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WO2000056942A1 - Procede de recuperation de metaux precieux - Google Patents

Procede de recuperation de metaux precieux Download PDF

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Publication number
WO2000056942A1
WO2000056942A1 PCT/AU2000/000228 AU0000228W WO0056942A1 WO 2000056942 A1 WO2000056942 A1 WO 2000056942A1 AU 0000228 W AU0000228 W AU 0000228W WO 0056942 A1 WO0056942 A1 WO 0056942A1
Authority
WO
WIPO (PCT)
Prior art keywords
metal
matte
metal values
leaching
feed material
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.)
Ceased
Application number
PCT/AU2000/000228
Other languages
English (en)
Inventor
Rodney David Elvish
Rodney Lloyd Leonard
Michael Raymond Davis
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
COMPASS RESOURCES NL
GUARDIAN RESOURCES NL
Original Assignee
COMPASS RESOURCES NL
GUARDIAN RESOURCES NL
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by COMPASS RESOURCES NL, GUARDIAN RESOURCES NL filed Critical COMPASS RESOURCES NL
Priority to AU32634/00A priority Critical patent/AU762257B2/en
Publication of WO2000056942A1 publication Critical patent/WO2000056942A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • C22B15/0026—Pyrometallurgy
    • C22B15/0028—Smelting or converting
    • 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
    • C22B15/0067—Leaching or slurrying with acids or salts thereof
    • C22B15/0071—Leaching or slurrying with acids or salts thereof containing sulfur
    • 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
    • C22B23/02—Obtaining nickel or cobalt by dry processes
    • C22B23/025—Obtaining nickel or cobalt by dry processes with formation of a matte or by matte refining or converting into nickel or cobalt, e.g. by the Oxford process
    • 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
    • C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
    • C22B23/043—Sulfurated acids or salts thereof
    • 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

