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WO2009149521A1 - Procédé de récupération de métaux de base à partir de minerais - Google Patents

Procédé de récupération de métaux de base à partir de minerais Download PDF

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Publication number
WO2009149521A1
WO2009149521A1 PCT/AU2009/000754 AU2009000754W WO2009149521A1 WO 2009149521 A1 WO2009149521 A1 WO 2009149521A1 AU 2009000754 W AU2009000754 W AU 2009000754W WO 2009149521 A1 WO2009149521 A1 WO 2009149521A1
Authority
WO
WIPO (PCT)
Prior art keywords
nickel
leaching
leach
ore
hydrometallurgical method
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/AU2009/000754
Other languages
English (en)
Inventor
Michael Rodriguez
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.)
Poseidon Nickel Ltd
Original Assignee
Poseidon Nickel Ltd
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
Priority claimed from AU2008903042A external-priority patent/AU2008903042A0/en
Priority claimed from AU2008100563A external-priority patent/AU2008100563C4/en
Application filed by Poseidon Nickel Ltd filed Critical Poseidon Nickel Ltd
Priority to EP09761186.7A priority Critical patent/EP2288736A4/fr
Priority to BRPI0909874A priority patent/BRPI0909874A2/pt
Priority to CA2727556A priority patent/CA2727556A1/fr
Priority to AU2009257202A priority patent/AU2009257202A1/en
Publication of WO2009149521A1 publication Critical patent/WO2009149521A1/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
    • C22B1/00—Preliminary treatment of ores or scrap
    • 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
    • C22B23/005—Preliminary treatment of ores, e.g. by roasting or by the Krupp-Renn 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
    • 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
    • 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
    • C22B3/02—Apparatus therefor
    • 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

