Note: Descriptions are shown in the official language in which they were submitted.
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Process and Device for the Reworking
of a Dilute Sulphuric Acid Solution Which Contains
Dissolved Ferrous Sulphate or a Mixture of Dissolved
Metal Sulphates Which are Mainly Ferrous Sulphate _
- 5 The invention relates to a process for the reworking of a
dilute sulphuric acid solution which contains dissolved ferrous
sulphate or a mixture of dissolved metal sulphates consisting
mainly of ferrous sulphate. The sulphuric acid solution is
concentrated to from about 40% to about 85% by weight H2SO4 (%
related to the liquid portion), thereby resulting in the
formation of a slurry of metal sulphates and sulphuric acid.
The precipitate of metal sulphates is subsequently separated
from this slurry.
The invention further relates to a device for carrying out
such a process.
Numerous variants of the above process have been described
since some chemical processes produce large amounts of dilute
sulphuric acid as by-products in which various dissolved metal
sulphates are present. Formerly these sulphuric acid solutions
... .
used to be considered as a waste product and were dumped in
public waters. This is no longer done today for reasons of
~ environmental protection. Instead, attempts have been made to
:, reprocess the sulphuric acid waste solutions in such a way that
their H2SO4 content can be reused in chemical processes. As a
~ 25 rule, this requires concentrating the dilute sulphuric acid
-~' solutions to more than about 40% by weight H2SO4. At this
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' concentration, most of the metal sulphates dissolved in the
- sulphuric acid precipitate, generally in the form of modifi-
- cations with a low content of water of crystallization. Fer-
rous sulphate for instance crystallizes as monohydrate.
For many uses of the reconcentrated sulphuric acid, these
precipitated metal sulphates - also known as "filter salt"-
need to be removed from the acid. In view of the large amounts
. of dilute sulphuric acid reprocessed this way by industry,
methods are looked for whereby only small amounts of the
valuable, reusable reconcentrated sulphuric acid adhere to the
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filter salt after filtration. Moreover, a low content of free
sulphuric acid reduces the cost of filter salt disposal since
adhering acid would either have to be neutralized before
dumping the salt or would, unprofitably, require relatively
5 large amounts of energy if the filter salt were to be thermally
decomposed for recovery of SO2 and production of sulphuric
acid. Separation of the filter salt, however, must be feasible
and reliable in a permanent operation.
For these reasons, it is often not feasible to make large-
10 scale use of the above-described processes for reconcentrating
dilute sulphuric acid solutions containing metal sulphates.
Since many operations (e.g~, titanium dioxide production)
i currently generate enormous quantities of dilute sulphuric acid
solution that have to be reprocessed, extended downtimes or
15 interruptions in the reworking process are intolerable without
providing expensive storage facilities for the sulphuric acid
solutions or throttling the production for the duration of the
trouble. In particular, when the dilute sulphuric acid
contains large amounts of dissolved ferrous sulphate, the
20 separation of the filter salt from the reconcentrated sulphuric
acid still constitutes an unsatisfactorily answered problem.
~; A known method is to use screen centrifuges for this sep-
aration. These centrifuges permit to largely free the filter
salt of adhering sulphuric acid. (Forschungsber.-Bundesminist.
