Note: Descriptions are shown in the official language in which they were submitted.
4X
This invention relates to a process for the recovery of indium and
tin and, more particularly, to a metallurgical process -for separately recovering
indium and tin from metallurgical intermediate products.
ln the processing of complex sulfide ores and concentrates for the
recovery of primary metals such as lead, zinc and copper, intermediate products
are formed which may contain indium and tin, as well as many other elements
such as zinc, lead, copper, iron, arsenic, antimony, cadmium, bismuth, silver
and gold. Such intermediate products include flotation concentrates and
tailings, slags, fumes, drosses, residues and electrolytic slimes. Where
indium and tin values are sufficient to warrant recovery, a recovery process
demands the separation of these metals from the other metals, either dircctly
or from secondary concentrates.
The recovery of indium and tin from intermediate products obtained in
the processing of complex lead-zinc concentrates has heretofore been accom-
plished by any of a number of methods alone and in combination, such as
chloridizing or sulfating, roasting, fuming, acid leaching, caustic fusion,
precipitation as phosphate or stannate, and elec-trolysis. According to United
States patent 2,052,387, which issued August 25, 1936, indium-bearing material
is subjected to roasting or blast furnace treatment and the resulting indium-
containing product is leached with sulfuric acidO 'I'he indium is precipitated
as indium hydroxide by neutralization of the resulting solution with zinc
oxide. The indium precipitate is rcdissolved and the indium is reprecipitated
as indium sulfide. Impurities such as copper, arsenic, antimony and tin co-
precipitate with the sulfide and can be removed from the sulfide by leaching
the precipitate with sodium hydroxide.
According to United States patent 2,12~,180, which issued July 19,
1938, metallic tin is removed from lead alloys by treatment with molten caustic
soda and the spent reagent containing sodium stannate is reacted with calcium
- 1 - ~'
s
hydroxide at room temperature to form insoluble calcium stannate.
According to United States patent 2,241,438, which issued May 13,
1941, lead sulfate residue containing indium is leached with acid~ indium in
the leach solution is precipitated as indium phosphate and the phosphate is
converted to the hydroxide, which is roasted and reduced with hydrogen to
yield indium metal.
In United States patent 2,384,610, which issued September 11, 1942,
there is disclosed a method for recovering indium lrom material containing
zinc, iron, aluminum and arsenic. The material is leached with dilute sulfuric
acid to dissolve zinc, the leach residue is leached in strong acid, indium is
precipitated, the precipitate is treated with alkali to dissolve aluminum, the
residue is dissolved in sulfuric acid, indium is sponged with zinc, the sponge
is dissolved and the solution is electrolyzed to recover indium.
In United States patent 2,586,649, which issued February 19, 1952,
there is disclosed a methGd for the recovery of indium from an acidic solution
containing indium, arsenic, cadmium, zincJ iron and lead by precipitating
indium as indium arsenate, converting the arsenate to hydroxide with caustic,
dissolving the hydroxide in acid and recovering indium, or igniting the
hydroxide to form indium oxide. These prior art processes have the disadvan-
tage of being complex and having many steps involving a number of intermediate
compounds beEore the indium and/or tin are rccovered.
It has now becn ~ound that inclium and tin can be readily and sepa-
rately recovered in a concentrated Eorm from metallurgical oxiclic and sulfatic
intermediate products by subjecting material to treatments with sodi~ml hydroxide
(caustic soda) or potassium hydroxide (caustic potash). More particularly, it
has been found that by subjecting intermediate products to a leach with sodium
hydroxide or potassium hydroxide solu-tion and subjecting the Leach residue to
a fusion with caustic soda or caustic potash, indium and tin can be eEfectively
L4~4S
separated from each other and from metals such as lead, zinc and arsenic. The
process of the invention can be carried out by using either sodium hydroxide
or potassium hydroxide, and with equal results. The use of sodium hydroxide
is preerred for economic reasons. The two hydroxides will be re-ferred to
hereinafter as caustic.