  • the present invention relates to a method for the recovery of base metals from sulphide and/or oxide ores. More particularly, though not exclusively, the invention relates to a hydrometallurgical method for leaching of nickel from a combination of nickel sulphide and nickel oxide ores.
  • Nickel sulphide ores have traditionally been treated via a pyrometallurgical smelting process, in order to recover nickel as a high grade nickel matte.
  • the nickel content of the matte can range from 60 to 80% nickel as a sulphide.
  • Hydrometallurgical processes such as leaching have historically not been applied to nickel sulphide ores or concentrates, as smelting is commercially competitive when compared to hydrometallurgical processes.
  • smelting unlocks significant energy credits that is converted to electrical energy and produces sulphuric acid or sulphur, as by-products.
  • This co-generation approach improves the overall competitiveness of pyrometallurgical process when compared to hydrometallurgical processes.
  • hydrometallurgical processes such as the Activox or the Albion Process typically require fine grinding P90 or minus 10 microns, which consumes energy.
  • HPAL High Pressure Acid Leach
  • Ni nickel sulphide ores also contain magnesium (Mg expressed as MgO) and when treated through a concentrator produce a sulphide concentrate that has a low iron (Fe) to MgO ratio.
  • Mg magnesium
  • Fe iron
  • a low iron to MgO ratio impacts on flash furnace slag chemistry.
  • the slag becomes viscous and can be difficult to remove from the furnace without increasing the slag operating temperature.
  • Some of these ores also contain arsenic (As) at levels that require careful blending to manage the occupational health and safety aspects of arsenic and its impact on human health, which makes these sulphide ores undesirable for smelting.
  • the present invention aims to alleviate or at least partially alleviate some of the difficulties associated with the conventional pyrometallurgical and hydrometallurgical processes for the treatment of nickel sulphide ores or concentrates. However it will be understood that it is not limited in its application to nickel sulphide ores or concentrates.
  • the previous discussion of the background to the invention is intended to facilitate an understanding of the present invention only. The discussion is not an acknowledgement or admission that any of the material referred to is or was part of the common general knowledge as at the priority date of this application. References to prior art in this specification are provided for illustrative purposes only and are not to be taken as an admission that such prior art is part of the common general knowledge in Australia or elsewhere. Summary of the Invention
  • a hydrometallurgical method for leaching a base metal in a combined pressure acid leach comprising the steps of: combining a sulphide ore or concentrate with a laterite or other oxide ore and mixing them together to form a slurry; leaching the combined slurry in a pressure acid leach circuit; and, providing an oxidant to the pressure acid leach circuit wherein the oxidant allows for the conversion of substantially all of the sulphide to transition through to sulphate.
  • the step of combining sulphide ore or concentrate with laterite or other oxide ore and mixing them involves milling the ores together.
  • the method comprises the further step of leaching the combined sulphide and oxide ore together with pregnant leach solution produced from an atmospheric leach circuit, and without the requirement of additional sulphuric acid.
  • the base metal is selected from the group consisting of nickel, cobalt, copper, lead and zinc.
  • the sulphide ore or concentrate is a nickel sulphide or concentrate and the laterite or other oxide ore is a nickel laterite or other nickel oxide ore.
  • the method further comprises the steps of directing a nickel laterite or other nickel oxide ore to an atmospheric leach process to produce a pregnant leach solution, and adding the pregnant leach solution to the combined sulphide ore or concentrate and laterite or other nickel oxide ore during the combining step.
  • the pressure acid leach circuit comprises a series of pressure Pachuca tanks.
  • the preferred oxidant is oxygen or air; ferric iron generated in a separate atmospheric leach process, and/or manganese present in the ores as manganese dioxide (MnO 2 ) may also be used.
  • the method further comprises a roasting step in which pyrite is roasted to form a metallurgical gas.
  • the metallurgical gas is preferably cooled and conditioned before passing to a wet end of a sulphuric acid plant, the sulphuric acid plant typically being used to generate sulphuric acid for use in the method of the invention as required.
  • the pyrite is mined from the same ore deposit as the sulphide ore used in the combining step of the invention.
  • the metallurgical gas comprises at least about 9 to 11% sulphur dioxide (SO 2 )
  • a hydrometallurgical method for leaching nickel comprising the steps of: combining nickel sulphide ore or concentrate with nickel laterite or other oxide ore and mixing them together to form a slurry; leaching the combined slurry in a pressure acid leach circuit; and, providing an oxidant to the pressure acid leach circuit wherein the oxidant allows for the conversion of substantially all of the nickel sulphide to transition through to nickel sulphate.
  • the method further comprises the steps of directing a nickel laterite or other nickel oxide ore to an atmospheric leach process to produce a pregnant leach solution, and adding the pregnant leach solution to the combined sulphide ore or concentrate and laterite or other nickel oxide ore during the combining and milling step.
  • the pregnant leach solution (PLS) from the atmospheric leach circuit preferably has a ferric iron concentration within the range of 10 to 60 g/L
  • the PLS from the atmospheric leach circuit has a free acid concentration of less than 30 g/l.
  • the PLS from the atmospheric leach circuit has a nickel concentration of >4 g/l.
  • the nickel sulphide ore or concentrate preferably has a nickel concentration within the range of about 1 to 10% Ni.
  • the nickel laterite or oxide ore has a nickel concentration within the range of 0.8 to 3%.
  • the nickel laterite or oxide ore for the atmospheric leach is a saprolite or smectite ore and the laterite or oxide ore required for the pressure acid leach is a limonite ore.
  • the pressure acid leach circuit comprises a series of pressure Pachuca tanks.
  • the free acid concentration achieved in the pressure acid leach is maintained within the range of 30 to 80 g/l.
  • the temperature within the pressure Pachuca tanks is maintained between 160° to 26O 0 C. More preferably, the temperature within the pressure Pachuca tanks is maintained at about 220° to 25O 0 C.
