02 1:2.3)
(3) Caustic soda
4,000
65 tons
0 225/ton
14,625
8 tons
0 Rs.860/ton
6,880
25,505
(B) Utilities
(1) Electricity
(2) Steam
(3) Water
40,000 KW
0 R*0.12/ KW
4,800
450 tons
© Rs.12/ton
•
5,400
15 x 10 gals.
0 Re. 1/1000 gals •
Total
1,500
Rs. 11,700
(C) Labour
(1) Three chemists
Rs. 250 p.m.
(2) 12 skilled
bearers
Rs.
9,000
90 p.m
12,960
Total
Rs* 21,960
(0) Maintenance and
repairs 0 5/6 on plant
and equipment
2,500
(E) Depreciation on
machinery 0 10 %
5,030
(F) Depreciation on
building05#
750
(0) Interest on capital cost 0 6%
6,600
contd..«
306
Particulars
(H)
Quantity
Cost
Es
Insurance and taxes on capital
investment Q 3%
3,300
Total
A + B
•
.
Rs. 18,180
+ C + D + E + F + Gr + H
»
Rs, 7 7 ,3 4 5 ,
Total product
=
JO
=
Rs* 2578/ton
Cost of production
Equipment
tons
Specification
Cost
(approx. Rs.
(1) Solution tank
for sodium
silicate one
(2) Tank for
caustic soda
one
Stone lined
4' x 4' x 4*
u
•»
640
640
(3) Reaction vessel
with stirrer,
two
40 eft. each M.S.
with s.s, lining
14,000
(4) Filter press
two
Plate and fraae
type C.I. or
wooden
10,000
(5) Dryer, Tray
type one
s.s. trays
5,000
(6) Micro pulverriser, one
8,000
(7) Pumps (centri­
fugal), six
4,000
(8) Boiler
250 lbs of s t e a ^ h r .
8,000
Rs. 50,280~
Flow chart of the preparation of Magnesium Trisilicate
is given in the next page.
307
M A G N E S IU M S IL IC A T E
(PHARMACEUTICAL GRADE ]
SEA BITTER N 6 S 0 I
(M g 3 ° 3 / 0
PR O C E S S
A n ta c id
is
th e
m
m a g n e s iu m
p r e p a r e d
c la r if ie d
ix t u r e
s e a
s ilic a t e
p o s itio n s
s ilic a t e
th e
c
e ith e r
o f d
o s
c a u s t ic
i f f e
fr o m
s o d a
a d ju s t th e
m o l r a tio
M
p r e c ip it a te
- s ,s lim y
s ilic a t e
r e a c t io n
b itte r n
p r e p a r e d
s o d iu m
c o m
b y
o f
w ith a
fr o m
r e
n
t
s o d iu m
s o
a s
to
N a / l- 'S I Q r
is
w a s h e d t d r ie d . T h e d r y i n g
f ilt e r e d
te m p e ra ­
90 " C .
Compositioni-SlOj 48'3B; MgO 21*28, Loss on
tu re
s h o u ld
n o t e x c e e d
FgnlTton 2B-30 percent.
A tld tc n s u m in g ccrp adTy:-148 ml o f 0 - 1 N H C l/g
o f Ignited m a te r ia l
U
S
E
- -
AN A N T A C ID FO R REDUCING
G A S TR IC A C ID IT V .
CENTRAL SALTS MARINE CHEMICALS RESEARCH INSTITUTE
B H A V N A 6 A B
Photograph 10: Diagrammatic flow sheet of
magnesium trisilicate
PHO TO G RAPHY SECTION
C entral Salt f* 'V/aWns
C h e m ic a ls Res.
B
H
A
V
N
M
G
in s titu te
A
R
. - ^
308
10.2
Pharmaceutical Magnesium Trisilicate
(Li;;ht Variety)
According to the process described earlier
magnesium trisilicate is prepared by reacting soluble
magnesium salt with a mixture of sodium silicate and
caustic soda.
Magnesium trisilicate precipitate so
obtained is very slimy.
This can be filtered in plate
and frame type filter press but for making it reasonably
free from soluble impurities a minimum of six washings
are required.
Hence an alternate process based on the
reaction between magnesium hydroxide and silica sol
which obviate the need for such time consuming and hence
costly operations has been worked out.