Accordingly, there is provided a process for the separate recovery
of indium and tin from indium- and tin-bearing materials in oxidic or sulEatic
form and including fumes and flue dusts which process comprises the steps oE
leaching said materials with a solution of caustic; subjecting th0 leach
residue to a fusion with solid caustic; leaching the fusion product with
water; recovering the water-leach residue as an indium concentrate; treating
the water-leach solution with calcium hydroxide and recovering a concentrate
containing tin as calciunt hexa-hydroxo stannate. According to a second embodi-
ment of the process of the invention, there is provided a process for separate
recovery of indium and tin from metallurgical intermediate products containing
tin, indium, lead, ~inc, copper, iron, antimony, bismuth and arsenic which
process comprises the steps of subjecting said products to a fuming operation
to obtain a -fume or flue dust; leaching said fume or flue dust in a caustic
leach with a solution of caustic to dissolve at least a portion of the lead,
zinc and arsenic in a leach solution and to provide a leach residue containing
tin and indium; subjccting said leach residue to a fusion with solid caustic
to convcrt said tin to a soluble stannate; leaching the fusion product with
water to substantially dissolve said solubLe stannate and any residual lead,
zinc and antimony in a water lea~h solution leaving an insoluble indium
containing concentrate; separating the indium-containing concentrate from said
water leach solution; adding calcium hydroxide to said water leach solution to
substantially precipitate said tin as calcium hexa-hydroxo stannate; recovering
the precipitated tin from the residual solution as calcium hexa-hydroxo stan-
nate; and returning residual solution to said caustic leach.
Preferably, the fuming operation is carried out at about lO00 to
1~00C in the presence of a reductant and an added sul:Eide; the caustic leach
is carried out at a temperature in the range of from about 15C to the boiling
point of the solution in a two-stage countercurrent leach with a caustic
solution containing about 200 g/L caustic; the fusion is carried out at a
temperature in the range ot about ~00 to 800C with an amoun-t oE solid caustic
about two to three times the amount of leach residue; the leaching with water
is carried out at below about 80C; and the water leach solution is treated at
about 50 C with lime slurry to substantially quantitatively precipitate tin as
calcium hexa-hydroxo stannate.
The invention will now be described in detail with reference to the
accompanying flow sheet.
Metallurgical intermediate products that can be treated in the
process of the present invention are flotation concentrates, flotation tailings,
fumes, flue dusts, slags, drosses, leach residues and electrolytic slimes
which are obtained in the processing of ores and concentrates for the recovery
of metals such as zinc, lead and copper. Fumes, leach residues and flue dusts
can usually be treated directly in a caustic leach, generally indicated at 1
while flotation concentrates and tailings, slags, drosses and electrolytic
slimes must be converted into an oxidic or sulfatic Eorm whlch is suitable Eor
leaching with caust:ic. Conversion may be accomplished by a pyrometalLurgical
treatment such as a :Euming, oxidation, or sulEating operation~ whereby at
least a portion oE the metals containcd in the Elotation concentrates and
tailings, slags, drosses, and electrolytic slimes become available in a caustic
leachable Eorm, such as an oxicle fume or Elue dust. For example, when drosses
and slags are submitted to a fuming operation 2, shown with interrupted lines,
in a ~urnace or converter, at temperatures in the range oE about 1000 to
~140~5
1400 C, major portions of the indium and the tin report in the fume emanating
from the furnace or converter. Major portions of other metals such as lead,
zinc, antimony, arsenic and cadmium are also volatilized and report in the
fume. The fuming operation is preferably carried out at temperatures in the
range of about 1000 to 1~00C and in the presence of an added recluctant such
as, for example, carbon monoxide, hydrogen, coal, or coke. The addition of a
sulfide, such as for example pyrrhotite, enhances the volatilization of indium
and particularly that of tin. The fumed slag or dross, which may contain
copper, iron, silica and lime, is removed from the furnace.
