WO1996007762A1 - Traitement de mineraux - Google Patents

Traitement de mineraux Download PDF

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Publication number
WO1996007762A1
WO1996007762A1 PCT/AU1995/000573 AU9500573W WO9607762A1 WO 1996007762 A1 WO1996007762 A1 WO 1996007762A1 AU 9500573 W AU9500573 W AU 9500573W WO 9607762 A1 WO9607762 A1 WO 9607762A1
Authority
WO
WIPO (PCT)
Prior art keywords
feed
acid
liquor
nickel
sulphide
Prior art date
Application number
PCT/AU1995/000573
Other languages
English (en)
Inventor
Thomas Salinovich
Charles William Douglas Blandy
Original Assignee
Western Mining Corporation Limited
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 Western Mining Corporation Limited filed Critical Western Mining Corporation Limited
Priority to AU33773/95A priority Critical patent/AU3377395A/en
Publication of WO1996007762A1 publication Critical patent/WO1996007762A1/fr

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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
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
    • C22B3/08—Sulfuric acid, other 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

  • the present invention relates to mineral processing. More particularly the invention relates to the processing of a feed material containing oxidised metals together with a metal sulphide containing feed component by pressure oxidation leaching to facilitate the recovery of metal values therefrom.
  • feed material At present it is usual for one type of feed material to be processed independently of other types of feed materials. In cases where mixed ore bodies occur it is common to treat different parts of the ore body by different methods. This may require physical separation of feed materials prior to treatment.
  • Sulphide containing ores are typically processed by roasting and/or smelting to oxidise some or all of the sulphidic component to facilitate subsequent extraction of metal values.
  • nickel sulphide ores are typically processed by smelting and refining techniques. These techniques may be complemented by an initial concentrating step prior to smelting to increase the metal content of the smelter feed.
  • Smelting of oxide ores for example laterite ores containing metal values such as nickel, chromium, iron and cobalt, requires very high temperatures for phase separation to produce ferro nickel, and high MgO levels for optimum slag and power consumption.
  • low MgO oxide ores require processing via acid pressure leaching requiring the separate manufacture of sulphuric acid to be supplied to the pressure leaching reactor.
  • the current smelting and refining techniques for processing sulphide ores and concentrates are restricted by the need to limit magnesium oxide levels in ores and concentrates and/or arsenic contents and/or selenium contents.
  • a further inefficiency is the high loss to the slag of cobalt values from smelted nickel cobalt ores and concentrates. Similar process and metal value recovery limitations can be encountered in the processing of other metal sulphide ores and concentrates.
  • separate processing has generally been required. This may involve physical separation of feed materials prior to treatment.
  • Separate processing also requires considerable additional resources which may preclude the establishment of separate processing facilities, such as at Leinster in Western Australia where sulphide and oxide ores containing nickel, cobalt, copper, zinc, gold and other metal values occur in the same ore body or nearby. Separate processing facilities generally involve lower efficiency leading to higher costs.
  • the present invention accordingly provides in one preferred embodiment a method for the treatment of a plurality of metal values in a feed containing sulphide and oxide components, the method including the step of oxidising the sulphide component in the feed at elevated temperature and pressure to generate an acid environment in-situ in which metal values from the sulphide and the oxide components are taken into solution and/or report to the solid phase in a form amenable to further treatment.
  • the present invention also provides in another preferred embodiment a method for the extraction of a plurality of metal values from a feed containing sulphide and oxide components, the method including the step of subjecting the feed in an aqueous environment to elevated temperature and pressure sufficient to oxidise the sulphide component in the feed to form an acid environment in-situ, wherein metal values from the sulphide and the oxide components are taken into solution in the acid phase and optionally also report to the solid phase in a form amenable to further processing, the method also including the further step of recovering metal values by subsequent recovery from the liquid phase and optionally the solid phase.
  • the present invention may be advantageously applied to feeds containing a variety of feed components including oxide and sulphide ores, concentrates and waste liquors, slags and tailings from other processes which contain metal values. Most preferably the present invention is applicable to feeds containing multiple base and/or precious metal values, ie feeds which contain three or more different base and/or precious metal values and which also contain sulphide and oxide components.
  • metal values is used herein to include metals not being impurities whether present in metallic, compound, mixed or other metal bearing forms.