25 Forsch. Technol., Technol. Forsch. Entwickl. 1984, BMFT-FB-T-
84-150). (Research report by the German Federal Ministry for
, Research and Technology, 1984, BMFT-FB-T-84-150). However,
: permanent operation of the centrifuges with the viscous, high-
specific-gravity slurry of filter salt/sulphuric acid
30 relatively frequently leads to mechanical damage to the plastic
linings of the centrifuge drums at certain spots. As these
linings serve to inhibit corrosion and as there is a risk of an
unbalanced state, such damages demand immediate repair to pre-
vent more extensive damage to the centrifuges. Repair work on
35 the centrifuge drums normally requires a new balancing of the
drums which can be performed only by a few specialized shops,
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especially so when the drums are large. Therefore repairs of
this type generally take a long time. -
t is also possible to use filters for separating the
metal sulphates in the slurry from the sulphuric acid. Pres-
sure filtration has been considered in particular because of
the high viscosities of the 40% to 85% strength reconcentrated
sulphuric acid solutions. EP-A2-133 505 published on February
; 27, 1985, for instance proposes to concentrate waste acid
derived from titanium dioxide production, i.e., a metal
sulphate-containing sulphuric acid solution of up to 28%
strength, thus obtaining a slurry of metal sulphates and 62% to
- 70% strength sulphuric acid solution, and to separate the metal
sulphates in a chamber filter press. The 62% to 70% strength
acid adhering to the filter cake can then be washed out by
means of further dilute waste acid or wash acid derived from
TiO2 production (about 8% to 10% strength sulphuric acid).
This would reduce the sulphuric acid content of the filter salt
-~ to an acceptable level. This procedure, however, implies
considerable disadvantages with regard to a trouble-free
permanent operation reworking large amounts of sulphuric acid
which contains especially ferrous sulphate. The use of a
chamber filter press for instance does generally not permit an
efficient washing operation since filtration and washing
` frequently leads to the formation of cracks in the filter cake
through which virtually the entire wash solution flows off
unutilized. If the filter salt cake contains ferrous sulphate
monohydrate, part of the monohydrate is transformed into
heptahydrate upon contact with water or dilute waste acid.
This transformation leads to a compacting and cementing of the
filter cake which is then removed only incompletely and with
difficulty from the filter chamber. Owing to the formation of
ferrous sulphate heptahydrate, moreover, the filter cloth is
often blinded during the washing procedure; in this case filter
salt separation has to be interrupted for exchanging or washing
the filter cloth. Consequently a largely smooth washing
operation cannot be warranted.
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EP-A2-194 544 published on September 17, 1986, describes a
further process for the concentration of a dilute sulphuric
acid solution which contains ferrous sulphate and other metal
sulphates. This process does not involve washing of the metal
sulphate filter cake. An acceptable level of residual H2SO4 in
the filter salt is to be achieved by blowing pressurized air
through the filter cake as received in filtration at overpres-
sure. The pressurized air blown through the cake is to expel
from its capillaries and pores as much adhering reconcentrated
acid as possible. If the H2SO4 content of the filter salt is
to be reduced in this manner by a few percentage points to
under 12% by weight, candle filters or leaf filters have to be
used which, however, require an expensive periphery in order to
function reliably over an extended period of time, as can be
taken from EP-A2-235 689, published on September 9, 1987.
Lower H2SO4 content of the filter salt cannot be achieved
in using a filter press. Even when a membrane filter press is
used and when the cake built up during pressure filtration is
squeezed at the end of the filtration at high pressure of e.g.,
16 bar or 8 bar by aid of the elastic membrane - which is
possible with this type of press - the residual H2SO4 content
of the discharged cake still comes up to 13.296 by weight or
; 12.3% by weight. In actual practice, however, (e.g., reworking
of the waste acid of a TiO2 plant) a reduction by 1% by weight
; 25 of the residual H2SO4 content in the filter salt can often mean
a saving of 500 to 1000 tons sulphuric acid of 100~6 strength
per year. Consequently residual H2SO4 contents in the filter
salt of more than 12% by weight are considered excessive as a
; rule. In addition, the high pressures at which the membrane is
pressed against the filter cake result in early wear of the
membranes, even if specific membrane materials are used. Fur-
thermore, as the filter cake is strongly compacted at pressures
above 8 bar, it is rather difficult to blow reconcentrated
sulphuric acid out of the capillaries of the cake because the
sulphuric acid solution to be expelled from the cake is highly
concentrated and therefore very viscous.
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The object of the present invention is to avoid the
shortcomings of the prior art hereinabove described and to
provide a process as mentioned in the beginning which permits
to reliably separate the filter salt from the sulphuric acid
~ 5 solution, the separated filter salt having a uniformly low
; content of free H2SO4.