Fumes, flue dusts and leach residues are fed and subjected to a
caustic leach, generally indicated at 1, with a solution of caustic. In the
caustic leach 1, metals such as lead, zinc and arsenic will dissolve as metal-
lates and form a leach solution, while indium and tin as well as antimony
remain mainly in the leach residue. The leach is carried out at temperatures
in the range of from about 15C to the boiling point of the solution at atmos-
pheric pressure and preferably at a temperature of about 95C. The caustic
solution which is added to the leach, and which may be a recycled solution,
may contain caustic in the range of about 50 to 200 g/L. The weight ratio
between the amounts of caustic and the fumes, flue dusts and residues will
vary depending on the composition of the Eeed to the leach and is typically
about 2:1. A retention time in the range oE about. one to Eour hours is usually
sufficient Eor the completion of the leach.
The caustlc leach may be carried out in one or more stages. The
leach is preferably carried out as a two-stage countercurrent leach as shown
in the flowsheet. In this countercurrent leach, fume, residue or flue dust is
reacted in the first stage caustic leach 3 witll caustic solution from the
liquid-solids separation 6, to be described, following the second stage caustic
leach 5. Additional caustic solution from liquid-solids separation 11, to be
4~
described, may also be added as indicated by the broken line. The reaction
mixture from the first stage leach is subjected to a liquid-solids separation
. The liquid fraction is a caustic solution which contains at leas~ a portion
of the arsenic, lead, zinc and traces of tin contained in the feed to the
leach. This solution is removed from the process and may be treated further
for the recovery of metal values. The first leach residue from separation
is subjected to the second stage caustic leach 5. Caustic in the form of
recycled residual caustic solution is added. To make up the desired caustic
to solids ratio in the leach, additional caustic may be added, either to the
first leach 3 or the second leach 5, as desired. The reaction mixture from
the second stage leach 5 is subjected to a liquid-solids separation 6. The
liquid fraction from separation 6 is passed to the first stage leach 3 and the
solids fraction is passed to caustic fusion 7. The first stage of the counter-
current leach is preferably carried out at temperatures between about 15 C and
the boiling point and the second stage at between about 80C and the boiling
point of the solution at atmospheric pressure. Most preferably, both stages
are conducted at a temperature of about 95C, and for a period of time of
about one to two hours for each stage.
In caustic fusion 7, the solids residue from separation 6 is fused
with solid caustic at a temperature in the range of about ~00 to 800C, typi-
cally about 650C. The f-usion results in the formation of a soluble stannate,
i.e. potassium or sodium stannate, whlch is dissoLved in a subsequcllt leach.
Prior to the Fusion, the tin (which is mainly oxicle) remains refractory and
for thc most part insoluble in caustic solution. The amount of solid caustic
used in the fusion is determined by the composition of the solids from sepa-
ration 6, especiaLly of course the amount of tin, and is typically about two
to three times the amount by weight of the solids residue. This amount of
caustic represents the major input of caustic into the process. This caustic
045
passes through the remainder of the process and is ultimately recycled to the
caustic leach 1. The balance of caustic in the process is maintained by
adding additional caustic directly to the caustic leach as described. The
fusion requires that the material be maintained in the temperature range
specified above for the period of a~out one to two hours.
The fused material Erom fusion 7 is subjected to a water leach 8 to
dissolve the soluble stannate. Because the solubility of the stannate decreases
with increasing caustic concentration in the leach solution and with increasing
temperature, the water leach is advantageously carried out at temperatures
below about 80C, pret'erably below about 50C. Any remaining lead and zinc
are also dissolved in leach 8. A retention time in the range of about one to
two hours is normally sufficient to complete the water leach. The leach
mixture is subjected to a liquid-solids separation 9.
The solids fraction from separation 9 is a concentrate containing
the indium. The indium in this concentrate represents normally at least 90%
; of the indium entering the process. The major associated impurity is antimony
as the antimonate. This concentrate may be further treated by any one of a
number of known methods such as leaching with acid and an oxidant followed by
precipitation of indium as sulfide, or by solvent extraction of indium.