Definitions

  • This invention relates to the recovery of metal values from a metal containing feed material. It particularly relates to the recovery of metal values, particularly cobalt, nickel, and copper from metal containing feed materials, such as ores, concentrates or mattes.
  • the feed materials may contain metal oxides and/or sulphides.
  • the feed material is typically first subjected to a pyrometallurgical process resulting in the formation of a sulphide matte containing the metal values, and a slag phase, and possibly also a fume.
  • the sulphide matte may then be typically subjected to a further pyrometallurgical process, or in some cases, a separate, hydrometallurgical process in which the matte is leached with a suitable lixiviant, preferably under high temperatures and/or pressures, and often under oxidising conditions.
  • the leaching process typically generates a pregnant, metal value containing leach solution and a solid phase containing leach residue and/or precipitates.
  • the solid phase principally contains the waste byproducts of the process, it is usually discarded.
  • it is often necessary to extend the leach time or conduct the leach under harsh conditions - such as at very high temperatures and pressures. This requires the utilisation of large, expensive, specialist equipment such as an autoclave, and ancillary equipment including feed heating, feed pumps, oxygen injection, and equipment for temperature control, water balance, flash let down etc. This also results in high energy consumption. It is an object of the present invention to provide a process for recovery of metal values from a feed material which overcomes, or at least alleviates, one or more of the above disadvantages of the prior art.
  • a process for the recovery of one or more metal values from a metal containing feed material including the steps of: (a) subjecting said feed material to a pyrometallurgical treatment in which the feed material is smelted to form a matte containing said one or more metal values and a slag phase;
  • step (c) returning said one or more solid phases to step (a) as a flux for the pyrometallurgical treatment.
  • the present invention also provides metal values recovered using the process defined above.
  • the term “matte” is defined as a fusion product produced from the pyrometallurgical treatment of the metal containing feed material, and contains metal sulphides, optionally together with metals and/or metal alloys.
  • concentration is defined herein as being a metal value-containing product which is concentrated from ore after removal of gangue.
  • the process of the invention has the advantage that any metal values which are remaining in the solid phase after the leaching process can be returned to the recovery process for further treatment, instead of being discarded to waste. Further, because any unleached metals are returned to the pyrometallurgical treatment, very high overall recovery of metal values can be achieved by successive leachings of the matte using leaching conditions which are less severe than those utilised in prior art processes, or in a manner to reduce overall processing capital and/or operating costs.
  • the hydrometallurgical treatment further includes adding a neutralising agent to the pregnant leach solution in order to modify the pH thereof.
  • pH adjustment is effected in order to cause precipitation of one or more metals or impurities from solution, typically a metal other than those of interest.
  • Any unwanted solid material resulting from the neutralisation step, such as precipitate, residues etc., can be also recycled to smelting step (a) as a flux material for the slag phase.
  • the metal value containing pregnant leach solution can then be treated using conventional chemical or electrolytical extraction means in order to selectively recover the metal values.
  • step (b) By recycling one or more unwanted solid phases from step (b) to the smelting step (a), any metal values contained in those residues or precipitates are returned to the recovery process for further treatment. Accordingly, the overall recovery of those metal values is enhanced, and the amount of waste material produced is minimised, thereby reducing capital and/or operating costs.
  • the pyrometallurgical and hydrometallurgical stages are integrated into a single process, so that residues from the hydrometallurgical stage can be easily recycled into an earlier pyrometallurgical stage.
  • the invention is applicable for the recovery of base metal values, such as copper, cobalt and nickel possibly together with precious metals, such as silver, gold, platinum, palladium, (rhodium, ruthenium, osmium and iridium) from ores or concentrates, although it is not limited to this application.
  • the invention. also encompasses recovery of lead.
  • the feed material containing the base metals typically comprises sulphide ores, concentrates and/or mattes.
