CA2155050C - Recovery of nickel using heap leaching - Google Patents
Recovery of nickel using heap leaching Download PDFInfo
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- CA2155050C CA2155050C CA002155050A CA2155050A CA2155050C CA 2155050 C CA2155050 C CA 2155050C CA 002155050 A CA002155050 A CA 002155050A CA 2155050 A CA2155050 A CA 2155050A CA 2155050 C CA2155050 C CA 2155050C
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- solution
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- nickel
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- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 title claims abstract description 76
- 229910052759 nickel Inorganic materials 0.000 title claims abstract description 38
- 238000002386 leaching Methods 0.000 title claims abstract description 19
- 238000011084 recovery Methods 0.000 title description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 24
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 14
- 230000003647 oxidation Effects 0.000 claims abstract description 13
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 13
- 229910052742 iron Inorganic materials 0.000 claims abstract description 12
- 238000005363 electrowinning Methods 0.000 claims abstract description 10
- 229910000863 Ferronickel Inorganic materials 0.000 claims abstract description 9
- 238000005342 ion exchange Methods 0.000 claims abstract description 7
- 239000003153 chemical reaction reagent Substances 0.000 claims abstract description 5
- 238000000638 solvent extraction Methods 0.000 claims abstract description 5
- 238000000034 method Methods 0.000 claims description 40
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 11
- 229910021653 sulphate ion Inorganic materials 0.000 claims description 11
- 230000001580 bacterial effect Effects 0.000 claims description 9
- 241000605222 Acidithiobacillus ferrooxidans Species 0.000 claims description 7
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims description 5
- 241000605272 Acidithiobacillus thiooxidans Species 0.000 claims description 3
- 241000589921 Leptospirillum ferrooxidans Species 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- WWNBZGLDODTKEM-UHFFFAOYSA-N sulfanylidenenickel Chemical group [Ni]=S WWNBZGLDODTKEM-UHFFFAOYSA-N 0.000 description 6
- 229910052500 inorganic mineral Inorganic materials 0.000 description 5
- 229910052751 metal Inorganic materials 0.000 description 5
- 239000002184 metal Substances 0.000 description 5
- 239000011707 mineral Substances 0.000 description 5
- 235000010755 mineral Nutrition 0.000 description 5
- 229910052952 pyrrhotite Inorganic materials 0.000 description 5
- 239000002253 acid Substances 0.000 description 4
- 239000003456 ion exchange resin Substances 0.000 description 3
- 229920003303 ion-exchange polymer Polymers 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 239000010935 stainless steel Substances 0.000 description 3
- 229910001220 stainless steel Inorganic materials 0.000 description 3
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 2
- 239000005569 Iron sulphate Substances 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
- 229920001429 chelating resin Polymers 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 239000011790 ferrous sulphate Substances 0.000 description 2
- 235000003891 ferrous sulphate Nutrition 0.000 description 2
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 2
- LGQLOGILCSXPEA-UHFFFAOYSA-L nickel sulfate Chemical compound [Ni+2].[O-]S([O-])(=O)=O LGQLOGILCSXPEA-UHFFFAOYSA-L 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 125000002915 carbonyl group Chemical group [*:2]C([*:1])=O 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000009291 froth flotation Methods 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 229910052935 jarosite Inorganic materials 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052953 millerite Inorganic materials 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 229910052954 pentlandite Inorganic materials 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 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
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0407—Leaching processes
-
- 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
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
-
- 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
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/18—Extraction of metal compounds from ores or concentrates by wet processes with the aid of microorganisms or enzymes, e.g. bacteria or algae
-
- 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
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Biochemistry (AREA)
- Biotechnology (AREA)
- Microbiology (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The production of nickel from a sulphide ore by heap leaching the ore by subjecting the ore to biological oxidation, separating nickel from iron, into an eluate solution, by solvent extraction or the use of an ion exchange reagent, and electrowinning ferronickel from the eluate solution.
Description
~1~~D5~
BACKGROUND OF THE INVENTION
This invention relates to the recovery of nickel from sulphide ores.