It has been surprisingly discovered that the reconcen-
trated sulphuric acid solution, still remaining after filtra-
tion, in the cavities of the filter cake consisting of ferrous
sulphate monohydrate-containing filter salt, can be washed out
without compacting the filter cake or blinding the filter cloth
provided the wash liquid is a sulphuric acid solution contain-
ing from about 30% to about 35~ by weight H2SO4.
; The present invention therefore relates to a process for
- 15 the reworking of a dilute sulphuric acid solution which con-
tains dissolved ferrous sulphate or a mixture of dissolved
metal sulphates which are mainly ferrous sulphate. The sul-
- phuric acid solution is concentrated to a content of from about
40% to about 85% by weight H2SO4, (~ related to the liquid
portion), thereby resulting in the formation of a slurry of
metal sulphates and sulphuric acid. The precipitated metal
; sulphates are subsequently separated from this slurry.
The process is characterized in that:
the separation of the metal sulphates is effected by
filtration at overpressure in a membrane filter
- press, and
the filter cake formed thereby is washed, the wash liquid
being a sulphuric acid solution which contains from
about 30% to about 35% by weight H2SO4.
The invention further relates to a specific device for carrying
out this process.
The washing step using sulphuric acid solution which
; contains from about 30~ to about 35% by weight H2SO4, obviously
has the effect of suppressing the dissolution of iron sulphate
; 35 monohydrate from the filter salt cake and the precipitation of
the corresponding heptahydrate from the wash liquid in the
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filter cake and filter cloth. Consequently the filter cake is
-not compacted during washing and the filter cloth is blinded
only to the small extent as would be the case if washing non-
ferrous metal sulphates. This means that the metal sulphates
can largely be separated from the slurry without difficulty.
This considerably facilitates reducing the amount of free
sulphuric acid in the filter salt in an industrial-scale
operation. It is now possible to separate filter salt
containing large amounts of ferrous sulphate monohydrate by
using low-maintenance membrane filter presses instead of
centrifuges, at operating conditions which permit a permanent
operation without excessive wear, and to reach at the same time
residual H2SO4 contents in the filter salt of less than 10% by
weight.
15If the reconcentrated sulphuric acid solution adhering to
; the filter salt is expelled virtually completely by the 30% to
35% strength sulphuric acid wash solution, a residual H2SO4
content of 8% by weight or even less can be achieved.
Membrane filter presses as used in the process of the
present invention generally consist of several filter plates,
like simple chamber filter presses. In the membrane filter
press, however, each of the usual chamber filter plates is
doubled by a neighbouring filter plate to which an inflatable
membrane is affixed in such a way that the membrane when under
pressure is pressed against the filter cake in the filter
chamber to compress the cake uniformly vertically to the cake
surface.
These filter presses readily handle slurries with a solids
content up to about 50~ by weight. Therefore, membrane filtert 30 presses are suitable for all applications of the process of the
instant invention in actual practice.
,~It is a particular advantage of the membrane filter
presses that they permit rapid and efficient washing of the
filter cake using only small amounts of wash liquid. The
presses are operated in batches, a filtration cycle normally
consisting of the following steps:
1) Fill the filter chambers with slurry and allow a filter
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cake to build up.
2) Squeeze the filter cake. 7'
3) Wash the filter cake.
4) Press the washed filter cake.
5) Blow compressed air through the washed filter cake.
6) Discharge the cake from the filter press.
Pressure filtration covers step 1 and optionally step 2.
; The process of the present invention preferably uses all steps
- listed above in the order given for separating the precipitated
filter salt from the reconcentrated sulphuric acid, but steps
2, 4 and 5 need not all be carried through necessarily.
Compression of the filtered material prior to the washing
operation compacts the filter cake and, especially if the lat-
ter shows cracks, gaps or similar structural defects, homo-
genizes it in such a way that the cake throughout its surface
has pores of nearly the same size and capillaries with very
- similar diameters. In the subsequent washing procedure,
therefore, the filter cake at all points develops essentially
} the same resistance to the wash liquid, and the wash liquid
. 20 therefore does not shortcircuit through larger cracks or chan-
. nels in the cake in which case the cake would not be washed
~, effectively.