  • the feed material may also contain lead values which are typically removed early in the pyrometallurgical treatment as fume. It is noted that any lead which does report to the matte during smelting will usually report to the solid residue remaining after the subsequent leaching step and is therefore recycled to the smelting step.
  • the smelting step (a) produces a matte containing the metal values.
  • the matte usually comprises a mixture of copper, cobalt and nickel sulphides, possibly together with iron and sulphur. It may also contain one or more metals and/or alloy phases.
  • the matte may subsequently be separated into one or more segregated mattes and/or alloys by conventional means, with one or more segregated phases removed for use or further processing before the remaining matte is subjected to the hydrometallurgical treatment.
  • the metal value containing matte produced in step (a) is fed, after grinding if necessary, to a leaching stage in step (b).
  • the leaching may occur under atmospheric conditions, preferably the leaching is conducted under elevated temperature and/or pressure, for example, in an autoclave.
  • the lixiviant may comprise an acid, preferably a mineral acid, such as sulphuric acid, or a base, such as ammonia.
  • the lixiviant is an acid, more preferably sulphuric acid.
  • the sulphuric acid is derived from waste gases evolved from furnaces used in the pyrometallurgical stage. The gases are typically cooled and cleaned ahead of a contact sulphuric acid plant.
  • the temperature of leaching may be from ambient to 270°C and is typically from 90°C to 270°C.
  • the temperature of leaching is from 90°C to 220°C.
  • the solid residue remaining after the leaching stage is likely to contain, in addition to any unrecovered metal values, various iron compounds such as iron oxides and/or hydroxides and/or sulphates, such as jarosite. These solids are separated from the leaching solution and returned to the smelting stage step (a) where they function as a flux for the slag phase. Metal values remaining in the solid residue will generally be separated from the slag and incorporated into the matte.
  • any metal values remaining in the solid residue will be returned to the pyrometallurgical stage, rather than be lost. Accordingly the operating conditions of the leach can beneficially be moderated because it is not critical to maximise the recovery of metal values during the leach.
  • leaching is conducted under pressure in an autoclave, the temperature and pressure requirements can be reduced, thereby reducing such requirements as energy requirements, oxygen feed pressure, cooling and cost. Indeed, leaching can be effectively conducted partly or completely under atmospheric conditions, with high recovery, although the length of the process increases.
  • the metal value containing pregnant leach solution generated in step (b) may be treated with a neutralising agent.
  • the neutralising agent is an alkaline material such as a metal carbonate or hydroxide.
  • the neutralising agent is an alkaline material, more preferably is a metal carbonate such as a magnesium and/or calcium carbonate.
  • Preferred carbonates are limestone (CaC0 3 ) dolomite (CaMg(C0 3 ) 2 ) or magnesite (MgC0 3 ).
  • the neutralising agents may advantageously be naturally occurring, such as unpurified dolomite, calcite or magnesite which are convenient and relatively inexpensive to use. Any other metal containing phases present as impurities in the carbonates can be incorporated into the metal recovery process by returning any solid precipitate or residue from the neutralising stage to the smelting stage in step (a). For example, some naturally occurring dolomites contain cobalt and manganese.
  • a solid residue containing cobalt and manganese can be recycled to the smelting stage where cobalt is incorporated into the sulphide matte within the rest of the cobalt value and, under suitable pyrometallurgical conditions, the majority of the (deleterious) manganese constitutes a flux and is incorporated into the slag phase, thereby being separated from the metal values.
  • the solid residue remaining from such a neutralisation step typically includes sulphates, hydroxides and possibly oxides.
  • the increase in pH of an acidic, pregnant leach solution effected by neutralisation with an alkaline material such as carbonate can cause the precipitation of compounds from solution, in particular iron compounds, principally as iron oxides and/or hydroxides.
  • the neutralisation therefore substantially removes undesirable soluble iron from the pregnant leach solution thereby facilitating subsequent extraction of the metal values of interest with the precipitate returned to smelting step (a) as a flux material.
  • a maximum pH of about 3.5 has been found necessary in order to limit coprecipitation of cobalt and nickel compounds with the iron compounds (and any other impurities), which are typically discarded to waste.
  • this limitation is not as crucial to the present invention, because any coprecipitated cobalt and nickel will be returned to the pyrometallurgical stage for further processing, rather than being discarded to waste.