  • the oxygen over pressure within the pressure Pachuca tanks is maintained between 100 to 1000 kPag.
  • the ratio of nickel sulphide ore or concentrate: nickel laterite or other nickel oxide ore in the combining step is about 3:7.
  • the process of leaching the combined slurry approaches autogenous leaching, releasing energy, generating sulphuric acid and producing hematite and alunite as the predominant residue minerals.
  • a hydrometallurgical method for leaching nickel comprising the steps of: combining nickel sulphide ore or concentrate with nickel laterite or other nickel oxide ore in relative proportions selected to achieve optimum density and milling them together to form a slurry; leaching the combined slurry in a pressure acid leach circuit; and, providing air or oxygen to the pressure acid leach circuit wherein the air or oxygen allows for the conversion of substantially all of the nickel sulphide to transition through to nickel sulphate.
  • the method further comprises the steps of directing a nickel laterite or other nickel oxide ore to an atmospheric leach process to produce a pregnant leach solution, and adding the pregnant leach solution to the combined sulphide ore or concentrate and laterite or other nickel oxide ore during the combining and milling step.
  • the ratio of nickel sulphide ore or concentrate: nickel laterite or other nickel oxide ore in the combining step is about 3:7.
  • Figure 1(a) and (b) is a schematic diagram of a process circuit of a preferred method for leaching nickel in accordance with the present invention
  • Figure 2(a) and (b) is a schematic diagram of a process circuit of a further preferred method for leaching nickel in accordance with the present invention.
  • a preferred embodiment of the hydrometallurgical method for leaching of a base metal according to the invention relates to the leaching of nickel.
  • the method preferably comprises the step of directing a nickel laterite or other nickel oxide ore to an atmospheric leach process 10, which in the embodiment of Figure 1 is a first heap leach process (not illustrated).
  • the clarified pregnant leach solution (PLS) from the first heap leach process is then directed to a milling circuit 12.
  • the PLS is preferably heated prior to injection into the milling circuit 12.
  • the PLS may be derived from any suitable atmospheric leach process and it not limited to heap leaching. However in the event that a suitable source of PLS from an atmospheric leach process is not available, water may be substituted for the PLS that is directed to the milling circuit.
  • the method further comprises the step of combining nickel sulphide ore or concentrate 14 with nickel laterite or other nickel oxide ore 16 and milling the combination in the milling circuit 12 with the clarified PLS from the first heap leach process 10 (and/or water as the case may be).
  • the nickel sulphide ore or concentrate 14 preferably has a nickel concentration within the range of about 1 to 10% Ni.
  • the nickel laterite or other nickel oxide ore 16 should have a nickel concentration within the range of 0.8 to 3% Ni.
  • the ratio of nickel sulphide ore (or concentrate): nickel laterite ore (or other nickel oxide ore) is about 3:7. More preferably, the nickel laterite or nickel oxide ore for the atmospheric leach is a saprolite smectite ore and the laterite or oxide ore used for the combined leach is a limonite ore.
  • the viscosity of laterite ores is impacted by additives such as free acid or total dissolved solids.
  • Limonites typically exhibit a reduction in viscosity when solutions from a heap leach operation are slurried with limonite ores. That is, for a given weight percent, solids milling in PLS reduces the viscosity of the pulp. However with saprolite or smectite ores slurrying in PLS will increase the viscosity for a given weight percent solids. Adding sulphides to all laterite ores, whether limonite, saprolite or smectite, acts to reduce the viscosity and is considered innovative.
  • saprolite or smectite is the preferred ore for the atmospheric leach
  • limonite is the preferred ore for milling in atmospheric PLS due to the improvement in slurry density achieved.
  • the milling is typically carried out using the PLS from the first heap leach process instead of, or in addition to, water.
  • the clarified PLS from the first heap leach process preferably has a ferric iron concentration within the range of 10 to 60 g/l.
  • the PLS from the first heap leach process 10 has a free acid concentration of less than 30g/l.
  • the PLS from the first heap leach process 10 has a nickel concentration of more than 4 g/l.
  • a further significant benefit of adding the PLS to the milling circuit 12 is that the head grade of ore passing through the plant is doubled. This, together with acid credits, greatly improves the economies of scale and efficiency of the plant.
  • the milled combined ore from the milling circuit 12 is then subject to a screening step in screening circuit 18. Oversize ore is directed from the screening circuit 18 back to the first heap leach process 10. Undersize ore is fed from the screening circuit 18 to a slurry tank 19, and the combined slurry is then pumped by high pressure slurry pumps to a combined pressure acid leach (CPAL) circuit 20. Wash from the screening circuit 18 is returned to the milling circuit 12.
  • CPAL combined pressure acid leach
  • the combined pressure Pachuca acid leach (CPPAL) circuit 20 comprises a series of pressure Pachuca tanks 22, in which pressure leaching of the combined slurry occurs preferably without the addition of sulphuric acid.
  • the temperature within the pressure Pachuca tanks is maintained between 160° to 260° C, and more preferably between 220° to 250° C.
  • the use of brick-lined Pachuca tanks 22 instead of an autoclave, is much less expensive to maintain due to the high maintenance cost of the titanium used in autoclaves.
  • pressure leaching in the CPPAL 20 occurs for about 90 minutes at a temperature of about 250° C and a pressure of about 44 bar.
  • the nickel and cobalt in the combined slurry is converted to soluble sulphates. More particularly, the nickel and cobalt in the form of sulphides is largely converted to the metal sulphates via the usual chemical transition steps.
  • An oxidant is preferably injected into the Pachuca tanks 22.
  • the preferred oxidant is oxygen or air; ferric iron generated in a separate atmospheric leach process, and/or manganese present in the ores as manganese dioxide (MnO 2 ) may also be used.
  • the oxygen over pressure within the pressure Pachuca tanks is maintained between 100 to 1000 kPag. Without oxygen or air in the CPPAL a significant amount of iron as ferrous remains in solution "locking up" sulphuric acid. However with sufficient oxygen (or other oxidant) most of the iron is converted to hematite.