  • the feed used in accordance with the present invention should contain sulphide and oxide components but may include other sulphur containing feed components such as sulphur itself, sulphur mattes and sulphur concentrates.
  • the sulphide and oxide components of a feed used in accordance with the present invention may be found in a single ore body or may be provided by a blended feed from multiple sources.
  • the present invention may be advantageously applied, for example, by mixing a predominantly sulphide ore (which may or may not contain oxide components) with a predominantly oxide ore (which may or may not contain sulphide components) to form a mixed feed for use in accordance with the invention.
  • the sulphide and oxide components of a feed used in accordance with the invention generate an acidic environment in the aqueous medium of the reaction vessel. It is convenient for the acid to be expressed in terms of sulphuric acid equivalent. It is to be appreciated however that the acidic environment is unlikely to consist solely of sulphuric acid (H2SO4).
  • the method provided by the present invention may also be advantageously applied in the presence of halide ions, for example, chloride ions. Such ions may be introduced into the reaction vessel from the feed materials themselves.
  • Another potential source of halide ions such as chloride ions is the water supply which may include, for example, seawater or hyper saline water from aquifiers.
  • the reaction can be expected to occur more quickly and/or give higher extraction levels in the presence of chloride ions. This may be attributed to the chloride ions favouring the generation of hydrochloric acid in the reaction environment. While it is convenient to refer herein to chloride ions as represented by hydrochloric acid it is to be appreciated that the acidic environment is unlikely to consist solely of hydrochloric acid (HC1).
  • HC1 hydrochloric acid
  • the feed used in accordance with the present invention may contain a variety of metal values and/or impurities including but not limited to nickel, cobalt, zinc, magnesium, copper, chromium, uranium, thorium and related radioactive elements, lead, rhodium, cadmium, vanadium, gallium, gold, silver, platinum and related precious metals.
  • the invention is particularly applicable to feeds containing a plurality of metal values.
  • the invention is preferably applied to a feed containing three or more different values.
  • Such a multiple metal feed may be found in a single deposit.
  • a mixed feed may be prepared by blending or mixing two or more feed components each containing one or more metal values.
  • the present invention may, for example, be applied to a mixed feed containing components from one or more separate ore bodies.
  • the metal values in each component of a mixed feed may be the same as or different from the metal values in each other component of the mixed feed.
  • the treatment at elevated temperature and pressure according to the present invention may be carried out in an autoclave or other pressure vessel.
  • other vessels capable of withstanding the temperatures, pressures and reaction conditions involved may also be used in accordance with the invention.
  • the treatment method provided by the present invention involves the use of elevated temperatures and pressures.
  • the method provided by the present invention should preferably be operated at temperatures of at least 180 C C.
  • the presently preferred temperature range is 180-280°Cwith a range of 200 to 220 °C being particularly preferred.
  • Equipment for use in accordance with the present invention is preferably designed on the desired temperature plus an oxygen over pressure allowance of up to 10 atmospheres.
  • the method provided by the present invention is carried out with oxygen overpressures in the range of 2 to 8 atmospheres.
  • the preferred temperature is typically about 250 C C or higher for maximising the recovery of multiple metal values.
  • the preferred temperature is typically about 250 C C or higher for maximising the recovery of multiple metal values.
  • temperatures in the region of 180-220°Ccan be expected to be generally acceptable.
  • Temperature, pressure, acid concentration and retention time all affect metal yields.
  • Each mix of oxides and sulphides is preferably optimised to achieve a preferred balance in the recovery, temperature, acid level, time and pressure relationships.
  • the feed components fed to the reaction vessel should be present in proportions suitable to achieve a balance between acid generating materials and acid consuming materials such that the leach discharge is controlled to a desired acid condition (gm/litre of free acid). This may require supplementary addition of acid, acid producing or acid consuming materials.
  • the acid condition in autoclave discharge is most preferably approximately 30-40 g/1 free acid as H2SO4 for lateritic ores which can contain chromium, cobalt, nickel and magnesium values.
  • H2SO4 free acid
  • the acid condition in autoclave discharge is most preferably approximately 30-40 g/1 free acid as H2SO4 for lateritic ores which can contain chromium, cobalt, nickel and magnesium values.
  • localised high concentrations of acid should be avoided.
  • Such localised high concentrations of acid give rise to undesirable scaling effects.
  • complex reactions can be expected to occur in the reaction vessel at the elevated temperatures and pressures which may be employed in accordance with the present invention. Variations in feed materials also influence the anticipated reactions.