`~ This holds good also for the filter cakes of all subse-
quent filtrations of slurry batches if the conditions are not
,.'J ~5 changed. Therefore all filter cakes come into contact with
virtually the same amount of wash liquid, resulting in a uni-
formly washed-out filter salt. Moreover, squeezing of the
filter cake reduces its moisture content (or increases its
solids content). Consequently, lower quantities of 30% to 35% `~
. 30 strength sulphuric acid are required in the subsequent washing
step to expel the smaller quantity of 40% to 85% strength sul-
phuric acid solution from the cake. This in turn means a
shortened washing operation.
When carrying through the process of the present inven-
35 tion, the pressure must not be too high in squeezing the filter
cake before the washing. Excessive pressure would not only
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; overburden the membranes in the long run, but would compact
and drain the filter salt material too much. As a consequence,
the filter cake would not be sufficiently permeable for the
wash liquid to pass through. No more washing could then be
realized. As a rule, the pressure at which the membrane is
pressed against the filter cake should range below 8 bar and
pressing time should be 5 minutes at most. In many cases, a
short squeezing for say 1 minute at a pressure of 5 bar will be
sufficient to develop an appropriate structure of the filter
salt cake. The optimal pressing conditions naturally are also
dependent on the composition of the filtered material, on its
- mean particle size and on the concentration of the sulphuric
acid solution to be expelled; this concentration considerably
; affects the viscosity of the solution. If necessary, the
optimal pressing condition can readily be determined by the
~; expert in two or three scouting experiments.
The wash liquid for washing the filter cake is an aqueous
sulphuric acid solution containing 30% to 35% by weight H2SO4.
, Sulphuric acid solutions with more than 35% by weight H2SO4 are
also usable in general as they show the same behaviour towards
~^ the filter cake in the washing operation as do the 30% to 35%
solutions. Their wash-out effect, however, is low, particu-
larly if low-concentration sulphuric acid solutions are washed
out of the filter cake.
The wash liquid may contain metal sulphates, e.g. ferrous,
aluminum-, magnesium- and other sulphates and in addition,
small amounts of chromium sulphate or vanadium sulphate.
` There are two different ways of feeding the wash liquid to
the filter cake in the press, viz. either through the slurry
feed channel of the membrane filter press, i.e., the channel
through which the slurry was previously fed to the filter
~ chambers, or through the wash channel. The wash channel (which
-~ may also serve other purposes in other steps of the filtration
cycle) passes wash liquid only to those filter plates equipped
with membranes. The wash liquid is admitted between the-
possibly inflated - membrane and the filter cake and is dis-
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tributed all over the filter cake surface to come out at the
opposite side of the filter cake. The wash filtrate is dis-
charged via the filter cloth. Washing by admitting the liquid
via the wash channel is preferred because it results in a par-
ticularly uniform contact of the filter cake with the washliquid.
The 40% to 85~ strength sulphuric acid solution filling
the cavities of the filter cake before the washing operation is
slowly expelled from the cake, viz. to the extent that the 30%
to 35~ strength sulphuric acid wash liquid is forced through
the cake. The wash filtrate obtained therefore consists
initially of the same 40% to 85% strength sulphuric acid
solution as the filtrate obtained in separating the filter salt
from the slurry, which separation was performed before the
washing. These filtrates should preferably be united.