  • the combined ore is preferably leached in the pressure Pachuca tanks 22 without adding acid and most of the energy required is generated by the oxidation of the sulphide minerals.
  • the process within the CPPAL 20 approaches autogenous leaching, releasing energy, generating sulphuric acid and producing hematite and alunite as the predominant residue minerals.
  • sulphides produce acid, whereas laterites and other oxide ores consume acid. Therefore with the correct balance of the two kinds of ores in the combined slurry fed to the CPPAL 20 the acid released in the hydrolysis circuit as free acid can be matched with the acid consumed.
  • an acid plant 24 is provided to direct high pressure acid to the Pachuca tanks 22.
  • Steam generated by the acid plant 24 is also injected into the Pachuca tanks 22 at 60 bar.
  • the balance of the steam may be used for generating power.
  • the resulting leach slurry exiting from the pressure Pachuca tanks 22 is at high temperatures (typically between 160° to 260° C). Some of this heat is used to preheat the combined slurry as it is fed into the CPPAL 20 to further improve the efficiency of the CPPAL 20.
  • a heater coil 26 uses some of the waste heat to generate steam, which is then fed back to a preheat circuit 28 on the CPPAL feed to heat the combined slurry to about 176° C.
  • the PLS solutions have been found to scale in a similar way that an autoclave will scale in a typical HPAL operation.
  • the first stage preheater 28 is kept below 180° C to prevent iron and aluminium in the PLS solution (added to the milling circuit) from precipitating in the preheat circuit.
  • the leach slurry exiting from the CPPAL 20 undergoes further cooling to atmospheric temperature and pressure in a flash cooling circuit 30. Waste heat from the flash cooling circuit 30 is used for preheating the PLS from the first heap leach process 10.
  • the leach slurry then undergoes solid/liquid separation (thickening) in a counter current decantation (CCD) circuit 32 (see Figure 1(b)).
  • the CCD circuit 32 typically consists of five thickeners which separate the slurry into two streams.
  • the first stream consisting of the pressure leach residue solids is eventually sent as underflow from the last thickener to tailings.
  • the second stream consisting of the clarified solution (containing dissolved nickel and cobalt sulphates) is then preferably directed to a second heap leach process 34 (not shown).
  • the clarified solution from the CCD circuit 32 still has a substantial volume of free acid (typically about 20 litres/tonne) available for further downstream processing.
  • the purpose of the second heap leach process 34 is to utilise this free acid for further leaching of nickel (and cobalt) from a nickel laterite or other nickel oxide ore, rather than wasting it by removal in a neutralisation circuit.
  • the free acid can be removed in a conventional neutralisation circuit, without passing the solution through a second heap leach.
  • the PLS from the second heap leach process 34 is then subject to iron removal using calcrete in a conventional precipitation circuit 36 consisting of a series of agitated tanks. Calcrete is not as efficient as limestone or quicklime for iron removal, however it is readily available locally.
  • the calcrete 37 is milled and mixed with water to produce calcrete slurry.
  • the calcrete slurry is used to neutralise the free acid in the PLS from the second heap leach process, and to precipitate the ferric ions in solution as jarosite/geothite.
  • An iron free clarified solution is obtained by treating the solution from the precipitation circuit 36 in a second CCD circuit 38 for solid/liquid separation (thickening).
  • the thickener underflow solids are discharged with the pressure leach residue solids from the first CCD circuit 32 to tailings.
  • the iron free clarified solution is then subjected to a direct solvent extraction process 40 and electrowinning process 42 in a conventional manner for the extraction and refining of nickel, cobalt, zinc and copper.
  • Solvent extraction raffinate and a barren liquor bleed from the electrowinning process 42 is returned to the first CCD circuit 32 as wash liquor.
  • the invention may also include the additional step of mining pyrite 13 from the same deposit 15 as that from which the nickel sulphide 14 ore is mined.
  • the iron sulphides of the pyrite 13 are roasted in a roasting step 17 and the resulting metallurgical gas 21 is cooled through a waste heat boiler 23.
  • the resulting steam 25 is used to drive a turbine thereby generating power which may be used in the process plant as required.
  • the metallurgical gas stream passes to a conditioning step 27 through a wet end of the acid plant 24 prior to making sulphuric acid which is then used to leach nickel and cobalt in an atmospheric leach process.
  • the metallurgical gas 21 comprises at least about 9 to 11% sulphur dioxide (SO 2 ) .
  • the gas 21 is prepared for the integration into a standard sulphur burning sulphuric acid plant 24. As it is the product of a metallurgical process it passes through a heat recovery section or boiler 23, following which is passes to a conditioning step 27. In the conditioning step, the gas 21 passes to a humidifying tower to remove volatiles and some water, it then passes to mist precipitators which remove most of the water, following which it passes to a drying tower for final water removal. The gas stream then passes into the acid plant 24. Sulphur is burnt as required to maintain a nominal gas strength.
  • Example 1 The present invention is further illustrated by way of the following non-limiting examples: Example 1
  • test conditions are provided in Table 3.
  • the CPPAL of a combined laterite or oxide ore with a sulphide ore or concentrate when leached in pregnant solution from a separate atmospheric leach process, with an overpressure of oxygen of 700 kPag, can successfully extract nickel and cobalt without the addition of acid.
  • saprolite or smectite is used for the atmospheric leach and limonite is the preferred ore for milling in atmospheric leach pregnant solution due to the improvement in slurry density achieved.
  • clarified solution from either a heap leach or atmospheric leach can be applied to replace water for milling in the CPPAL circuit.
  • a direct synergistic solvent extraction and electro- winning process is applied for the extraction and refining of nickel, cobalt, zinc and copper.
  • CPPAL process can be applied to a wide variety of nickel, cobalt, copper and zinc bearing laterite and sulphide ores or concentrates.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Metallurgy (AREA)
  • Manufacturing & Machinery (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Geology (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