  • compounds may dissociate and a variety of ions, some of which may be unstable, can be expected to occur. Accordingly the following example reactions are to be understood to be non-limiting and included for illustrative purposes only.
  • Examples of some non-limiting simplified nett reactions that consume acid and which may occur in performing a method provided by the present invention include:
  • NiO + H 2 S0 NiS0 + H 2 0
  • Examples of some non-limiting simplified nett reactions that produce acid and which may occur in performing a method provided by the present invention include:
  • the feed material used in accordance with the present invention may also be adjusted to achieve a heat balance between exothermic an endothermic heats of reaction.
  • the heat contents of the feed and exit streams from the reaction should be such that external heat energy requirements or cooling requirements in the leach system are autogenous or minimised with or without heat energy recycle from the reaction vessel discharge products to the feed materials.
  • the feed components may be pre-blended in the desired ratios and pumped into the reaction vessel as an aqueous slurry.
  • Other handling and charging techniques are also envisaged within the scope of the present invention. These may include, for example, operation of a batch autoclave.
  • the feed being preferably introduced as a slurry or slurries
  • other materials which may be added to the reaction vessel include water, oxygen, other oxidants, acid (if required) recycled leach solids discharge (after cooling) for reactor cooling as or if required, and steam for any required heating.
  • the reaction times required to achieve oxidation of the sulphidic components in the feed and leaching of metal values into the liquid or solid phases are typically in the range of 0.5-2.0 hours.
  • the metal values in a mixed feed may be contained in either the liquid phase or the solids phase or both depending upon the nature of the feed and the metals being extracted.
  • the reaction product is typically discharged in the form of a slurry which may require pH adjustment to facilitate recovery of individual metals in downstream processing.
  • the pH required for subsequent processing is dependent upon the metals to be recovered and the process to h ⁇ employed for extraction of the desired metals from the liquid and/or solids streams.
  • the pH may be kept relatively low (say about 2) during which time copper may be extracted by means such as solvent extraction. Subsequently, pH may be raised to remove iron eg. by precipitation at pH 3.5 to 4. Remaining valuable metals may be recovered after iron removal, for example by solvent extraction. This subsequent recovery of metals may be carried out in a series of steps involving increasing pH.
  • the form of downstream processing suitable for recovery of metal values is dependent upon the nature of the metal values to be extracted.
  • a wide variety of recovery techniques including but not limited to resin-in-pulp, solvent-in-pulp, precipitation, electrowinning, solvent extraction and leaching such as cyanidation followed by carbon-in-pulp or carbon-in-leach extraction and physical techniques are all envisaged within the scope of the present invention.
  • Hydroxamic acids which can exhibit very high levels of extraction of the desired metal ions into the solvent and can have the ability to operate over a wide pH range, ie in acidic and basic conditions, may be suitable for multiple metal extraction.
  • the treatment and extraction methods provided by the present invention provide a number of advantages over known prior art methods in that multiple sulphidic and oxide feed components can be processed through the one facility without any need for separation and that feed materials that are not generally considered economic for metal extraction may become economic for processing in accordance with the present invention. Further, feed materials not amenable to conventional processing such as high MgO and/or high arsenic sulphidic or oxide feeds may become economically treatable in accordance in the present invention. Also the cobalt in nickel smelter slags can be recovered and may become economically treatable in accordance with the present invention.
  • the methods provided by the present invention also facilitate the separation of desired metal values from undesired impurities. For example, desired metal values may be separated by selective extraction from solution of desired metal values from undesired impurities, or by separation of desired metal values taken into solution from undesired
  • the energy expenditure for process healing in the reaction vessel may be minimised or eliminated by use of the methods provided by the present invention and the invention may obviate the need for an acid production plant or the purchase of acid in a majority of circumstances where the sulphur balance in the feed is correctly proportioned - while at the same time avoiding sulphur dioxide production requiring subsequent processing.
  • FIGURE 1 is a block diagram of a simplified flow sheet for Example 1;
  • FIGURE 2 is a block diagram of a simplified flow sheet for Example 2.
  • FIGURE 3 is a block diagram of a simplified flow sheet for Example 3. 20 DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS
  • Ml Keith Concentrate may be formulated whereby the acid consuming constituents of the mixture balance with the acid producing constituents and a heat balance is achieved