The process
is described here in the background of factors like
preparation raw material, selection of proper reactants
etc., consideration of which has helped in overcoming
the handicaps of the earlier process*
Magnesium hydroxide required for the process
can be precipitated from magnesium chloride using either
caustic soda or slaked lime.
Though caustic soda has a.
definite advantage over lime in that it does not introduce
any contamination with calcium carbonate or calcium
sulphate in the final product, its cost would offset
this advantage and hence slaked lime is
preferred.
The slake! lime is prepared by slaking calcined lime*
slurrjring and sieving through 150 B.S. mesh screen
309
to get thick line slurry containing about 1% calcium
carbonate as the only inpurity.
When this upgraded
lime slurry is reacted with magnesium chloride, the
calcium chloride produced does not react later with
the acid solution of sodium silicate to give any in­
soluble salts and hence it is not necessary to wash
the slimy magnesium hydroxide free of soluble salts.
This makes the process practical and economic.
Fused magnesium chloride, usually contains
1?6 magnesium sulphate. As a result even prolonged
washing of magnesium trisilicate fails to wash the
precipitate free of sulphate ions.
Hence the sulphate
in fused magnesium chloride is removed by treatment
with a concentrated solution of calcium chloride*
Silica sol is prepared by reacting sodium
silicate solution with hydrochloric acid in preference
to sulphuric acid.
Sulphuric acid has the disadvantage
that excess of it would later react with calcium
chloride present in the magnesium hydroxide slurry
giving rise to calcium sulphate contamination in the
final product.
The magnesium chloride solution is treated
with the upgraded lime slurry to precipitate magnesium
hydroxide in the form of a slurry which in turn
is treated at faO - 90°C under constant stirring with
silica sol.
The granular precipitate of magnesium
tri silicate is filtered, washed and dried at a temper—
ature not exceeding 11QPC.
A distinct, advantage
of this process is that-magnesium silicate of anydesired molecular ratio MgOsSiOg c a n be obtained
by adjusting, the quantities of. magrie’siua hydroxide
and silica sol.
-- T h e characteristic-feature of .the product .
is that :(i) it is very light,
its bulk density, b e i n g
only 0*2 g/c.c as against 0.3-5 g/c.c, for- that prepared
by- the double .decomposition process and (2) the
filtration' is easy (3) magnesium hydroxide slurry does
not need .any- washing -to-make .it free from-calcium salts
prior, to- its reaction i t h
silica, sol.
This results
"in saving of time and increasing the output.
Th e
product confirms to t h e specification of Indian
fharinaeopeia (I .P.) as may be. seen in Table 35- Th.e
calcium oxide content (for. which I.P. gives no limit)
is w i t h i n :1%,,the permissible-limit given in the
■
' ! ‘
;
national formulary for magnesium hydroxide
gg
.«
This
can further be reduced by the use of better quality
of lime.
Table 3 5 . '• -Characteristics "of Magnesium Trisilicate
- prepared by sol process
Product from
. sol process
. ~ (TT~~~~
SiOg/MgOnTw)
(2)
" 27075”
J
. Limits specified
by I.P*
>
!
(5)
T T o S - 2.31
Acid absorption
ml of .05 I HCl/g- of the igni ted
material
316 ,
‘ 250
Table contd.*
311
Table contd..*
(D
(2)
(3)
Sulphate
1000 p.p.m
Chloride
Traces
Calcium oxide
2400 p.p.m
355 p »p »m
0 .8
Hot prescribed
Nil*
* when using caustic soda as precipitant.
Table 36
Project Cost for the manufacture of Magnesium
Trisilicate (light variety) 100 kg/day by
sol process
Capital Investment
Rs
(1)
Cost of plant
60,000
(2)
Building
10,000
(3)
Working capital
21,000
(4)
Erection charges
(5)
Contingency
0 10JJ on plant cost
6,000
3,000
Total
Rs 1,00,000
Cost of production! 100 kg/day for 300 days in a year
Particulars
Quantity
Cost per annua
(A) Raw materials
(1) Magnesium chloride
(2) Lime
62.4 tons
0 Rs.170/ton
10*650
12.5 tons
4,000
0 Rs.330/toa
(3) Sodium silicate
65 tons
0 Rs*225/ton
14,625
contd...