Nickel metal has been recovered from nickel sulphide bearing ore bodies by conventional procedures wherein the ore is ground fine and the nickel sulphide minerals are concentrated by froth flotation to produce a nickel sulphide concentrate. The nickel sulphide minerals may be present as pentlandite, pyrrhotite, millerite or other sulphide minerals.
The concentrate is treated further by smelting and reduction to produce a nickel bearing matte which contains nickel, cobalt, copper and iron.
Various techniques are known for refining the matte to produce pure metal. These include leaching, pressure leaching, hydrogen reduction, electrowinning, the Carbonyl process, and so on. In general the refining processes are expensive and produce nickel metal to varying degrees of purity, roughly dependent on the cost of the process employed.
Nickel metal has many applications but its use in stainless steel is becoming more dominant. For stainless steel, nickel metal does not need to be as pure as for other applications and it can be used as ferronickel.
Ferronickel is produced from ores of nickel other than sulphide ores. If however it is possible to produce ferronickel from sulphide ores then, when nickel for stainless steel is not required in a pure state, it is possible to avoid refining to produce pure nickel.
SUMMARY OF THE INVENTION
The invention is concerned with a process to produce impure nickel in the form of ferronickel from sulphide ores.
The invention provides a method of producing nickel from a sulphide ore wherein the ore is subjected to heap leaching, a solution of nickel sulphate and iron sulphate, produced by the leaching, is treated with a solvent extraction or ion exchange reagent which is selective for nickel over ferrous iron whereby the nickel is separated from the iron and transferred in a concentrated form into an eluate solution, and the eluate solution is subjected to an electrowinning process to produce ferronickel.
The leaching process may include a first phase of treating the ore with a solution of ferric sulphate, carrying biological strains which promote biological oxidation.
The biological oxidation process may be carried out using Thiobacillus ferrooxidans.
Preferably a mixture of one or more of Thiobacillus ferrooxidans, Thiobacillus thiooxidans and Leptospirillum ferrooxidans is used in the oxidation step.
The Thiobacillus ferrooxidans preferably mainly consists of the strain TF-FC-1, which is described in the specification of Australian patent No.
618177, issued on April 6, 1992, and which has been deposited at the Australian Government Analytical Laboratories, under Accession No.
N 90/010723.
The solution which promotes bacterial activity may be adjusted in concentration, pH or nutrients.
Finally the ore is washed and the solution separated from the ore heap.
The first leaching phase may be continued for a period of from 2 to 10 days.
The second phase may continue for a period of from 100 to 300 days, typically about 200 days.
In the second phase the biological solution may have a pH from 1,8 to 3,5 typically about 3,0.
21~5~~~
The sulphide ore is preferably crushed to below 6mm.
The invention further extends to a method of producing nickel from a sulphide ore which includes the steps of heap leaching the ore in a first phase by treating the ore with a ferric sulphate and biological solution which promotes oxidation, heap leaching the ore in a second phase by treating the ore with a biological solution at a pH in the range of from 1,8 to 3,5, separating nickel from a solution produced by the second phase, into an eluate solution, and subjecting the eluate solution to an electrowinning process to recover nickel.
The biological solution, in each phase, preferably includes the strain TF-FC-1.
BRIEF DESCRIPTION OF THE DRAWING
The invention is further described by way of example with reference to the accompanying drawing which illustrates in block form a flow diagram of the process of the invention.
DESCRIPTION OF PREFERRED EMBODIMENT
The accompanying drawing illustrates the process of the invention applied to the production of ferronickel from low grade nickel sulphide minerals.
The process includes the following main process steps: a series of heap leaching phases 10A and 10B, an ion exchange step 12 and an electrowinning stage 14.