The leach solution from separation 9 is treated for the recovery of
tin in tin precipitation 10. Treatment of the solution at a temperature of
about 50C with calcium hydroxide, containing a slight excess, for example a
10-30% mo]ar excess, Oe calcium with respect to tin in the solution~ results
in the precipitation Oe calcium hexa-hydroxo stannate. This precipitation is
both selective and substantially qucultitative. 'I'he precipitate is separated
from solution in liquid-solids separation 11. The solids Eraction is CaSn(OH)6,
which can be readily treated Eor the recovery of tin. The solution is a
caustic solution which is recycled to the caustic leach 1, or in the case oE a
:~2~4(~
two-stage countercurrent leach, to the second caustic leach 5. If desired, a
portion of the caustic solution recycled to leach 5 may be fed to the first
caustic leach 3. The calcium stannate, which usually contains less than 1%
each of Pb, Zn, As and Sb is recovered. The overall recovery of tin is usually
in the range of about 80 to 90%.
The liquid-solids separations in the process may be carried out by
any of a number of known procedures, such as settling, filtrating and centri-
fuging. Separation of solids from liquid is normally readily accomplished by
settling and/or filtration.
The invention will now be illustrated by means of the following non-
limitative examples.
Example 1
This example shows that a slag from retreatment of lead dross can be
fumed to provide a material amenable to treatment for the recovery of indium
and tin.
Three 50 g portions of slag were each placed in a crucible along
with 5, 10 and 15 g of iron sulfide concentrate ~mostly pyrrhotite), respec-
tively. Each charge was placed in a muffle furnace and a cap assembly was
positioned. An inert atmosphere was maintained by admitting nitrogen gas at a
rate of one L/min during the heating period. The reaction was carried out
under reducing conditions at 1260C by replacing the Elow of nitrogen with
carbon monoxide for 100 minutes. At the end of the period, the gas flow was
turned off and; a~ter cooling, the entire crucible cmd reactlon products were
ground to a fine homogeneous mixture for analyses.
The copper, silica and lime remained substantially in the residual
slag, while the zlnc, arsenic and antimony, tinl and lead reported substan-
tially to the fume. The indiwn divides between the slag remaining and the
fume.
~L2~ S
The initial slag composition was determined. The residua]. slag and
the fume were ana:Lysed for tin, indium and lead, and the distributions between
the residual slag and the fume determined. The analyses are given in Table
IA, and the deportments in Table IB.
TABLE IA
Slag Composition In Percentages
Sn In Yb Zn Fe Cu Sb As Si.O CaO
8.7 2.4 33.8 4.3 10.5 8.4 1.6 1.6 9.4 1.1
FeS* F:inal Weight Fume Residual Slag Fume Analyses
Test Slag Cor.c. Weight Loss Weight Analyses in % in %
No. in g in g :in g in % in g Sn In Pb Sn In Pb
1 50 5 33.2 39.6 21.8 5.13 2.14 15.00 12.2n 2.20 5~.70
2 50 10 37.2 38.1 22.8 2.48 1.68 15.90 15.00 2.50 48.10
3 50 15 38.2 41.2 26.8 2.30 1.72 11.90 12.90 2.00 46.20
* added as iron sulfide concentrate
s
TABLE IB
_ Deport nts
Test Residual Slag Fume
No. Sn In Pb Sn In Pb
1 Weight in g 1.70 0.71 4.97 2.65 0.49 11.90
Distribution %39.1 59.2 29.4 60.9 40.8 70.6
2 Weight in g 0.92 0.62 5.93 3.43 0.58 11.00
Distribution %21.1 51.7 35.1 78.9 48.3 65.0
3 Weight in g 0.88 0.66 4.53 3.47 0.54 12.40
Distribution %20.2 54.8 26.8 79.8 45.2 73.2
Example 2
Fumes similar in composition as the fume composition in Table IA
were leached with a 200 g/L sodium hydroxide solution at 95C for 4 hours.