312
c o n t d ..
P a rtic u la rs -
Q u a n tity
(4 ) H y d ro c h lo ric a c id
. .
. Cost p e r annum
Rs
40 to n s
© R s.300/ton
:
1 2 , 000.
T o ta l
-Rs 4 1 ,2 7 5
(B) U t i l i t i e s
(1 ) E l e c t r i c i t y
'2 0 ,0 0 0 KW
'
2 ,4 0 0
© Rs»o. 12/KW :
(2 ) Steam
225 to n s
R s.12/ton
2 ,7 0 0
&
(3 ) W ater
' '
7 .5 x 10^ g a ls *
@ Re.I/IO O O g a l s .
750
T o ta l-
Rs
;
5,850
(C) Labour
(1 ). T hree c h e m is ts
Rs, 250 p . a .
= (2 ) 12 s k i l l e d
b e a re rs
Rs.
9 ,0 0 0
90 p.m .
.
12,960
T o ta l
Rs 2 1 ,9 6 0
(D M a in te n a n c e and
r e p a i r s © 5 % on
p l a n t .and equipm ent ,
3 ,0 0 0
(E ^ D e p re c ia tio n on-.^
m ach in ery © 10^
p la n t c o st
6 ,0 0 0
-
(F ) D e p r e c ia tio n on
. b u i l d i n g © 5%
’
500.
(G ) I n t e r e s t on w orking c a p i t a l
@ 6fe>
1,260
: (H )In su ra n c e and ta x e s on c a p i t a l
,
in v e s tm e n t @ 3% '
3 ,0 0 0
c o n td ..
.
313
A
+ B
+ C + 1) + B
+ .F- + G- + H
Total product
Cost of p r o d u c t i o n
Equipment
(1) L i m e s l a k i n g &
sieving equipment
/■
a >»
82,845 .
=
. 3 0
= Rs»
27§1.5/ ton
Specification
.
Cost
( a p p r o x . ) Rs.
.
'
700
(2) L i m e s l u r r y ' s t orage M . S . p a i n t e d
tank
with epoxy paint
d i a . 1 x » 9 (metres)
. (3) M a g n e s i u m chloride.
storage tank
(4)
tons
Reaction vessel
for p r e c i pitating
magnesium hydroxide
M.S.painted
.
with acid resistant epoxy paint
~ .dia 1J x 1,9(iaetres)l000
S.S. d i a 1 x 1 . 1
(metres)
;•
(5) H y d r o c h l o r i c a c i d
storage tank
.
.
:
600
S.S.
dia 1x.9
. (metres)
2200.
2000
(6) S o d i u m s i l i c a t e
tank
.
S.S.
d i a .1 x . 9
(metres)
2000
;
(7) S o l p r e p a r a t i o n
tank
S.S,
dia 1 x.9
.(metres)
2000
.
(8) R e a c t i o n v e s s e l !
for m a g n e s i u m
,
hydroxide & sol
(9.) F i v e ‘e l e c t r i c
motors
.
(10) S t i r r e r s , f i t t i n g
e q u i p m e n t s & "elec­
tric a c c e s s o r i e s
.
S.S. dia 1 x 1 . 9
(metres)
double jacketted
.
10000
..
2500
■ ‘
2000
contd.. .
.
314
Equipment
Specification
Cost (approx. )Rs.
(11) pumps centrifugal
six
(12) Filter press
two
(13) Drier, Tray
type one
4,000
Plate and frame
type C.I. or
wooden
10,000
5,000
s.s. trays
(14) Pulveriser,
one
(15) Boiler
8,000
250 lbs of steam/hr
Total
8,000
Rs. 60,000
The diagrammatic flow sheet of light variety of magnesium
trisilicate is given in the next page.
\
314 f\
■photograph 11: Diagrammatic flow sheet of light
variety of magnesium trisilicate
315
10.3
Preparation of Heavy Basic Magnesium Carbonate
Heavy basic Magnesium carbonate is used in
medicine as antacid and laxative, as an ingredient for
compounding bismuth lozenges and in pyrotechnic compo­
sitions.
Information on the method of production of
this chemical is very meagre.
in Thorpe's Dictionary
material.