  • This may optionally include recycle of cooled leach discharge to leach feed for control of the heat balance.
  • the Leinster Oxide Ore is a mixed nickel oxide/silicate ore from the Leinster area of Western Australia and the Leinster Secondary Concentrate is a concentrate formed from multiple metal sulphide ore containing nickel, cobalt, copper, gold, zinc, etc also 30 from the Leinster area of Western Australia.
  • the Mt Keith Concentrate is a similar multiple metal sulphide ore, however the Concentrate includes a high magnesia concentration which may cause difficulty in smelting by prior art methods.
  • the Mt Keith deposit is also in Western Australia.
  • a feed comprising a mixture of Leinster Oxide Ore, Leinster Secondary - r Concentrate and Mt Keith Concentrates is in this example embodiment introduced at ambient temperature into an autoclave by pumping in an aqueous slurry.
  • Oxygen is admitted into the autoclave to oxidise the sulphides generating an acid environment and to also oxidise the iron from sulphide minerals such as pentlandite, pyrrhotite and pyrite through to hematite.
  • Multiple metals are released into solution generating acid ions which leach the oxide metal values into solution and the sulphur forms sulphate ions.
  • Acid is consumed by magnesia minerals to form magnesium sulphate. Other acid consuming reactions include alunite and jarosite formation.
  • the preferred leach temperature is approximately 210-240°C with retention time at 0.75 to 1.5 hours and at a leach density of 35 to 45% solids and at an acid concentration of approximately 40g/l H2SO4.
  • Leach discharge is preferably flash cooled in one or more stages to ambient pressure and to temperatures below boiling point.
  • Flash cooled leach discharge is then further cooled as necessary.
  • the slurry then reports to solid liquid separation.
  • the pregnant acid liquor is neutralised to approximately pH4 using limestone and/or lime.
  • the solids from neutralisation are preferably recycled to solid liquid separation feed. (The pH adjustment could be done direct on the part cooled, or cooled leach discharge slurry).
  • the neutralised pregnant liquor is clarified then subjected to a solvent extraction stage to remove elements such as copper before being subjected to further stages for selective extraction of nickel, cobalt, zinc etc.
  • the loaded organics are in each case, preferably stripped with sulphuric acid.
  • Cobalt, copper, zinc and/or manganese may be recovered from their respective strip liquor or rejected.
  • Nickel may be recovered from its respective strip liquor.
  • FIGURE 1 A block diagram of a simplified flow sheet for this example of one possible use of the methods provided by the present invention for the recovery of nickel values from mixed nickel sulphide and nickel oxide ores is included herein as FIGURE 1.
  • nickel oxides can be high in silica (40 to 60% Si ⁇ 2) and contain more than 1% Ni and approximately 0.1% Co.
  • a mixed feed of nickel oxide, auriferous pyrite and convenor slag may be fed to an autoclave and processed in accordance with the present invention as set out in the flowsheet included herein as FIGURE 2.
  • the nickel oxide ore is used as the acid sink and as a source of nickel and cobalt.
  • the refractory auriferous pyrites is used as an in-situ energy and acid source and in doing so the need to roast is eliminated. There is an environmental advantage in that sulphur no longer reports to atmosphere as sulphur dioxide.
  • Gold from the pyrites is eventually recovered from washed autoclave discharge solids via the well known CIP/CIL techniques. Cyanided free milling pyrite is added to the autoclave as a further source of an in-situ energy and acid which results in the recovery of further gold. This source of pyrite is presently discharged to tailings dams.
  • Convenor slag may be added as a source of nickel and cobalt.
  • the slag may have some energy value from encapsulated matte/sulphides but will be largely neutral in respect to being an acid consumer.
  • Cobalt extracted from slag into solution should be in the order of 95 to 98%.
  • Residual gold left in the solids phase after cyanidation will be typically 1 g/t less than if the auriferrous pyrite was cyanided directly.
  • Pressure oxidised auriferous pyrite is more amenable to cyanidation than direct cyanidation of auriferrous pyrite.
  • Copper concentrate from Nifty and copper/gold concentrate from Telfer may be sent to Leinster and pressure oxygen leached in conjunction with Leinster nickel oxide ores in accordance with the invention to produce nickel, cobalt, copper and/or zinc and/or gold etc.
  • Leinster at Yeelirrie there occurs a large calcrete uranium ore body. The calcrete reacts very readily with cold dilute acid and could be used in lieu of limestone for acid neutralisation purposes outside of the leach autoclave. Uranium could therefore also be produced and this also applies to the EXAMPLE NO. 1.
  • Advantages of combining the Nifty and Telfer concentrates, together with the Leinster metal oxide ore to form a feed in accordance with the present invention include: Allows the Nifty sulphide ore body to be brought into production (Nifty oxide ores will be depleted well before Nifty sulphides are depleted but nevertheless, a combined Nifty sulphide and Nifty oxide ores pressure leach could be contemplated. Nifty currently imports acid for its heap leach operations).
  • FIGURE 3 A block flowsheet for the process of EXAMPLE NO. 3 is included herein as FIGURE 3.