The resulting residue analyzed 8.4% In, 22.4% Sn, 32.4% Zn and 5.2% Pb. The
leach solution contained 1.4 g/L Sn, 19.5 g/L Zn and 17.5 g/L Pb. 25 g of the
leach residue was fused with 65 g solid caustic at 800C for 30 minutes and
the fusion product was subsequently leached with water. The final results
showed that 80% of the tin, 60% of the zinc and 50% oE the lead were extracted
from the fumes, leaving a residue analyzing 23.9% In, 10.4% Sn and 3.4% Sb.
The results Oe the leaching test show that fumes obtained from a
slag are amenable to caustic leaching.
Example 3
This example illustrates the process of the invention by means of a
four-pass loc]c test. All streams wcre circulated in the manner as shown on
the flowsheet and all intermediate solutions were sampled. Caustlc leaches
-- ],0 --
404S
for increments of 200 g of an electric furnace flue dust were carried out at
95 C with 2L of solution containing 200 g/L NaOH and for a 2 hour retention
time. Total input to the test was 22.0 g In, 121.9 g Sn, 388.6 g Pb, 78.6 g
Zn, 26.6 g As and 28.4 g Sb. The liquid/solids separation after the first
caustic leach was made by settling, resulting in a supernatant liquor to
settled solids ratio of 10:1. Settled slurry was used as the input to the
second caustic leach. The liquid/solids separation after the second caustic
leach was made by settling followed by filtration. The residue was not washed
and was dried at 110C. The total amount of dried residue (66.7 g) was fused
with caustic (first three passes 400 g NaOH each; fourth pass 200 g NaOH) in a
250 ml nickel crucible at 650C for 90 minutes. The fusion product was leached
in 2L of water at 55C for 2h. The liquid/solids separation was by settling
and filtration. The water leach residue (indium concentrate) was dried at
110C. The caustic fusion leach solution was treated with about the stoichio-
metric quantity of Ca(OH)2 at 80C for 2h for the precipitation of calcium
hexa-hydroxo stannate. The system was cooled and the slurry allowed to settle.
The settled solids filtered rapidly and were displacement washed, giving a
residue of tin concentrate.
The analyses of the fourth pass of the caustic leaches, the water
leach and the tin precipitation are given in Table IIA, and the metal distri-
butions are given in Table IIB.
- 11 -
TABLE IIA
_. .
FOURTH PASS ANALYSES
-
In Sn Pb Zn As S~
g/L g/L g/L g/L g/L g/L
~IRST CAUSTIC LEACH
sol'n. in 2000 mL 0.037 0.64 26.0 4.3 0.75 0.700
out 1680 mL (purge) 0.037 1.2 43.0 12.3 1.80 0.069
SECOND CAUSTIC LEACH
sol'n. in 1900 mL 0.008 0.33 3.7 2.2 0.11 0.033
out 2075 mL 0.035 0.47 21.0 3.1 0.56 1.350
WATER LEACH
leach res.
~indium concentrate) 29.0%4.0% 4.2%2.3% 0.004% 13.3%
sol'n. out 2100 mL 14 13.5 3.5 2.0 0.08 57
TIN PRECIPITATION
sol'n. in 2000 mL 0.014 13.5 3.5 2.0 0.08 0.057
out 2000 mL 0.006 0.1 3.9 2.1 0.08 0.018
residue ~tin concentrate) 0.09% 36.8%0.27% 0.33% 0.013% 0.8%
TABLE~IIB
WEIGHT
In Sn Pb Zn As Sb
g g g g g g
FIRST CAUSTIC LEACH
sol'n in 2000 mL 0.07~ 1.2852.00 8.60 1.50 1.~0
out 1680 mL tpurge) 0.0622.0272.20 20.66 3.02 0.12
sol'n gain ~loss)(0.012)0.7420.20 12.06 1.52 ~1.28)
SECOND CAUSTIC LEACH
sol'n in 1900 mL 0.015 0.63 7.03 ~.18 0.21 0.06
out 2075 mL 0.073 0.98~3.58 6.43 1.16 2.80
sol'n gain 0.058 0.3536.55 2.25 0.95 2.7
WATER LEACH
leach res.