A method has been outlined
169
3 for the preparation of the
A number of experiments performed in this
Institute in accordance with tuis procedure failed
to yield heavy basic magnesium carbonate of required
bulk density.
A systematic investigation for deternining
the conditions for the production of the chemical of
tho required quality was therefore undertaken.
Variation of the concentration of the reactants
at different temperatures at atmospheric pressure was
found inadequate to yield the desired product.
the cue from the theory put forward by Holland
Taking
170
for
the formation of the heavy magnesium carbonate,-magnesite
in nature, the employment of high pressure was consi­
dered useful for the formation of heavy basic magnesium
ciu’bonate, as pressure would be conducive to produce
a more compact material.
Accordingly preparation of
basic magnesium carbonate in a pressure vessel was
attempted and material with the required bulk density
and specification was obtained.
A double jacketted cylindrical vessel designed
for working at high pressures and fitted with a stirrer
was used as the reaction vessel.
The vessel had am
attached feeder vessel connected by a valve through
which sodium.carbonate solution.could be fed into the
reaction, vessel under pressure.
Preliminary experiments showed that at a
r
O
pressure of
2*8 kg/ cm
’
‘
and temperature of 122°C,
the addition of sodium carbonate solution 32.8
.
% w/v
to hot sea bittern containing 5.8$ magnesium w/v,gave
a product of the required density? the material was
however, unsuitable as its sulphate content.was higher
than required by specifications (*5 .per cent.SO^).
A -solution of commercial magnesium chloride on' the
other hand did not yield a product of the required
bulk density.
It was therefore felt that the presence
of sodium chloride in the bittern would be conducive
to the production of heavy carbonate. , Trials showed
that the presence of 5,.8$ w/v sodium chloride in the
magnesium,chloride solution gave basic magnesium
carbonate of required bulk density,.
It was further
found that instead of taking magnesium chloride in
the reaction vessel and adding sodium carbonate to it,
sodium carbonate solution (33 per cent) could be
advantageously taken in the reaction vessel, heated
to 132°C and maintained at a pressure of 2.S kg/ cm
and a mixture of magnesium chloride (29*05 g
and 5.8 g NaCl per 100 ml) forced into the reaction
vessel at the same pressure in'smaller quarititjesoat
a time? under this condition,the product obtained was
for 30 minutes and discharged udder pressure'V^"The ;'pfe*dl~ '
pitate was filtered under vacuum and washed with boiling
water until it was free from chloride and dried at 110°C.
The product had. a' bulk density between 35 -40 lbs/
cu.ft (.5-.7 g/c,c) and was of a higher purity than that
prescribed in British Pharmacopoeia
Table 37
171
Comparison of the purity of heavy basic
magnesium carbonate prepared with B . P .
specifications
. B.P . (1958)
Limits
...
Arsenic,p.p.m
..
Limits of laboratory
made product
2
Copper*
Absent
No blue colour
No blue colour
Iron, p.p.m
400
Trace
Calcium,$ CaO
0.7
Trace
Chloride,?S
0.0355
•
Sulphate,% S6^
.
0.0097 .
0.5
0.0321
Lead, p.p.m
10.'
Absent
Ash, %
42.45
45
Water soluble
material,^,
*
-
.
1
■
0.5
1 g of the substance in 25 ml dilute HC1 and 25 ml
water boiled to remove COg and made alkaline with
dilute NH4 0H.
318
Table 38
Project cost for the manufacture of heavy
basic magnesium carbonate (special,.grade)
(1) Cost of plant
Rs
71,000
(2) Building
20,000
(3) Working capital
16,200
(4) Erection charges
on plant cost
9 10#
7 j100
(5) Contingencies
3,500
Total
Rs*1 ,17,800
Cost of production for producing 100 kg/dav for
300 days
\
Particulars
Quantity
Cost ber annum
\
(A) Raw Materials
Rs»\
(1) Magnesium
80 tons
chloride I.S .1. 9 Rs. 300/ton
grade
(2)Soda ash
grade
24,000
I.S .1.
42 tons
9 Bs 500/ton
(3) CoffiEon salt
21,100
6.6 tons
9 Rs»35/toa
Total
231
Rs, 45,331
(B) Utilities
(1) Steam
(2) Electricity
172.32 tons
9 Rs.15/ton
2,600
34816 KW
5,200
9 9s 0.15/KW
(3) Water
1,88,800 gals
9 Rs. 2/1000 gals.
Total
377
Rs.
contd...