Abstract

Un traitement permet de lessiver une charge mélangée contenant plusieurs métaux présentant une valeur, dans un autoclave par oxydation des éléments contenant du soufre pour produire in situ de l'acide sulfurique. Les éléments de la charge sont choisis de façon à donner un équilibre acide approprié lors de l'oxydation. La boue résultant de ce lessivage est neutralisée et les métaux récupérés par des procédés tels que l'extraction électrolytique, la cyanuration, l'extraction par solvant, etc., après qu'elle soit passée par une étape de séparation des solides et des liquides.
PCT/AU1995/000573 1994-09-05 1995-09-04 Traitement de mineraux WO1996007762A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU33773/95A AU3377395A (en) 1994-09-05 1995-09-04 Mineral processing

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AUPM7908A AUPM790894A0 (en) 1994-09-05 1994-09-05 Mineral processing
AUPM7908 1994-09-05

Publications (1)

Publication Number Publication Date
WO1996007762A1 true WO1996007762A1 (fr) 1996-03-14

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Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6641642B2 (en) 2001-12-21 2003-11-04 Newmont Usa Limited High temperature pressure oxidation of ores and ore concentrates containing silver using controlled precipitation of sulfate species
WO2010031137A1 (fr) * 2008-09-19 2010-03-25 Murrin Murrin Operations Pty Ltd Procédé hydrométallurgique permettant de lixivier des métaux de base
WO2013020175A1 (fr) 2011-08-08 2013-02-14 Xstrata Queensland Limited Traitement de matières sulfurées
EP2288736A4 (fr) * 2008-06-13 2015-10-21 Poseidon Nickel Ltd Procédé de récupération de métaux de base à partir de minerais
EP2288735A4 (fr) * 2008-06-13 2016-05-11 Poseidon Nickel Ltd Procédé rhéologique pour la récupération hydrométallurgique de métaux de base à partir de minerais
WO2018187855A1 (fr) * 2017-04-14 2018-10-18 Sherritt International Corporation Lixiviation oxydative sous pression, à faible acidité et faible teneur en solides, de charges sulfurées
US20210156003A1 (en) * 2017-08-08 2021-05-27 Cobalt Blue Holdings Ltd Recovery of metals from pyrite

Citations (9)