L’invention concerne un procédé hydrométallurgique pour lixivier un métal de base lors d’une lixiviation acide sous pression combinée. Le procédé selon l’invention comprend les étapes de combinaison d’un minerai sulfuré (14) ou d’un concentré avec une latérite ou un autre minerai oxydé (16) et de mélange de ces éléments pour former une pâte dans un circuit de broyage (12). La pâte combinée est lixiviée dans un circuit de lixiviation acide sous pression (20) qui comprend une série de cuves Pachuca sous pression (cuves 22). Un oxydant tel que l’oxygène ou l’air est introduit dans le circuit de lixiviation acide sous pression de manière à ce que l’oxydant permette la conversion de sensiblement la totalité du sulfure en un produit de transition, puis en sulfate.
PCT/AU2009/000754 2008-06-13 2009-06-15 Procédé de récupération de métaux de base à partir de minerais Ceased WO2009149521A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EP09761186.7A EP2288736A4 (fr) 2008-06-13 2009-06-15 Procédé de récupération de métaux de base à partir de minerais
BRPI0909874A BRPI0909874A2 (pt) 2008-06-13 2009-06-15 "método hidrometalúrgico para a lixiviação de um metal básico em uma lixívia ácida combinada sob pressão e método hidrometalúrgico para a lixiviação de níquel"
CA2727556A CA2727556A1 (fr) 2008-06-13 2009-06-15 Procede de recuperation de metaux de base a partir de minerais
AU2009257202A AU2009257202A1 (en) 2008-06-13 2009-06-15 Method for the recovery of base metals from ores