8,177
519
Particulars
Cost oer annum
Quantity
Rs
(C) Labour
(1) Chemist, one
Rs.400 p.m.
4,800
(2) Attendants,four
Rs. 100 p.m.
4,800
(3) Mechanie-cumfitter
Rs.150 p.m.
1,800
Total
Rs. 11,400
(D) Maintenance and
repairs 0 3# on plant
and equipment
2,130
(B) Depreciation on
machinery 0 10#
7,100
(F) Depreciation on
building 0 5%
1,000
(G) Interest on working
capital @ 9#
1,459
Total
Rs. 11,689
3*600
(H) Packing charges
A + B
+ C + D+ E+ F + G+ H
Total product per annua
♦
Cost of production
= Rs. 80,197
= 30,000 kg
80197
Rs. 2.6732
30000
Rs. 2.70/kg
Equipments cost and specifications are given in the
next page.
4) Open .pan double*
•‘ Jacke'tted. vessel
3) Compressor
2) Feeder vessel
1) Pressure vessel
Specifications
'
and provision
'
I.D 91 ems, depth 45.5 cits'
contd....
•Inner shell S.s. water Jacket m.s,
pressure
Capacity 20 eft. at 100 Ibs/sq.inch
with feeding and discharge arrangement
S.S. height 50 ems dia 38 ems. complete
gear' fitted with. & H.P. motor.
through a stiffling box and'reduction
for stirrer to run at a speed of 40 r.p.m.
inlet, condensate outlet
feeding and discharge arrangements, steam
• 46 eras and .height 61. ems-,' Complete with
•Pr. 2Q0 p.s.i 5/Design pr.100 p.s.i. Dia,.
Inner shell s*S| steam Jacket M.S. Design
,
5 ,0 0 0
,
8 000
000
12,000
.
cost approx
in Rs.
.
1
Equipment
o
CM
K\
Rs, 7 1 ,0 0 0
3 .0 0 0
n e x t page.
Plow C h art o f th e p r e p a r a t i o n o f heavy b a s ic magnesium c a r b o n a te i s g iv e n i n th e
T o ta l
2 .0 0 0
C a p a c ity to sfcavi
100 k g / day
C a p a c ity to h o ld 800 l i t r e s o f s o l u t i o n
9) S to ra g e ta n k
10) S ie v in g eq u ip m en t
5.000
S is e r a i ^ e 1 0 , o f t ,/ M i n .
8 ) Bumps
2 0 ,0 0 0
C a p a c ity t o s u p p ly 450 l b s s t e a i a / h r .
7) B o ile r
10,000
5 ,0 0 0
C a p a c ity to d ry 100 kg i n 24 h r s , a t 100°C
2M d i a . p ip e s 75 cm s, h e ig h t
o f th e r e c e i v e r 30 cms su p p o rte d on t h r e e
above th e f i l t e r i n g p l a t e , 18 cms h e ig h t
S.S.M ug f i l t e r ; c i i a 90 c*s h e ig h t 20 cms,
6 ) T ray d r i e r
5 ) .F i l t e r i n g u n i t
c o n td ...
K\
CM
i
322
H E A V M
|
B A S IC
M A G N E S IU M
C A R B O N A T E
PROCESS
I
i
flomesta fortoraft i f high bulk
density [o-5ro-7g/irfl is prepored 1
by ihe reaction between soda ash
and magnesium chloride .under I
• controlled conditions of pressure n
| [j%s kg/Sq, Cm)ond temperoSire,"
1
USED
IN
Expjosives, •
P y r o te c h n ic s
6
^
. Pharmaceuticals.
, •
■
■
T H E
IN S T IT U T E H A S P R EP AR ED
SUPPLIED' ISOO Kg.OF THIS CHEHfCAC
■ O F R E Q U IR E D
ORDNANCE
S P E C IF IC A T IO N S T O
F A C T O R IE S O F I N D I A .
CENTRAL SALT £. MARINE CHEMICALS RESEARCH IN STITU TE
BHAVNAGAR
Photograph
12 .. D i a g r a m m a t i c f l o w sheet of
h e a v y has i c m a g n e s i u m
carbonate