GB2089775A - Recovery of copper from arsenical drosses - Google Patents
Recovery of copper from arsenical drosses Download PDFInfo
- Publication number
- GB2089775A GB2089775A GB8136596A GB8136596A GB2089775A GB 2089775 A GB2089775 A GB 2089775A GB 8136596 A GB8136596 A GB 8136596A GB 8136596 A GB8136596 A GB 8136596A GB 2089775 A GB2089775 A GB 2089775A
- Authority
- GB
- United Kingdom
- Prior art keywords
- copper
- arsenate
- raffinate
- arsenic
- leaching
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 229910052802 copper Inorganic materials 0.000 title claims abstract description 41
- 239000010949 copper Substances 0.000 title claims abstract description 41
- 238000011084 recovery Methods 0.000 title description 6
- 229910052785 arsenic Inorganic materials 0.000 claims abstract description 23
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000002386 leaching Methods 0.000 claims abstract description 22
- 238000000034 method Methods 0.000 claims abstract description 21
- 229940000489 arsenate Drugs 0.000 claims abstract description 18
- DJHGAFSJWGLOIV-UHFFFAOYSA-K Arsenate3- Chemical compound [O-][As]([O-])([O-])=O DJHGAFSJWGLOIV-UHFFFAOYSA-K 0.000 claims abstract description 16
- 150000001450 anions Chemical class 0.000 claims abstract description 11
- 230000001590 oxidative effect Effects 0.000 claims abstract description 5
- MKOYQDCOZXHZSO-UHFFFAOYSA-N [Cu].[Cu].[Cu].[As] Chemical compound [Cu].[Cu].[Cu].[As] MKOYQDCOZXHZSO-UHFFFAOYSA-N 0.000 claims abstract description 4
- 150000001495 arsenic compounds Chemical class 0.000 claims abstract description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 26
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical group [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- 229910021529 ammonia Inorganic materials 0.000 claims description 10
- 229910021653 sulphate ion Inorganic materials 0.000 claims description 9
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 8
- -1 arsenate ions Chemical class 0.000 claims description 6
- MHUWZNTUIIFHAS-XPWSMXQVSA-N 9-octadecenoic acid 1-[(phosphonoxy)methyl]-1,2-ethanediyl ester Chemical compound CCCCCCCC\C=C\CCCCCCCC(=O)OCC(COP(O)(O)=O)OC(=O)CCCCCCC\C=C\CCCCCCCC MHUWZNTUIIFHAS-XPWSMXQVSA-N 0.000 claims description 5
- 239000003960 organic solvent Substances 0.000 claims description 5
- 229940047047 sodium arsenate Drugs 0.000 claims description 5
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 4
- BMWMWYBEJWFCJI-UHFFFAOYSA-K iron(3+);trioxido(oxo)-$l^{5}-arsane Chemical compound [Fe+3].[O-][As]([O-])([O-])=O BMWMWYBEJWFCJI-UHFFFAOYSA-K 0.000 claims description 4
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 3
- 239000000908 ammonium hydroxide Substances 0.000 claims description 3
- UKUVVAMSXXBMRX-UHFFFAOYSA-N 2,4,5-trithia-1,3-diarsabicyclo[1.1.1]pentane Chemical compound S1[As]2S[As]1S2 UKUVVAMSXXBMRX-UHFFFAOYSA-N 0.000 claims description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 2
- 239000007789 gas Substances 0.000 claims description 2
- 150000003839 salts Chemical class 0.000 claims description 2
- 230000001376 precipitating effect Effects 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 24
- 239000000706 filtrate Substances 0.000 description 7
- 238000004458 analytical method Methods 0.000 description 5
- 238000005406 washing Methods 0.000 description 5
- ARUVKPQLZAKDPS-UHFFFAOYSA-L copper(II) sulfate Chemical compound [Cu+2].[O-][S+2]([O-])([O-])[O-] ARUVKPQLZAKDPS-UHFFFAOYSA-L 0.000 description 4
- 235000011121 sodium hydroxide Nutrition 0.000 description 4
- 239000011701 zinc Substances 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 3
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical group [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 3
- XPVHUBFHKQQSDA-UHFFFAOYSA-N ammonium arsenate Chemical group [NH4+].[NH4+].O[As]([O-])([O-])=O XPVHUBFHKQQSDA-UHFFFAOYSA-N 0.000 description 3
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000001117 sulphuric acid Substances 0.000 description 3
- 235000011149 sulphuric acid Nutrition 0.000 description 3
- 229910052725 zinc Inorganic materials 0.000 description 3