While the concentrated acid is being expelled, the two
sulphuric acid solutions of different concentrations slightly
~ mix with each other at their contact areas so that the concen-
- tration of the sulphuric acid ln a more or less thick layer
drops from the level of the concentrated solution to the level
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of the wash liquid. Once the sulphuric acid solution of this
layer comes out of the filter cake, the sulphuric acid concen-
tration of the filtrate drops relatively rapidly. From a
certain moment onward it may therefore often be advisable to
stop uniting the filtrate with that recovered initially. This
stop is effected preferably when the sulphuric acid concentra-
`~ tion of the filtrate has not yet dropped by more than 5% by
weight, optimally by less than 1% by weight from its initial
level. The desired point can be determined by current - op-
tionally automatic - measurement of the sulphuric acid con-
centration in the filtrate. In routine cases with unmodified
process parameters, one may once measure the period from the
moment washing begins till the suitable point is reached and
then proceed with the subsequent batches by regularly beginning
to separate the wash filtrate from the slurry filtrate after
these intervals.
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The washed filter cake may additionally be pressed if
necessary, and/or compressed air may be blown through it to
reduce its moisture content. The cavities of the washed filter
cake contain an essentially more dilute sulphuric acid solution
than the cake obtained after filtration. And if the filter
cake is washed through long enough, it will contain only the
wash liquid with 30% to 35% by weight H2SO4.
As the viscosity of sulphuric acid solutions strongly
decreases with declining concentration, the more dilute sul-
phuric acid is much more readily blown out of the washed filter
. .
cake by means of compressed air than the relatively concen-
trated acid adhering to the cake immediately after filtration.
This "blowing dry" which serves to expel moisture from the
cake, therefore removes more moisture from the washed filter
cake and effects a higher solids content than it would if the
'` filter cake had been left as obtained upon filtration. A
filter salt with roughly 29% residual moisture (71% solids) is
~ obtained for instance if 5 bar air is blown for 10 minutes
:'~! through a filter cake separated from a metal sulphate/sulphuric
acid slurry with 66.5% by weight H2SO4 obtained according to
the present invention; and a filter salt with only 22% residual
moisture (78~ solids) is obtained if the same filter cake is
previously washed with a 33% by weight sulphuric acid solution
so intensively that the sulphuric acid left in the cake cavi-
ties has an average concentration of not more than about 50% by
'; weight H2SO4, and if compressed air is blown through the washed
-~ cake under the same conditions as mentioned above. The washed
filter cake is blown dry preferably with compressed air of 3 to
6 bar applied for 10 to 15 minutes. The residual content of
` 30 free H2SO4 in the separated metal sulphates should then pre-
ferably be at least less than 10% by weight.
In a particularly favourable embodiment of the present
invention the dilute sulphuric acid solution is concentrated in
several steps, concentration being designed in such a way that
in one of the steps the sulphuric acid solution is concentrated
up to an H2SO4 content of 30% to 35% by weight. Part of this
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30% to 35% sulphuric acid solution is branched off and used as
wash liquid.
In concentrating the dilute sulphuric acid solution, it is
advisable to proceed as follows: in a first step evaporate the
acid solution to 26% to 29% by weight H2SO4 and then cool it
down to a temperature of 10 to 25 C. As a result of the
cooling, part of the metal sulphates dissolved in the sulphuric
acid precipitate in a form rich in water of crystallization
` (e.g., FeSO4.7H2O, MgSO4.7H2O). The high content of crystal-
lization water in these metal sulphate modifications effects a
further concentration of the 26% to 29% sulphuric acid solution
to a content of 30% to 35% by weight H2SO4. After separation
of the precipitate from the sulphuric acid solution, the latter
is used as wash liquid according to the present invention.
In a specific embodiment of the process of this invention,
the filtrate obtained at the beginning of the washing treatment
is united with the filtrate obtained in the filtration of the
metal sulphate/sulphuric acid slurry, for as long as the H2SO4
contents of both filtrates do not yet much differ from each
other (e.g., by less than 5% by weight). In this procedure,
the remainder of the first-mentioned filtrate whose H2SO4
content naturally equals at least that of the wash liquid, is
returned, preferably wholly, to the concentration step.