(indium concentrate) ~.93 0.68 0.71 0.39 _ 2.26
sol'n out 2100 mL0.03 28.357.35 ~.20 0.17 0.12
TIN PRECIPITATION
_
sol'n in 2000 mL 0.028 27.007.00 ~.O0 0.16 0.11
out 2000 mL 0.012 0.20 7.80 ~.20 0.16 0.04
residue ~tin
concentrate) 0.043 25.250.13 0.16 0.01 0.38
BALANCE
dust input in 200 g 5.5030.~7 97.15 19.6~ 6.66 7.09
acco~mted output 5.03 27.8965.78 19.26 2.65 ~.14
Unaccounted loss ~gain) 8.6% 8.5% 32.3% 1.93% 60.2% ~1.6%
recovery 89.6% 82.9%
~Z~4Q4~
The results of the lock test indicate excellent recoveries of In in
the final concentrate and of Sn as calcium hexa-hydroxo stannate. The indium
recovery for the fourth pass was 89.6%. The indium concentrate assayed In
29%, Sn 4.0%, Pb 4.2%, Zn 2.3~, As 0.004%, and Sb 13.3%. The tin recovery for
the fourth pass was 82.9%. The tin concentrate assayed Sn 36.8%, In 0.09%, Pb
0.27%, Zn 0.33%, As 0.013%, Sb 0.8%. The first caustic leach solution (purge
for Pb, Zn, and As) assayed In 0.037 g/L, Sn 1.2 g/L, Pb 43 g/L, Zn 12.3 g/L,
As 1.8 g/L and Sb 0.069 g/L.
200 g of input dust in the fourth pass yielded 17.0 g of indium
concentrate and 68.6 g of tin concentrate. For this treatment, 400 g of NaOH
and 19 g of Ca~OH)2 were used.
The recoveries for indium, tin and lead for the four-pass lock test
are given in Tables III, IV and V, respectively. From the inputs and reco-
veries it can be calculated that the overall recovery of Indium was 80.6%, of
tin 88.1%, and of lead 85.1%.
TABLE III
Indium Concentrate
Weights Indium AnalysesIndium Recoveries
in g in % in g
1st pass 13.4 30.6 4.10
2nd pass 23.4 18.4 4.31
3rd pass 22.0 20.0 4.40
4th pass 17.0 29.0 4.93
'['OTAI, 17.-/4
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~4~
TABL~ IV
Tin Concentrate
Water-Leach Solution Tin-Precipitation Solution Precipitated
Tin
volume analysis Tin volume analysis TinRecovered
in ml iJl g/L Sn in g in ml in g/L Sn in g in g
-
1st pass 1950 13.5 26.33 1850 1.20 2.22 24.11
2nd pass 1980 14.5 28,71 2000 0~31 0.62 28.09
3rd pass 2000 14.5 29.00 2000 0.33 0.66 28.34
4th pass 2000 13.5 27,00 2000 0.10 0.20 26.80
TOTAL: 107.34
TABLE V
Lead in First Caustic Leach Solution ~purge~
Volume Lead AnalysesLead
in ml in g/L in g
1st pass 1810 51.0 92.3
2nd pass 1860 44.5 82.8
3rd pass 1675 18.4 30.8
4th pass 1680 43.0 72.2
Other 4th pass
inteImediates 52.4
TOTAL 330.5
The very low In concentration in the solutions (Table II) indicate
that recoveries Oe In and Sn in an industrial scale process are likely to be
considerably higher.
It is 1mderstood that variations can be made in the process according
to the invention without departing Erom the scope oE the invention. Eor
example, a portion of the leach resiclue from the leach with caustic solution
can be removed Erom the process and directly treated Eor the recovery oE
indium either by itself or together with the indium concentrate obtained after
- 15 -
4Q~5
the removal of tin. Such a procedure can be usef~ll if low concentrations of
tin are present in the starting materials.
- 16 _