The sulphide ore 16, which is to be treated, contains a high proportion of the mineral pyrrhotite. It has been found that pyrrhotite reacts with ferric sulphate in solution and ferric sulphate is reduced to ferrous sulphate:
Fe,SB + 7Fe2(S04)3 -~ 21 FeS04 + 8S
It is convenient to carry out the heap leach process in two phases 10A and 1 OB respectively. In the first phase 10A, a ferric sulphate solution is passed through the heap of ore to reduce pyrrhotite. This phase is usually completed in a period of from two to ten days. This phase is important because pyrrhotite interferes with bacterial oxidation. Ferric sulphate solution is continuously generated in an agitated tank where bacterial oxidation converts ferrous to ferric sulphate. Solution from the heap carrying ferrous sulphate is recycled to the tank 20.
The activity of the ferric oxidation tank is promoted by allowing iron to precipitate as Jarosite. Bacterial population is promoted by attachment to the solid. The solid precipitate is removed from solution in a settler before it is pumped to the heap. The solid is returned to the agitated tank.
The bacterial strain is TF-FC-1, as hereinbefore described.
In the second phase of heap leaching (10B), the ore is treated with a solution from a large storage pond 24. The second phase can have a duration of from 100 to 300 days, and normally about 200 days, but the time period depends on the size of the ore according to the degree of crushing. The ore is conveniently crushed to below 6mm, but the size varies according to the ore type.
There is good reason to allow the pH of the solution in the second phase to be about 3,0, but it could be in the range 1,8 to 3,5. The ore usually contains acid consuming constituents because magnesium is invariably present. The high pH reduces acid consumption to a very low level. The acid consumption can be zero if enough acid is generated by oxidation of sulphur in the ore. Remarkably, bacterial activity is good at high pH, although the iron content of the solution is negligible. Bacterial activity in the second phase is mainly in the heap of ore. The bacterial strain is again TF-FC-1. These bacteria are similar to those used on refractory gold ores where iron, nickel and sulphur dissolve to form nickel sulphate and iron sulphate in solution.
A portion of solution 22 is drawn from the storage pond 24 and is directed to the ion exchange step 12. Nickel is adsorbed from solution by an ion exchange resin which is selective for nickel. There are several ion exchange resins which can be used for this process which are marketed under the general grouping of chelating resins. These resins are selective for nickel relative to ferrous iron but not ferric iron. There is very little iron in solution. Any iron present will be ferrous iron. The problem associated with ferric sulphate is thus largely eliminated and the chelating resins are effective in separating the nickel from the iron in solution and allowing the nickel to be transferred in a concentrated form into an eluate solution 30.
The solution 30 is subjected to a known electrowinning process 14 to produce an alloy 32 of nickel and iron. The solution, marked 34, remaining after electrowinning still contains nickel and is reused to elute further nickel from the ion exchange resin.
BACKGROUND OF THE INVENTION
This invention relates to the recovery of nickel from sulphide ores.
Nickel metal has been recovered from nickel sulphide bearing ore bodies by conventional procedures wherein the ore is ground fine and the nickel sulphide minerals are concentrated by froth flotation to produce a nickel sulphide concentrate. The nickel sulphide minerals may be present as pentlandite, pyrrhotite, millerite or other sulphide minerals.
The concentrate is treated further by smelting and reduction to produce a nickel bearing matte which contains nickel, cobalt, copper and iron.
Various techniques are known for refining the matte to produce pure metal. These include leaching, pressure leaching, hydrogen reduction, electrowinning, the Carbonyl process, and so on. In general the refining processes are expensive and produce nickel metal to varying degrees of purity, roughly dependent on the cost of the process employed.
Nickel metal has many applications but its use in stainless steel is becoming more dominant. For stainless steel, nickel metal does not need to be as pure as for other applications and it can be used as ferronickel.
Ferronickel is produced from ores of nickel other than sulphide ores. If however it is possible to produce ferronickel from sulphide ores then, when nickel for stainless steel is not required in a pure state, it is possible to avoid refining to produce pure nickel.
SUMMARY OF THE INVENTION
The invention is concerned with a process to produce impure nickel in the form of ferronickel from sulphide ores.