- 229910000563 Arsenical copper Inorganic materials 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 238000013019 agitation Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000012065 filter cake Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 230000007928 solubilization Effects 0.000 description 2
- 238000005063 solubilization Methods 0.000 description 2
- 229910017251 AsO4 Inorganic materials 0.000 description 1
- RMBBSOLAGVEUSI-UHFFFAOYSA-H Calcium arsenate Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-][As]([O-])([O-])=O.[O-][As]([O-])([O-])=O RMBBSOLAGVEUSI-UHFFFAOYSA-H 0.000 description 1
- 244000007645 Citrus mitis Species 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 238000010793 Steam injection (oil industry) Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 239000001166 ammonium sulphate Substances 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 239000011260 aqueous acid Substances 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229940103357 calcium arsenate Drugs 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 210000003298 dental enamel Anatomy 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- 235000012245 magnesium oxide Nutrition 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 238000003921 particle size analysis Methods 0.000 description 1
- 239000000049 pigment Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- TUNFSRHWOTWDNC-UHFFFAOYSA-N tetradecanoic acid Chemical compound CCCCCCCCCCCCCC(O)=O TUNFSRHWOTWDNC-UHFFFAOYSA-N 0.000 description 1
- 239000011864 timber preservative Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B15/00—Obtaining copper
- C22B15/0063—Hydrometallurgy
- C22B15/0084—Treating solutions
- C22B15/0089—Treating solutions by chemical methods
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B15/00—Obtaining copper
- C22B15/0063—Hydrometallurgy
- C22B15/0065—Leaching or slurrying
- C22B15/0078—Leaching or slurrying with ammoniacal solutions, e.g. ammonium hydroxide
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B30/00—Obtaining antimony, arsenic or bismuth
- C22B30/04—Obtaining arsenic
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
A process for leaching copper and arsenic from copper dross (1) containing copper arsenide and separated from molten lead bullion comprises leaching the dross with an aqueous ammoniacal solution (4) containing arsenate as the predominant anion under oxidizing conditions to obtain a leachate (5), removing copper from the leachate to obtain a raffinate (12) and re-cycling raffinate to the leaching stage, and removing a bleed (13) of raffinate from the circuit and precipitating a substantially insoluble arsenic compound from the raffinate bleed to remove arsenic from the circuit. <IMAGE>
Description
SPECIFICATION
Recovery of copper from arsenical drosses
This invention relates to the recovery of copper from arsenical drosses, and more particularly to the leaching and recovery of copper and arsenic from drosses containing substantial amounts of arsenic, derived from the blast-furnace smelting of lead or zinc bearing oxidic materials.
High levels of arsenic in the feeds to certain lead/zinc blast-furnaces lead to high arsenic contents in the copper drosses recovered from the lead bullion. For example, samples of drosses obtained from two North
American smelters contained 7.6 and 10.9% (dry weight) of arsenic. The processing of these arsenical drosses by pyrometallurgical methods usually leads to environmental and hygiene problems and to processing difficulties which arise due to speiss formation. Hence, there is a need for a hydrometallurgical technique whereby arsenic can be removed within the plant in a safely-disposable form (e.g. ferric arsenate) for dumping or sale.
It is known to use aqueous ammoniacal sulphate/carbonate mixtures for leaching copper from drosses separated from lead bullion produced in a zinc/lead blastfurnace (see for example British Patent
Specification No. 1 399 281). Also where a substantial proportion of sulphur is present in such a dross it is known to use a leach solution consisting predominantly of ammonium sulphate and ammonium hydroxide in the substantial absence of carbonate ions (see British Patent Specification No. 1 490 813).