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GB1189957A (en) * 1967-06-12 1970-04-29 Union Carbide Canada Ltd Simultaneous Leaching of Zinc and Manganese Ores
US4084961A (en) * 1976-09-10 1978-04-18 Sunshine Mining Company Treatment of metal bearing mineral material
SU870475A1 (ru) * 1979-12-12 1981-10-07 Государственный проектный и научно-исследовательский институт "Гипроникель" Способ переработки окисленной пульпы
GB2108480A (en) * 1981-10-30 1983-05-18 Sherritt Gordon Mines Ltd Acid leach process for treating magnetic and non-magnetic nickel-copper mattes
EP0096499A1 (fr) * 1982-06-03 1983-12-21 Sherritt Gordon Mines Limited Récupération de zinc à partir de matières zincifères sulfurées
EP0100237A2 (fr) * 1982-07-27 1984-02-08 Sherritt Gordon Mines Limited Extraction de zinc de matières sulfurées zincifères
US4472359A (en) * 1981-02-27 1984-09-18 Metallgesellschaft Ag Method of pressure leaching
AU3089384A (en) * 1983-07-22 1985-01-24 California Nickel Corp. Liberating nickel and cobalt enriched fines from laterite ore
US4548794A (en) * 1983-07-22 1985-10-22 California Nickel Corporation Method of recovering nickel from laterite ores

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Publication number Priority date Publication date Assignee Title
GB1189957A (en) * 1967-06-12 1970-04-29 Union Carbide Canada Ltd Simultaneous Leaching of Zinc and Manganese Ores
US4084961A (en) * 1976-09-10 1978-04-18 Sunshine Mining Company Treatment of metal bearing mineral material
SU870475A1 (ru) * 1979-12-12 1981-10-07 Государственный проектный и научно-исследовательский институт "Гипроникель" Способ переработки окисленной пульпы
US4472359A (en) * 1981-02-27 1984-09-18 Metallgesellschaft Ag Method of pressure leaching
GB2108480A (en) * 1981-10-30 1983-05-18 Sherritt Gordon Mines Ltd Acid leach process for treating magnetic and non-magnetic nickel-copper mattes
EP0096499A1 (fr) * 1982-06-03 1983-12-21 Sherritt Gordon Mines Limited Récupération de zinc à partir de matières zincifères sulfurées
EP0100237A2 (fr) * 1982-07-27 1984-02-08 Sherritt Gordon Mines Limited Extraction de zinc de matières sulfurées zincifères
AU3089384A (en) * 1983-07-22 1985-01-24 California Nickel Corp. Liberating nickel and cobalt enriched fines from laterite ore
US4548794A (en) * 1983-07-22 1985-10-22 California Nickel Corporation Method of recovering nickel from laterite ores

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Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6641642B2 (en) 2001-12-21 2003-11-04 Newmont Usa Limited High temperature pressure oxidation of ores and ore concentrates containing silver using controlled precipitation of sulfate species
EP2288736A4 (fr) * 2008-06-13 2015-10-21 Poseidon Nickel Ltd Procédé de récupération de métaux de base à partir de minerais
EP2288735A4 (fr) * 2008-06-13 2016-05-11 Poseidon Nickel Ltd Procédé rhéologique pour la récupération hydrométallurgique de métaux de base à partir de minerais
WO2010031137A1 (fr) * 2008-09-19 2010-03-25 Murrin Murrin Operations Pty Ltd Procédé hydrométallurgique permettant de lixivier des métaux de base
AU2009295281B2 (en) * 2008-09-19 2015-03-26 Murrin Murrin Operations Pty Ltd A Hydrometallurgical method for leaching base metals
WO2013020175A1 (fr) 2011-08-08 2013-02-14 Xstrata Queensland Limited Traitement de matières sulfurées
US8999274B2 (en) 2011-08-08 2015-04-07 Glencore Queensland Limited Treatment of sulphidic materials
WO2018187855A1 (fr) * 2017-04-14 2018-10-18 Sherritt International Corporation Lixiviation oxydative sous pression, à faible acidité et faible teneur en solides, de charges sulfurées
US11118244B2 (en) 2017-04-14 2021-09-14 Sherritt International Corporation Low acidity, low solids pressure oxidative leaching of sulphidic feeds
US20210156003A1 (en) * 2017-08-08 2021-05-27 Cobalt Blue Holdings Ltd Recovery of metals from pyrite

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