The invention provides a method of producing nickel from a sulphide ore wherein the ore is subjected to heap leaching, a solution of nickel sulphate and iron sulphate, produced by the leaching, is treated with a solvent extraction or ion exchange reagent which is selective for nickel over ferrous iron whereby the nickel is separated from the iron and transferred in a concentrated form into an eluate solution, and the eluate solution is subjected to an electrowinning process to produce ferronickel.
The leaching process may include a first phase of treating the ore with a solution of ferric sulphate, carrying biological strains which promote biological oxidation.
The biological oxidation process may be carried out using Thiobacillus ferrooxidans.
Preferably a mixture of one or more of Thiobacillus ferrooxidans, Thiobacillus thiooxidans and Leptospirillum ferrooxidans is used in the oxidation step.
The Thiobacillus ferrooxidans preferably mainly consists of the strain TF-FC-1, which is described in the specification of Australian patent No.
618177, issued on April 6, 1992, and which has been deposited at the Australian Government Analytical Laboratories, under Accession No.
N 90/010723.
The solution which promotes bacterial activity may be adjusted in concentration, pH or nutrients.
Finally the ore is washed and the solution separated from the ore heap.
The first leaching phase may be continued for a period of from 2 to 10 days.
The second phase may continue for a period of from 100 to 300 days, typically about 200 days.
In the second phase the biological solution may have a pH from 1,8 to 3,5 typically about 3,0.
21~5~~~
The sulphide ore is preferably crushed to below 6mm.
The invention further extends to a method of producing nickel from a sulphide ore which includes the steps of heap leaching the ore in a first phase by treating the ore with a ferric sulphate and biological solution which promotes oxidation, heap leaching the ore in a second phase by treating the ore with a biological solution at a pH in the range of from 1,8 to 3,5, separating nickel from a solution produced by the second phase, into an eluate solution, and subjecting the eluate solution to an electrowinning process to recover nickel.
The biological solution, in each phase, preferably includes the strain TF-FC-1.
BRIEF DESCRIPTION OF THE DRAWING
The invention is further described by way of example with reference to the accompanying drawing which illustrates in block form a flow diagram of the process of the invention.
DESCRIPTION OF PREFERRED EMBODIMENT
The accompanying drawing illustrates the process of the invention applied to the production of ferronickel from low grade nickel sulphide minerals.
The process includes the following main process steps: a series of heap leaching phases 10A and 10B, an ion exchange step 12 and an electrowinning stage 14.
The sulphide ore 16, which is to be treated, contains a high proportion of the mineral pyrrhotite. It has been found that pyrrhotite reacts with ferric sulphate in solution and ferric sulphate is reduced to ferrous sulphate:
Fe,SB + 7Fe2(S04)3 -~ 21 FeS04 + 8S
It is convenient to carry out the heap leach process in two phases 10A and 1 OB respectively. In the first phase 10A, a ferric sulphate solution is passed through the heap of ore to reduce pyrrhotite. This phase is usually completed in a period of from two to ten days. This phase is important because pyrrhotite interferes with bacterial oxidation. Ferric sulphate solution is continuously generated in an agitated tank where bacterial oxidation converts ferrous to ferric sulphate. Solution from the heap carrying ferrous sulphate is recycled to the tank 20.
The activity of the ferric oxidation tank is promoted by allowing iron to precipitate as Jarosite. Bacterial population is promoted by attachment to the solid. The solid precipitate is removed from solution in a settler before it is pumped to the heap. The solid is returned to the agitated tank.
The bacterial strain is TF-FC-1, as hereinbefore described.
In the second phase of heap leaching (10B), the ore is treated with a solution from a large storage pond 24. The second phase can have a duration of from 100 to 300 days, and normally about 200 days, but the time period depends on the size of the ore according to the degree of crushing. The ore is conveniently crushed to below 6mm, but the size varies according to the ore type.