However, the problem of leaching copper from high arsenic - content dross has only recently been investigated and one of the main difficulties associated with such a problem is to produce not only a copper-bearing solution amenable to subsequent copper recovery (as cathode copper or a copper salt) but also to produce an arsenical product which is in an inert and safely-disposable form or suitable for processing to a saleable product. Preferably the arsenical product should be commercially saleable, e.g. as a pigment, ceramic enamel, paint, mordant or timber preservative, but this is only possible in a few locations in the world.
The present invention provides a process for leaching copper and arsenic from copper dross containing copper arsenide and separated from molten lead bullion, comprising leaching the dross, in finely-divided form, with an aqueous ammoniacal solution containing arsenate as the predominant anion, under oxidizing conditions, to obtain a leachate, removing copper from the leachate to obtain a raffinate and re-cycling raffinate to the leaching stage, and wherein a bleed of raffinate is removed from the circuit and a substantially insoluble arsenic compound is precipitated, directly or indirectly, from the raffinate bleed, to remove arsenic from the circuit.
Preferably the aqueous ammoniacal leach solution also contains sulphate ions and/or carbonate ions.
The leach solution should preferably contain at least 50 mole per cent of arsenate ions, based on all anions present in the leach solution. More preferably the mole ratio of arsenate to all other anions present in the leach solution is at least 2:1.
Preferably copper is extracted from the leachate by means of a copper-selective organic solvent, e.g. an aromatic hydroxy-oxime such as those sold by Henkel Corporation under the Trade Mark "LIX", to produce a raffinate for re-cycling to the leach reactor.
Alternatively, copper may be precipitated as oxide by boiling off ammonia, e.g. by steam injection.
Preferably the leach solution contains about40g/l (+ 10%) of ammonia (as ammonium hydroxide) in addition to any ammonia combined with sulphate and other anions other than arsenate. This ensures the maximum solubility of the arsenate ion when copper has been removed from the leachate with the organic solvent mentioned above. Higher or lower concentrations ofthis "free" ammonia may tend to encourage deposition of ammonium arsenate crystals in the raffinate, depending upon arsenate concentration.
Preferably the proportion of raffinate bled from the circuit is minimized to reduce the heating costs associated with the recovery of its ammonia content. This proportion depends on the quantity of arsenic leached in each cyle and/or the concentration of arsenic in the leach solution, i.e. the quantity of new arsenic leached must be equal to that withdrawn from the system. For example, in the case where 4.4-5.9g/l is leached, a 7.8-11.3% volume bleed of raffinate of the following typical concentration is required.
AsO4 36.6-53.8g/l (as As)
S04 15.5-33.1g/l (as S04) NH3 46-61 g/l (Total NH3).
The practical maximum arsenic concentration depends partly on the sulphate concentration. As the sulphate is derived from the oxidation of sulphur in the dross, its concentration in leachate and therefore its effect on arsenate solubility will vary from dross to dross. However, it has been found possible to use solutions containing up to 61 g/l arsenic (present as arsenate) and 66g/l S04 at room temperature.
Preferably the aqueous raffinate bleed solution is subjected to heating, more preferably boiling, in the presence of a base, e.g. lime, magnesium oxide or caustic soda (sodium hydroxide), in order to drive off ammonia and produce insoluble calcium arsenate, magnesium arsenate or a sodium arsenate solution.
Where sodium arsenate is produced this may be reacted with a ferric salt, e.g. ferric sulphate, at a pH value of 3-6 to vield an insoluble ferric arsenate which can be disposed of, e.g. by dumping. Alternatively, arsenic may be precipitated from the raffinate bleed as insoluble arsenic sulphide, e.g. by means of hydrogen sulphide.
The leaching stage should preferably be carried out with agitation and in the presence of an oxidizing gas, e.g. air or oxygen.
The temperature of leaching may be suitably from 20 to 100 C, but a temperature of from 40 to 60"C is preferred. The process is normally carried out at atmospheric pressure but may be carried out in a pressurized vessel.