  • the maximum pH of neutralisation can exceed 3.5, such as up to a pH value of 4.0. This has the advantage of allowing greater removal of iron (and any other impurities) from the pregnant leach solution thereby minimising impurities in the final product.
  • the process of the invention is particularly beneficial in the recovery of metal values from polymetallic ores and concentrates which are normally difficult to treat using conventional extraction/recovery techniques.
  • Fine grained, polymetallic ores must be crushed to a very fine particle size in order to adequately release and separate the different ore minerals from the gangue and from each other.
  • fine particles cannot be successfully subjected to conventional flotation techniques to separate ore particles from gangue particles.
  • fine ore particles cannot be successfully subjected to conventional differential flotation techniques to separate different types of ore minerals from each other.
  • the inventive process can avoid these problems by producing a bulk sulphide matte during the pyrometallurgical stage. The different types of sulphides in the matte can then be separated using hydrometallurgical techniques.
  • ore minerals can be separated from gangue minerals, by using fine grained flotation techniques.
  • oil agglomeration in which distillate, or other suitable oil, is used as a bridging agent to selectively agglomerate the ore minerals into "clumps" having a size suitable for flotation.
  • the invention is particularly advantageous for the direct extraction of cobalt from ore materials containing this element.
  • cobalt is instead produced as a byproduct of the processing of nickel, copper-nickel and copper-cobalt ores.
  • some cobalt is concentrated into a matte rather than being converted directly to metal, with much of the cobalt being oxidised and reporting to the slag.
  • the highest recovery of cobalt to the matte using conventional smelting techniques ranges from about 50% to about 75%.
  • Cobalt can also be produced hydrometallurgically from lateritic nickel (cobalt) deposits by leaching with ammoniacal ammonium carbonate. This process requires very high tonnages of feed material and produces very high amounts of residue, which are typically discarded. As a result, significant amounts of cobalt are lost in the residue, resulting in low recovery of Co, such as only about 40-50% recovery of cobalt.
  • the pyrometallurgical stage of the present invention can considerably reduce the bulk of ore material (especially due to release of lead fume) resulting in a hydrometallurgical feed material more highly concentrated in cobalt.
  • any cobalt and/or nickel which is inadvertently coprecipitated with iron and other impurities and lost to waste in the prior processes, would be recoverable in the process of the invention.
  • the amount of feed material required for each subsequent step is consistently being reduced. This means that the metal values are becoming significantly more concentrated in the feed material for each step, leading to greater efficiency and less waste.
  • FIGURE 1 is a flow chart illustrating the steps and their interrelationship of the process described in the Example.
  • the process of the invention is used to extract metal values from a fine grained, polymetallic ore (herein identified as "Brown's Ore") containing 3.3% lead, 0.6% copper, 0.13% cobalt and 0.11 % nickel.
  • the ore also contains small quantities of zinc and silver.
  • Mineralisation occurs as both oxide and sulphide minerals.
  • the oxide ore is primarily a mixture of malachite and cerussite with minor pyromorphite, along with remnants of pyrite in a matrix of muscovite and quartz with smaller amounts of kaolinite, graphite, goethite, and biotite.
  • covellite, chalcopyrite, galena, pyrite and pyrrhotite are also present along with tourmaline and zircon.
  • the cobalt and nickel in the oxide ore are included with goethite as a cobalt rich mineral which is optically similar to pure goethite. Some cobalt and nickel is also associated with the remnant pyrite.
  • the major sulphide minerals present are galena, pyrite, chalcopyrite with some covellite and digenite and a cobalt nickel sulphide, identified as siegenite.
  • the major gangue minerals are feldspar, mica, quartz and graphite.
  • the oxide component of the Brown's Ore is mined and treated separately to the sulphide component.
  • the oxide ore is leached separately and the leach solutions subsequently added to the pregnant leach solution arising from the treatment of sulphide ores, discussed below.
  • the sulphide component of the Brown's Ore is finely ground, preferably to a particle size of P ⁇ o of -30 microns. Due to the very fine grained nature of the ore, grinding to a small particle size is necessary to ensure that the ore minerals are adequately released. However, the small particle size of the ground ore means that conventional flotation methods cannot be used to separate the ore from the gangue, or indeed to separate the different ore minerals from each other. Instead the ground ore is first subjected to oil agglomeration, in which distillate is used as a bridging agent to selectively agglomerate the "collected" sulphides and native graphite to a size suitable for flotation.