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
AU2008903042A AU2008903042A0 (en) 2008-06-13 Method for the Recovery of Base Metals from Ores
AU2008903042 2008-06-13
AU2008100563A AU2008100563C4 (en) 2008-06-13 2008-06-19 Method for the Recovery of Nickel from Ores
AU2008100563 2008-06-19
AU2008903418 2008-07-03
AU2008903418A AU2008903418A0 (en) 2008-07-03 Improved Method for the Recovery of Base Metals from Ores

Publications (1)

Publication Number Publication Date
WO2009149521A1 true WO2009149521A1 (fr) 2009-12-17

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PCT/AU2009/000754 Ceased WO2009149521A1 (fr) 2008-06-13 2009-06-15 Procédé de récupération de métaux de base à partir de minerais

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EP (1) EP2288736A4 (fr)
AU (1) AU2009257202A1 (fr)
BR (1) BRPI0909874A2 (fr)
CA (1) CA2727556A1 (fr)
WO (1) WO2009149521A1 (fr)

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CN108165742A (zh) * 2018-02-11 2018-06-15 乐昌市绿叶环保科技有限公司 软锰矿浸出液中降低连二硫酸锰含量的方法
WO2022178628A1 (fr) * 2021-02-24 2022-09-01 Sherritt International Corporation Co-traitement de concentré de sulfure de cuivre avec du minerai latéritique de nickel

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US20060228279A1 (en) * 2005-04-07 2006-10-12 Finlay Campbell Process for recovery of nickel and cobalt from laterite ore
WO2007039663A1 (fr) * 2005-10-03 2007-04-12 Outotec Oyj. Traitement de concentres ou de minerais de sulfure de nickel avec du chlorure de sodium
WO2007071020A1 (fr) * 2005-12-23 2007-06-28 Harris G Bryn Procédé d'extraction de fer sous forme d'hématite d'un minerai contenant des métaux de base

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GB855218A (en) * 1957-12-10 1960-11-30 Sherritt Gordon Mines Ltd Improved method of extracting non-ferrous metals from metal bearing material
US6171564B1 (en) * 1997-08-15 2001-01-09 Cominco Engineering Services Ltd. Process for extraction of metal from an ore or concentrate containing nickel and/or cobalt
US20060228279A1 (en) * 2005-04-07 2006-10-12 Finlay Campbell Process for recovery of nickel and cobalt from laterite ore
WO2007039663A1 (fr) * 2005-10-03 2007-04-12 Outotec Oyj. Traitement de concentres ou de minerais de sulfure de nickel avec du chlorure de sodium
WO2007071020A1 (fr) * 2005-12-23 2007-06-28 Harris G Bryn Procédé d'extraction de fer sous forme d'hématite d'un minerai contenant des métaux de base

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Title
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CN108165742A (zh) * 2018-02-11 2018-06-15 乐昌市绿叶环保科技有限公司 软锰矿浸出液中降低连二硫酸锰含量的方法
WO2022178628A1 (fr) * 2021-02-24 2022-09-01 Sherritt International Corporation Co-traitement de concentré de sulfure de cuivre avec du minerai latéritique de nickel
US12286686B2 (en) 2021-02-24 2025-04-29 Sherritt International Corporation Co-processing of copper sulphide concentrate with nickel laterite ore

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BRPI0909874A2 (pt) 2015-10-06

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