There is good reason to allow the pH of the solution in the second phase to be about 3,0, but it could be in the range 1,8 to 3,5. The ore usually contains acid consuming constituents because magnesium is invariably present. The high pH reduces acid consumption to a very low level. The acid consumption can be zero if enough acid is generated by oxidation of sulphur in the ore. Remarkably, bacterial activity is good at high pH, although the iron content of the solution is negligible. Bacterial activity in the second phase is mainly in the heap of ore. The bacterial strain is again TF-FC-1. These bacteria are similar to those used on refractory gold ores where iron, nickel and sulphur dissolve to form nickel sulphate and iron sulphate in solution.
A portion of solution 22 is drawn from the storage pond 24 and is directed to the ion exchange step 12. Nickel is adsorbed from solution by an ion exchange resin which is selective for nickel. There are several ion exchange resins which can be used for this process which are marketed under the general grouping of chelating resins. These resins are selective for nickel relative to ferrous iron but not ferric iron. There is very little iron in solution. Any iron present will be ferrous iron. The problem associated with ferric sulphate is thus largely eliminated and the chelating resins are effective in separating the nickel from the iron in solution and allowing the nickel to be transferred in a concentrated form into an eluate solution 30.
The solution 30 is subjected to a known electrowinning process 14 to produce an alloy 32 of nickel and iron. The solution, marked 34, remaining after electrowinning still contains nickel and is reused to elute further nickel from the ion exchange resin.
Claims (16)
1. A method of producing nickel from a sulphide ore wherein:
(a) the ore is subjected to a heap leaching process which includes a phase of treating the ore with a first solution of ferric sulphate carrying biological strains which promote biological oxidation, (b) a second solution which is produced by the leaching process is treated with a solvent extraction or ion exchange reagent which is selective for nickel over ferrous iron whereby the nickel is separated from the iron and transferred in a concentrated form into an eluate solution, and (c) the eluate solution is subjected to an electrowinning process to produce ferronickel.
(a) the ore is subjected to a heap leaching process which includes a phase of treating the ore with a first solution of ferric sulphate carrying biological strains which promote biological oxidation, (b) a second solution which is produced by the leaching process is treated with a solvent extraction or ion exchange reagent which is selective for nickel over ferrous iron whereby the nickel is separated from the iron and transferred in a concentrated form into an eluate solution, and (c) the eluate solution is subjected to an electrowinning process to produce ferronickel.
2. A method according to claim 1 wherein a mixture of one or more of Thiobacillus ferrooxidans, Thiobacillus thiooxidans and Leptospirillum ferrooxidans is used in the oxidation step.
3. A method according to claim 2 wherein the Thiobacillus ferrooxidans includes the strain TF-FC-1.
4. A method according to any one of claims 1 to 3 wherein the phase is continued for a period of from 2 to 10 days.
5. A method according to any one of claims 1 to 4 wherein the leaching process includes a second phase of subjecting the ore to a biological solution which promotes bacterial activity.
6. A method according to claim 5 wherein the second phase continues for a period of from 100 to 300 days.
7. A method according to claim 5 wherein the second phase continues for a period of 200 days.
8. A method according to claim 5, 6 or 7 wherein the biological solution used in the second phase has a pH in the range of from 1,8 to 3,5.
9. A method according to claim 5, 6 or 7 wherein the biological solution has a pH of 3,0.
10. A method according to any one of claims 5 to 9 wherein the biological solution is a mixture of one or more of Thiobacillus ferrooxidans, Thiobacillus thiooxidans and Leptospirillum ferrooxidans.
11. A method according to claim 10 wherein the Thiobacillus ferrooxidans includes the strain TF-FC-1.
12. A method according to any one of claims 1 to 11 wherein the sulphide ore is crushed to below 6mm prior to heap leaching.
13. A method of producing nickel from a sulphide ore which includes the step of heap leaching the ore in a first phase by treating the ore with a first ferric sulphate and biological solution which promotes oxidation, heap leaching the ore in a second phase by treating the ore with a second biological solution at a pH in the range of from 1,8 to 3,5, separating nickel from a solution, produced by the second phase, into an eluate solution, and subjecting the eluate solution to an electrowinning process to recover nickel.