The copper-bearing organic solvent may be stripped with sulphuric acid and then the aqueous acid solution subjected to electrolysis or purified and subjected to crystallization to produce cathode copper or copper sulphate.
The invention will be further described, by way of example only, with reference to the accompanying drawing, which is a schematic flow sheet illustrating the process according to the present invention.
In the process illustrated in the drawing, arseniacal-bearing copper dross separated from pyrometallurgical lead bullion is fed through a line 1 into a leach reactor 2to which is also fed airthrough a line 3. In the reactor 2 the dross is leached, in finely-divided form, with an aqueous ammonical solution containing arsenate as the predominant anion fed into the reactor through a line 4, to give a leachate. The leachate is removed from the reactor 2 through a line 5 and fed to a mixer/settler system 6 where it is subjected to extraction with a copper-selective organic solvent, which has been washed and stripped with sulphuric acid, to produce aqueous copper sulphate.
Residual solids are removed from the reactor 2, by filtration, and discharged through a line 7. A filter (not shown) is provided in the line 7 and the washings from this filter fed to join the line 5.
The aqueous copper sulphate formed in the mixer/settler 6 is removed therefrom through a line 8 and passed to a further vessel 9 known as a tankhouse. Copper is recovered from the copper sulphate in the tankhouse 9 and discharged therefrom through a line 10, while strip acid (sulphuric acid) is recycled from the tankhouse 9 to the mixer/settler 6 through a line 11.
Removal of copper from the leachate solution in the mixer/settler 6 produces a raffinate which is recycled from the mixer/settler 6 to the reactor 2 through a line 12.
In this specification the term "raffinate" is to be understood as thus described, i.e. as the liquor obtained upon removal of copper from the leachate solution obtained by leaching arsenical-bearing copper dross with an aqueous ammoniacal solution containing arsenate as the predominant anion.
In addition a bleed of the raffinate discharged through the line 12 is passed through a line 13 to a still 14 into which caustic soda is introduced through a line 15. In the still 14the raffinate bleed solution is heated with the caustic soda to boil off ammonia which is removed through a line 16. This ammonia is absorbed in water supplied through a line 17 and recycled, through a line 18, to join the raffinate recycled through the line 12 to constitute the leaching solution fed into the reactor 2 through the line 4.
Sodium arsenate is removed from the still 14 through a line 19 and is treated with ferric sulphate to precipitate insoluble ferric arsenate.
The following experimental results iilustrate the leaching of arsenical copper dross with an ammonium arsenate solution, which constitutes the first stage of the process according to the invention as described above.
Arsenical copper dross having the following analysis (% by weight):
Pb Cu As Zn Fe S Ag
42.1 31.7 10.9 1.5 2.5 3.8 0.47 was leached with 1 litre of ammonium arsenate solution, initially containing no copper, under oxygen at atmospheric pressure and at 50 - 60"C for 6 hours, using an agitation rate of 1590 r.p.m.
The dross was first ground in a hammer-mill to give the following particle size analysis.
Size Fractional Cumulative
(Microns) % +425 0.006 100
+295-425 1.038 99.994
+212-295 3.287 98.956
+125-212 12.187 95.669 + 75-125 17.446 83.482
-75 66.036 66.036
Three leaching runs were carried out on this ground dross, giving the results as shown in the following
Table I. The line reference numerals given in the table in brackets correspond to those of the accompanying drawing.