  • the agglomerated particles are then subjected to flotation in a flotation machine to separate ore from gangue and to produce a concentrate containing mainly lead, copper, cobalt and nickel ore minerals, with small amounts of zinc and silver.
  • the concentrate is then fed into a first furnace where it undergoes direct smelting.
  • Direct smelting is the combination of a number of different smelting processes in a single furnace.
  • the principle smelting processes occurring in the first furnace includes the initial oxidation of metal sulphides and the subsequent reduction to metal. These processes are effected by utilising "submerged lance technology" and "submerged bath technology” which are licensed by Ausmelt Limited.
  • lead is fumed off under neutral to slightly reducing conditions and copper, cobalt and nickel are formed into a sulphide matte.
  • the lead fume from the first furnace is combined with recycled lead fume from a second furnace, briquetted and reduced to lead bullion in the second furnace. Two stages of kettle refining produce a 99.6% Pb bullion.
  • the recovery of copper, cobalt and nickel to the sulphide matte is high - around 95% or higher.
  • the sulphide matte typically contains approximately 37% copper, 12% cobalt, 11% nickel, 13% iron and 27% sulphur.
  • the matte may be subjected to controlled segregation cooling in order to produce a copper matte and a cobalt nickel matte, and/or a metal-cobalt alloy.
  • the Cu -Co -Ni matte is tapped, granulated and ground to form a feed material for the subsequent hydrometallurgical stage.
  • the ground feed material is subjected to pressure oxidation acid leaching in a small conventional autoclave at a rate of 3.4 tonnes/hour.
  • the autoclave is operated at around 210°C with oxygen injection to provide an operating pressure of around 3,000 kPa.
  • Leaching is effected using sulphuric acid derived from furnace off-gases during smelting.
  • the residence time is around 60 minutes.
  • the solid residue remaining from the leach process typically contains various iron compounds, such as iron oxides and/or hydroxides and/or sulphates, as well as any unrecovered metal values.
  • the residue is separated from the leach liquor and returned to the first furnace in the pyrometallurgical stage where it functions as a flux for the smelting process. Unrecovered metal values present in the leach residue are also returned to the smelting process and incorporated into the sulphide matte there produced.
  • the acidic leach liquor is subsequently partially neutralised by addition of a locally occurring cobalt containing dolomite. The neutralisation reaction results in formation of a solid precipitate which largely comprises iron compounds although, some Co and Ni may be coprecipitated.
  • the precipitate, and any solid residue remaining after pH adjustment, are also recycled to the pyrometallurgical stage as flux.
  • any metal values derived from the dolomite (e.g. cobalt) and present in the solid residue are incorporated into the sulphide matte produced during the smelting stage, and thereby enhance the overall recovery of those metal values.
  • the return of leach residue and/or precipitates to the smelting stage facilitates optimum pressure leaching conditions because the recovery of maximum cobalt from the leaching stage is not critical.
  • the precipitation and solution purification stages by pH adjustment can be optimised for iron and impurity precipitation as any coprecipitated cobalt and nickel is returned to the pyrometallurgical stage.
  • the pregnant leach solution is subjected to a series of solvent extraction and/or electrowinning processes, separated by purification steps, in order to recover the metal values of interest.
  • the precipitates from the purification steps were also returned to the pyrometallurgical stage.
  • Copper is recovered by copper solvent extraction using a chemical consisting of a phenolic oxime derivative having the trade name LIX622N, distributed by Cognis Australia Pty. Ltd.
  • the copper raffmate is then returned to the autoclave to increase the cobalt concentration to about 12.6 g/l and the nickel concentration to about 8.3 g/l.
  • a bleed stream is passed to secondary iron precipitation and then secondary copper solvent extraction.
  • Zinc, cobalt and nickel are recovered by solvent extraction using a bis(2.4,4-trimethylpentyl) phosphonic acid sold under the trade name Cyanex 272 distributed by Cytec Australia Ltd. Differential extraction is effected by varying the pH of the aqueous leach solution. The overall percentage recoveries of the metal values from the Brown's
  • the advantages of the present invention include: (i) high recovery of metal values; (ii) a reduction in waste byproducts;