14. A method according to claim 13 wherein the nickel is separated from the solution using a solvent extraction or ion exchange reagent.
15. A method according to claim 13 or 14 wherein the biological solution, in each phase, includes the strain TF-FC-1.
16. A method of producing nickel from a sulphide ore by heap leaching the ore by subjecting the ore to biological oxidation in a ferric sulphate solution, separating nickel from iron, into an eluate solution, by solvent extraction or the use of an ion exchange reagent, and electrowinning ferronickel from the eluate solution.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| ZA945687 | 1994-08-01 | ||
| ZA94/5687 | 1994-08-01 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2155050A1 CA2155050A1 (en) | 1996-02-02 |
| CA2155050C true CA2155050C (en) | 2002-10-01 |
Family
ID=25584184
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002155050A Expired - Fee Related CA2155050C (en) | 1994-08-01 | 1995-07-31 | Recovery of nickel using heap leaching |
Country Status (5)
| Country | Link |
|---|---|
| AU (1) | AU689599B2 (en) |
| CA (1) | CA2155050C (en) |
| FI (1) | FI110190B (en) |
| GB (1) | GB2291869B (en) |
| ZA (1) | ZA956205B (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5626648A (en) * | 1995-07-17 | 1997-05-06 | Bhp Minerals International Inc. | Recovery of nickel from bioleach solution |
| US6379919B1 (en) | 1999-05-28 | 2002-04-30 | Oxidor Corporation Inc | Method for isolating thiocyanate resistant bacteria |
| US6498031B1 (en) | 1999-05-28 | 2002-12-24 | Oxidor Corporation, Inc. | Column reactor for testing and evaluating refractory ores |
| AUPQ265199A0 (en) | 1999-09-03 | 1999-09-30 | Pacific Ore Technology Limited | Improved bacterial oxidation of sulphide ores and concentrates |
| AU770734B2 (en) * | 1999-09-22 | 2004-03-04 | Billiton S.A. Limited | Copper and nickel recovery |
| CA2353002C (en) | 2001-07-13 | 2009-12-01 | Teck Cominco Metals Ltd. | Heap bioleaching process for the extraction of zinc |
| US7455715B2 (en) | 2001-07-13 | 2008-11-25 | Teck Cominco Metals Ltd. | Heap bioleaching process for the extraction of zinc |
| EA012644B1 (en) * | 2004-09-17 | 2009-12-30 | БиЭйчПи БИЛЛИТОН ЭсЭсЭм ТЕКНОЛОДЖИ ПТИ ЛТД. | Production of ferro-nickel or nickel matte by a combined hydrometallurgical and pyrometallurgical process |
| EP3034635B1 (en) | 2014-12-15 | 2018-10-31 | Middle East Mine and Industry Company | Tank bioleaching of copper sulfide ores |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SE468286B (en) * | 1991-06-19 | 1992-12-07 | Boliden Mineral Ab | PROCEDURES FOR THE TREATMENT OF COMPLEX METAL SULPHIDE MATERIAL |
-
1995
- 1995-07-19 FI FI953488A patent/FI110190B/en active
- 1995-07-21 GB GB9514968A patent/GB2291869B/en not_active Expired - Fee Related
- 1995-07-26 ZA ZA956205A patent/ZA956205B/en unknown
- 1995-07-28 AU AU27263/95A patent/AU689599B2/en not_active Ceased
- 1995-07-31 CA CA002155050A patent/CA2155050C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| GB2291869B (en) | 1998-05-27 |
| CA2155050A1 (en) | 1996-02-02 |
| FI110190B (en) | 2002-12-13 |
| GB2291869A (en) | 1996-02-07 |
| AU2726395A (en) | 1996-02-15 |
| GB9514968D0 (en) | 1995-09-20 |
| FI953488A (en) | 1996-02-02 |
| AU689599B2 (en) | 1998-04-02 |
| ZA956205B (en) | 1996-03-13 |
| FI953488A0 (en) | 1995-07-19 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| MKLA | Lapsed |
Effective date: 20140731 |