TABLE I
Run No. 1 2 3
Dross Used (a) Weight 63.2 63.2 82.7 (line 1) (b) Copper content (g) 20.0 20.0 26.2 pH of initial leach solution 10.1 9.82 10.0
Copper Analyses (g) (%) (g) (%) (g) (%)
Filtrate (line 5) 18.99 95.55 18.85 94.34 24.50 93.48
Samples 0.64 3.20 0.36 1.80 0.48 1.83
Washings 0.20 1.00 0.30 1.50 0.49 1.87
Filter Cake (line 7) 0.25 1.25 0.47 2.35 0.74 2.82 20.08 100.00 19.98 99.99 26.21 100.00
Filtrate Volume (mls) (line 5) 979 945 970 pH 9.77 9.52 9.20
Filter Cake Dry Weight (g) (line 7) 36.1 38.3 49.8
% Copper 0.76 1.22 1.48
Analyses of Solutions (g/l)
NH3 Initial 45.8 61.0 52.8
Filtrate 45.5 57.9 52.7
SO4 Initial 22.3 46.8 36.0
Filtrate 26.6 50.8 39.4
As Initial 31.8 44.0 47.2
Filtrate 36.6 50.5 53.8
Analyses of Washings (g)
SO4 0.35 0.30 0.65
As 0.41 0.76 0.95
Arsenic in Dross Recovered in Filtrate and Washings (%) 64.5 65.1 65.9 As will be seen from the Table, the leaching process in accordance with the invention using arsenate leach liquor results in up to almost 99% copper solubilization (copper analysis of filtrate + samples + washings) coupled with 64-65% arsenic solubilization. A proportion of this arsenic is then bled out of the circuit after copper extraction in accordance with the invention as above described to leave an optimum amount of arsenate in solution for the purpose of leaching fresh dross.
Claims (12)
1. A process for leaching copper and arsenic from copper dross containing copper arsenide and separated from molten lead bullion, comprising leaching the dross, in finely-divided form, with an aqueous ammoniacal solution containing arsenate as the predominant anion, inder oxidizing conditions, to obtain a leachate, removing copper from the leachate to obtain a raffinate and re-cycling raffinate to the leaching stage, and wherein a bleed of raffinate is removed from the circuit and a substantially insoluble arsenic compound is precipitated, directly or indirectly, from the raffinate bleed, to remove arsenic from the circuit.
2. A process as claimed in Claim 1, wherein the leach solution contains sulphate and/or carbonate ions in addition to arsenate.
3. A process as claimed in Claim 1 or 2, wherein the leach solution contains at least 50 mole per cent of arsenate ions, based on all anions present.
4. A process as claimed in Claim 3, wherein the mole ratio of arsenate to all other anions present in the leach solution is at least 2:1.
5. A process as claimed in any of Claims 1 to 4, wherein the leach solution contains about 40 g/l of ammonia as ammonium hydroxide in addition to that combined with sulphate and other anions other than arsenate.
6. A process as claimed in any of Claims 1 to 5, wherein copper is removed from the leachate by means of a copper-selective organic solvent.
7. A process as claimed in any of Claims 1 to 6, wherein the raffinate bleed is heated, in the presence of a base, to drive off ammonia and form an arsenate compound.
8. A process as claimed in Claim 7, wherein the base is sodium hydroxide and wherein sodium arsenate is formed.
9. A process as claimed in Claim 8, wherein the sodium arsenate formed is reacted with a ferric salt to yield insoluble ferric arsenate.
10. A process as claimed in any of Claims 1 to 6, wherein insoluble arsenic sulphide is precipitated from the raffinate bleed by means of hydrogen sulphide.
11. A process as claimed in any of Claims 1 to 10, wherein leaching is carried out at 40 to 600C in the presence of an oxidizing gas.
12. A process according to Claim 1 for leaching copper and arsenic from copper dross containing copper arsenide, substantially as herein described with reference to the accompanying drawings.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB8136596A GB2089775B (en) | 1980-12-08 | 1981-12-04 | Recovery of copper from arsenical drosses |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB8039261 | 1980-12-08 | ||
| GB8136596A GB2089775B (en) | 1980-12-08 | 1981-12-04 | Recovery of copper from arsenical drosses |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| GB2089775A true GB2089775A (en) | 1982-06-30 |
| GB2089775B GB2089775B (en) | 1985-01-09 |
Family
ID=26277767
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB8136596A Expired GB2089775B (en) | 1980-12-08 | 1981-12-04 | Recovery of copper from arsenical drosses |
Country Status (1)
| Country | Link |
|---|---|
| GB (1) | GB2089775B (en) |
-
1981
- 1981-12-04 GB GB8136596A patent/GB2089775B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| GB2089775B (en) | 1985-01-09 |
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