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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)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

Ce procédé de récupération d'un ou de plusieurs métaux précieux à partir d'une matière de charge contenant du métal consiste, (a) à soumettre cette matière de charge à un traitement pyrométallurgique dans le cadre duquel la matière de charge est fondue pour constituer une matte contenant ce ou ces métaux précieux et une phase laitier, (b) soumettre cette matte à traitement hydrométallurgique comprenant la lixiviation de la matte afin dissoudre le ou les métaux précieux dans une solution, ce traitement hydrométallurgique se soldant par la formation d'une solution forte de lixiviation contenant le métal précieux ainsi qu'une ou plusieurs phases solides et, (c) à renvoyer la ou les phases solides aux fins de l'opération (a) sous forme de flux pour la phase laitier.
PCT/AU2000/000228 1999-03-24 2000-03-22 Procede de recuperation de metaux precieux Ceased WO2000056942A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU32634/00A AU762257B2 (en) 1999-03-24 2000-03-22 Process for recovering metal values

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AUPP9394A AUPP939499A0 (en) 1999-03-24 1999-03-24 Process for recovering metal values
AUPP9394 1999-03-24

Publications (1)

Publication Number Publication Date
WO2000056942A1 true WO2000056942A1 (fr) 2000-09-28

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Application Number Title Priority Date Filing Date
PCT/AU2000/000228 Ceased WO2000056942A1 (fr) 1999-03-24 2000-03-22 Procede de recuperation de metaux precieux

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AU (1) AUPP939499A0 (fr)
PE (1) PE20010057A1 (fr)
WO (1) WO2000056942A1 (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2870260A1 (fr) * 2004-05-13 2005-11-18 Sumitomo Metal Mining Co Procede hydrometallurgique de minerai d'oxyde de nickel
WO2013090981A1 (fr) * 2011-12-22 2013-06-27 Xstrata Technology Pty Ltd Procédé de fusion
US20250066875A1 (en) * 2023-08-25 2025-02-27 Korea Zinc Co., Ltd. All-in-one nickel recovering method for nickel recovery from raw materials containing nickel
US12325894B2 (en) 2023-08-25 2025-06-10 Korea Zinc Co., Ltd. All-in-one nickel recovering method for nickel metal recovery from raw materials containing nickel
US12385108B2 (en) 2023-08-25 2025-08-12 Korea Zinc Co., Ltd. All-in-one nickel recovering method for nickel hydroxide recovery from raw materials containing nickel

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4067952A (en) * 1974-09-06 1978-01-10 Anglo-Transvaal Consolidated Investment Company Limited Leaching of copper-nickel concentrates
US4152142A (en) * 1977-02-28 1979-05-01 Kennecott Copper Corporation Recovery of copper values from iron-containing ore materials as mined and smelted
US4298581A (en) * 1980-04-15 1981-11-03 Cabot Corporation Process for recovering chromium, vanadium, molybdenum and tungsten values from a feed material
US4448604A (en) * 1981-09-16 1984-05-15 Matthey Rustenburg Refiners (Pty) Limited Recovery of precious metals from leach residues
WO1996031629A2 (fr) * 1995-03-24 1996-10-10 Kennecott Holdings Corporation Procede de traitement de flux d'impuretes destines a etre rejetes

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4067952A (en) * 1974-09-06 1978-01-10 Anglo-Transvaal Consolidated Investment Company Limited Leaching of copper-nickel concentrates
US4152142A (en) * 1977-02-28 1979-05-01 Kennecott Copper Corporation Recovery of copper values from iron-containing ore materials as mined and smelted
US4298581A (en) * 1980-04-15 1981-11-03 Cabot Corporation Process for recovering chromium, vanadium, molybdenum and tungsten values from a feed material
US4448604A (en) * 1981-09-16 1984-05-15 Matthey Rustenburg Refiners (Pty) Limited Recovery of precious metals from leach residues
WO1996031629A2 (fr) * 1995-03-24 1996-10-10 Kennecott Holdings Corporation Procede de traitement de flux d'impuretes destines a etre rejetes

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2870260A1 (fr) * 2004-05-13 2005-11-18 Sumitomo Metal Mining Co Procede hydrometallurgique de minerai d'oxyde de nickel
WO2013090981A1 (fr) * 2011-12-22 2013-06-27 Xstrata Technology Pty Ltd Procédé de fusion
US20250066875A1 (en) * 2023-08-25 2025-02-27 Korea Zinc Co., Ltd. All-in-one nickel recovering method for nickel recovery from raw materials containing nickel
US12325894B2 (en) 2023-08-25 2025-06-10 Korea Zinc Co., Ltd. All-in-one nickel recovering method for nickel metal recovery from raw materials containing nickel
US12385108B2 (en) 2023-08-25 2025-08-12 Korea Zinc Co., Ltd. All-in-one nickel recovering method for nickel hydroxide recovery from raw materials containing nickel

Also Published As

Publication number Publication date
PE20010057A1 (es) 2001-02-01
AUPP939499A0 (en) 1999-04-15

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