-~ The process of the present invention is particularly suit-
^ 25 able for the reworking of dilute waste acid that is derived
~` from titanium dioxide production by the sulphate route using
specifically ilmenite feedstock material. This dilute waste
acid is concentrated up to 50% to 75~ by weight H2SO4, related
to the liquid. In this specific case it is particularly
beneficial to combine the process steps as described in the
claims. -
The resulting reconcentrated sulphuric acid solution can
profitably be reused for the digestion of titaniferous feed-
stock material in the sulphate process. If titanium dioxide
pigment of particularly high quality is to be produced in this
;~ way from the digested material, the percentage of metal ions
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adversely affecting the pigment properties (e.g., chromium and
especially vanadium) should be minimized in the digestion
mixture. A sufficient amount of the adverse metal ions that
originate from contaminations of the titaniferous feedstock are
normally discharged in the sulphate process as sulphates via
the dilute waste acid and in the subsequent dilute acid recon-
centration process via the filter salt. Therefore, care should
be taken to ensure that a sufficiently large amount of detri-
mental metal sulphates is discharged in the overall process and
that these sulphates do not accumulate in the recycled sul-
phuric acid, especially so in continual reconcentration of the
dilute waste acid from TiO2 pigment production and in recycling
of the reconcentrated sulphuric acid obtained in the process of
this invention.
If therefore the main part or all of the dilute wash fil-
trate is returned to the reconcentration stage in the process
; of this inventlon, the filter salt must be washed only to the
extent that the percentage of detrimental metal sulphates
eluted from the filter salt into the wash filtrate is small
enough not yet to impair the titanium dioxide hydrate precip-
itation. If necessary, one has to reduce the quantity of wash
liquid or the duration of the washing treatment and tolerate a
` somewhat higher loss of sulphuric acid not washed out of the
filter salt. In turn, a somewhat better capacity of the plant
is obtained. It should be noted that the sulphuric acid wash
liquid used in the process of this invention and preconcen-
trated to an H2S04 content of 30~ to 35~ by weight, less tends
` to elute metal sulphates from the filter cake owing to its
higher sulphate concentration than prior art wash liquid or
~, 30 untreated waste acids would do.
The filter salt separated according to this invention is
particularly suitable for the recovery of S02 by thermal decom-
position due to its low content of free H2S04 and residual
moisture.
A particularly suitable device for carrying through the
process of the present invention comprises:
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a) a first group of structural elements for concentrating the
- dilute sulphuric acid solution up to an H2SO4 content of
30~ to 35~ by weight;
b) a second group of structural elements for further concen-
trating this preconcentrated solution to produce a slurry
of metal sulphates and sulphuric acid with an H2SO4 con-
tent of 40~ to 85~ by weight, related to the liquid por-
tion;
c) at least one membrane filter press; and
d) means to remove the filtered solids and the filtrate from
the membrane filter press(es).
In this device, the first group of structural elements has
its discharge end connected with the feed end of the second
group of structural elements, via conveying means for the 30%
to 35% sulphuric acid solution. The discharge end of this
latter group is connected, via conveying means for the slurry
of metal sulphates/sulphuric acid, with the feed end of the
membrane filter press(es).
.i~! The device according to the invention is characterized in
that it comprises additional conveying means for the 30% to 35~
- sulphuric acid solution through which the first group of struc-
"3 tural elements can bypass the second group of structural ele-
q ments to discharge directly into the feed end of the slurry
',! feed channel and/or the wash channel of the membrane filter
press(es), and that the discharge end(s) of the membrane filter
press(es) can be connected with the feed end of the second
group of structural elements through additional conveying means
for returning the filtrate. This device provides, in a partic-
ularly simple way, suitable wash liquid for the washing proced-
ure according to this invention. When the H2SO4 content of the
wash filtrate discharged from the membrane filter press drops
to an inacceptably low value during or after the washing pro-
cedure, this filtrate whose H2SO4 content is naturally higher
than 30~ to 35%, may be passed to the second concentration
stage to replace previously withdrawn wash liquid.
The two groups of structural elements for the concen-
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- 14 -
tration section of the device may be made up in any way
appearing appropriate to one skilled in the art.
The first structural group for instance may consist of one
or several scrub towers (e.g., venturi scrubbers) in which the
initial solution is preconcentrated by means of hot exhaust
gases. In many cases it is appropriate to install a cooling
crystallization unit upstream of the scrubber and a filter to
separate metal sulphates rich in water of crystallization,
especially FeSO4.7H2O, since their separation enables an inex-
pensive further concentration of the sulphuric acid solution to
the desired H2SO4 content of 30~ to 35% by weight. Another
specific design of the first structural group can be taken from
Canadian Patent Application No. 581,141 of the Applicant, whose
disclosure is hereby referred to.
~ 15 The second structural group in which the preconcentrated
;;~ 30% to 35% sulphuric acid solution is further concentrated
thereby forming a slurry of metal sulphates and sulphuric acid
solution with an H2SO4 content of 40~ to 85% by weight, may
^ consist for instance of a multi-stage vacuum circulation evap-
~ 20 orator. The evaporator may be followed by a cooler or heat
`~ exchanger to recover waste heat, and/or by an agitated-vessel
cascade in which the precipitated metal sulphate crystals may
"mature" to adjust the particle size range best suited for
separation in the membrane filter press.
- 25 "Conveying means" are understood to be any means that one
` skilled in the art considers suitable for conveying sulphuric
`~ acid solutions or slurries of the defined H2SO4 contents
~, between the parts of the devices mentioned. These means com-
prise for example piping and pumps.
~; 30 If necessary, a device has to be provided additionally for
i removing sulphuric acid fumes from the exhaust air resulting
from dry-blowing the filter cake in the membrane filter press.
The invention is illustrated by, but not limited by, the
following Examples.
EXAMPLE 1
~ A waste acid as obtained in the production of titanium
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dioxide by the sulphate route using ilmenite feedstock, was
; reprocessed by the process of this invention. The waste acid
had the following composition:
:
Constituents % by weight
FeSO4 11.00
MgSO4 2.33
TiOS04 0.87
A12(SO4)3 0.25
MnS04 0 .1 9
VOSO4 0.13
CaSO4 0.10
Cr2(SO4)3 0.08
2S4 22.90
H2O/trace elements balance -
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The slurry of sulphuric acid solution and precipitated
metal sulphates had an H2SO4 content of 66.5% by weight, re-
` lated to the liquid. the particle diameter of the salts es-
sentially ranged between 10 and 30 microns (determined under
the microscope).
a) (Comparison) 5 Kg of the slurry of roughly 50 C were
, filtered in a membrane filter press consisting of one
chamber and having a filter area of 200 x 220 mm, the
slurry being fed to the filter chamber at a pressure of 5
bar. After 30 seconds, the filter cake was compressed for
roughly one minute at a pressure of 5 bar. Cake thickness
was 20 mm, residual moisture 40.7% by weight (correspond-
ing to only 59.3% by weight solids). The filter cake con-
tained 27.1% free H2SO4.
~ b) (Comparison) Procedure as described under a). After com-
- 30 pression, however, 5 bar air was blown for 10 minutes
through the filter cake. The residual moisture of the
cake was 28.9% by weight (71.1% by weight solids). The
H2SO4 content in the cake was analyzed to amount to 19.6%.
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- 16 -
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Owing to the different partial vapour pressures of water
and H2SO4, the H2SO4 concentration in the sulphuric acid
solution adhering to the cake had risen to 67.8% by weight
after through-blowing.
c) Procedure as under a). After filtration, however, the
filter cake was washed with 0.25 litres of dilute waste
acid preconcentrated to 33% by weight H2SO4 of 20 C. Sub-
sequently, 5 bar air was again blown through the cake for
; 10 minutes. Residual moisture of the cake was 24.6% by
weight (75.4% by weight solids). Residual H2SO4 content
` was 14.6% by weight.
d) Procedure was equal to that described under c). However,
0.5 litre of the 33% sulphuric acid solution was used for
washing the filter cake. Residual moisture of the cake
was 23.3% by weight (76.7% by weight solids). The analy-
- sis of the H2SO4 content in the cake showed 13.2% by
weight.
e) The experimental parameters were the same as in c) above.
` The filter cake, however, was washed with 1.5 litres of
the same wash liquid. The residual cake moisture was
21.9% by weight (78.1% by weight solids) at 10% weight
H2SO4 content. This corresponds to an H2SO4 concentra-
tion in the sulphuric acid solution in the cake of 45.7%
~' by weight.
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EXAMPLE 2
The same procedure was used as described in Example 1.
The slurry obtained in concentrating the waste acid, however,
was allowed to mature for a short while before the metal
sulphates were separated. Hence, their particle size was
slightly larger than in Example 1.
a) (Comparison) The experimental parameters equalled those of
Example lb). The residual moisture of the filter salt was
only 23.5% by weight (76.5% by weight solids). The analy-
; sis of free H2SO4 showed a residual content of 15.6% by
, 35 weight (corresponding to 66.6% by weight H2SO4 concentra-
tion in the sulphuric acid adhering to the filter salt).
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b) Experimental conditions were the same as in a) above. But
the cake was washed with 1 litre of waste acid preconcen-
trated to 33% by weight H2SO4. The filter salt cake then
contained 19.6% by weight residual moisture and 8.8% by
weight H2SO4.
EXAMPLE 3
In this Example the particle size of the metal sulphates
to be separated from the slurry essentially ranged between 15
and 70 microns. The H2SO4 content of the slurry was 65.2% by
` 10 weight related to liquid.
a) (Comparison) The other experimental conditions were the
same as in Example lb). The separated metal sulphates had
-~ a residual moisture content of 19.8% by weight. The con-
tent of adhering free H2SO4 was 13% by weight. The H2SO4
concentration in the adhering acid was therefore 65.7% by
weight.
- b) In modifying Experiment a), the filter cake was first
washed with 0.75 litre of the waste acid preconcentrated
to 33% by weight. The residual moisture in the cake was
17% by weight with an H2SO4 content of 8.3% by weight. ~
c) Washing with 1 litre preconcentrated acid, with the other :
parameters remaining the same as in b) above, resulted in
a filter salt with 17~i residual moisture and 8.0% by
~ weight free H2SO4.
'Ji 25 EXAMPLE 4
In an experiment close to actual production practice,
~ waste acid containing ferrous sulphate and obtained in the ;
!.,titanium dioxide production from ilmenite feedstock, was first ;
preconcentrated in several steps to 32% to 33% by weight H2SO4.
30Solids were then separated from the acid. A small part of this
preconcentrated waste acid was used as wash liquid. The major-
ity was further concentrated until the H2SO4 content of the
resulting slurry of sulphuric acid solution and metal sulphates
(chiefly ferrous sulphate monohydrate) was 68% to 70% by
weight, related to liquid.
These metal sulphates were separated from the slurry using
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- 18 -
a membrane filter press. The filter press had two chambers/
- each 50 mm deep, and a total filter area of 4.5 m2. The mem-
branes were made of rubber.
The Table on pages 19 and 20 gives a survey of these ex-
periments. In Experiments 4a to 4f the filter salt cake waswashed according to the present invention. In Experiments 4a
- to 4c wash liquid was fed via the slurry channel and also via
the wash liquid channel whereas in Experiments 4d to 4f the
wash liquid was fed only via the wash liquid channel. In
Experlments 4g to 4i the filter salt was not washed for
comparlson.
None of the experiments using filter salt washing showed a
compaction of the cake or blinding of the filter cloth as a
result of washing.
15Line #15 of the Table shows that the H2SO4 content of the
filter salt cake could readily be reduced by more than 50%.
The vanadium content of the filter salt could be kept at the
same level as would be obtained without filter salt washing
(cf. especially Experiments 4d to 4i, line #17). Hence, the i
. 20 adverse metal ions need not be suspected to markedly accumu-
late in the reconcentrated sulphuric acid as a result of re- -~
turning the wash filtrate to the concentration stage.
. If not otherwise stated, "%" in this text and table means
percent by weight (% by weight).
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