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WO2009026693A1 - Processus hydrométallurgique de récupération distincte du nickel et du cobalt à l'aide de résines échangeuses d'ions - Google Patents

Processus hydrométallurgique de récupération distincte du nickel et du cobalt à l'aide de résines échangeuses d'ions Download PDF

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Publication number
WO2009026693A1
WO2009026693A1 PCT/CA2008/001508 CA2008001508W WO2009026693A1 WO 2009026693 A1 WO2009026693 A1 WO 2009026693A1 CA 2008001508 W CA2008001508 W CA 2008001508W WO 2009026693 A1 WO2009026693 A1 WO 2009026693A1
Authority
WO
WIPO (PCT)
Prior art keywords
nickel
cobalt
resin
recovery
pulp
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/CA2008/001508
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English (en)
Inventor
Flavia Dutra Mendes
Tiago Valentim Berni
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.)
Vale Canada Ltd
Original Assignee
Vale Canada Ltd
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Filing date
Publication date
Application filed by Vale Canada Ltd filed Critical Vale Canada Ltd
Publication of WO2009026693A1 publication Critical patent/WO2009026693A1/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
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/42—Treatment or purification of solutions, e.g. obtained by leaching by ion-exchange extraction
    • 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
    • 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
    • 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
    • C22B23/0461—Treatment or purification of solutions, e.g. obtained by leaching by chemical methods
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0476—Separation of nickel from cobalt
    • 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
    • C22B23/0476—Separation of nickel from cobalt
    • C22B23/0484—Separation of nickel from cobalt in acidic type solutions
    • 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
    • C22B3/10—Hydrochloric acid, other halogenated 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 is related to the field of hydrometallurgical techniques for recovery of nickel and cobalt.
  • Chelating polymeric resins are examples of ionic exchangers very efficient in selectively removing heavy metals (such as nickel and cobalt) when compared to other exchangers.
  • These ionic-exchange polymeric resins are copolymers with covalently-linked functional groups, containing one or more donor atoms (Lewis Base). They can form coordinated bindings with most metal ions (Lewis Acid). Coulombic and hydrophobic interactions are also present, but their contribution in high metal-ion selectivity is rather small when compared to the Lewis acid-base interactions.
  • the iminodiacetic acid functional group the presence of weak acid clusters leads this exchanger to display high affinity for H+ ions. Hence, the lower the pH, the less selective is recovery of metal ions in view of competition with H+ ions.
  • These resins can normally be regenerated with acid solutions (sulfuric or chloride acid, for instance) and such regeneration is highly efficient.
  • Amberlite IRC 748 ® Both are chelating-type resins with different functional groups and made by different producers.
  • Dow Chemical Company has reported a series of chelating resins, among them Dowex M4195 ® , which is efficient in adsorbing transition metal cations, with high selectivity for copper, nickel and cobalt in the presence of high iron concentrations in a very acid medium (K.C. Jones, et al., "Continuous Recovery from Acidic Leach Liquids by Continuous Ion-Exchange and Electrowinning", Journal of Metals, pp. 19-25, April 1979).
  • This resin comprises a macroporous polistyrene/divinilbenzene-type copolymer, to which is affixed weak-base derived picolylamine chelating: bis-picolylamine (L.
  • M4195 its overall structure is based on the weakly-basic bis- picolilamine chelating group, which is covalently linked to the polestirene-divinilbenzene copolymer (see Table 2).
  • M4195 is the resin most often cited in the literature. However, no record was found of Ni/Co recovery in nickel lateritic ore treatment processes.
  • M4195 resin's functional clustering acts as a complexant agent more efficient for nickel, when compared to other resins, in the entire pH range.
  • its selectivity for cobalt is considerably less.
  • Cobalt which is swiftly adsorbed in initial loading (charging), soon desorbs, due to nickel's preferential selectivity.
  • Cu and Ni are effectively adsorbed, even at low pH values, in the following adsorption order: Cu>Ni>Co>Zn>Al.
  • Amberlite IRC 748 ® is a chelating-type resin with high selectivity for heavy metal cations, if compared to alkaline metals. Selectivity is reached by the iminodiacetic acid functional group chemically linked to a macroreticular matrix. According to its maker, Rohm & Haas Company, given its high selectivity for heavy metals and outstanding kinetic performance, this resin can remove metals from the solution, even in the presence of high concentration of calcium and sodium salts. Moreover, its macroreticular structure is highly resistant to osmotic shock and features excellent physical stability. Table 3 below shows the structure of the iminodiacetic acid functional group and some physical properties.
  • Industrial units which use hydrometallurgical processing to recover nickel and cobalt include a countercurrent multi-stage settling circuit, which is responsible for separating solid-liquid and washing solids, in order to maximize nickel and cobalt recoveries from the leaching effluent pulp.
  • a series of corrosion-resistant thickeners is used. However, they involve high capital and operating cost, occupy large areas and consume significant amounts of washing water.
  • An option replacing costly countercurrent settlement is to use a RIP system. This is used to recover nickel and cobalt from leached pulp, with no need to use thickeners.
  • nickel and cobalt would be individually recovered, separated and purified via continuous ionic exchange in countercurrent, for instance, based on concentrated eluant solution. This eluant solution could be based on chloride or sulfide. Final recovery could occur through electrolysis, pyrohydrolysis, reduction via hydrogen or precipitation methods, among other forms.
  • RIP technology can be used to enhance pre-existing systems or to replace conventional technologies. In cases wherein process engineering is taken into account, this technology could substitute counter current decantation ("CCD") technology and reduce environmental impact. In operating plants using the CCD process, RIP technology can improve the pre-existing technology, increase metal recovery and improve their purity, in addition to reducing environmental impact. This alternative, coupled to the solid-liquid separation circuit, becomes particularly attractive in cases wherein Iateritic ores are hampered by constrains (long deposition time) to CCD circuit processing, triggering metal losses in residues.
  • CCD counter current decantation
  • RIP is a process in which the ionic exchange polymeric resin directly contacts the leaching pulp in countercurrent. Sieve screening separates resin from pulp, and metals in the resin are recovered through elution. This system is commonly used in commercial uranium recovery, especially for low-grade and hard-to-settle pulps.
  • the carbon-in-pulp (“CIP") process has a similar concept, where coal (carbon) performs a role similar to resin's in the RIP process.
  • RIP technology's chief characteristic is the "sorption-leaching" phenomenon. In it, ionic exchange continuously removes nickel and cobalt from the liquid phase, allowing subsequent leaching. Therefore, an additional amount of nickel and cobalt is recovered from the pulp's solid portion, which is normally not recovered in other processes.
  • IONEX Continuous ionic exchange
  • the continuous ionic exchange system makes a large number of functions simultaneously possible, given its continuous operation, thus allowing the system to enjoy great flexibility.
  • the IONEX system can be adjusted in a pre-existing fixed resin bed or in a mobile bed system. Locating existing resin vases is not relevant, which translates into process advantages and less operating costs, with no need of a full upgrade.
  • Duyvesteyn, et al. describes a process for selectively recovering nickel by ion exchange absorption from a Ni/Co sulfuric acid feed solution obtained from limonite ore which is pressure leached with sulfuric acid and then neutralized and solid/liquid separated, containing nickel in the range of about 0.5 to 40 gpl and cobalt in the range of about 0.01 to 2 gpl as sulfates.
  • the document describes that the absorbed nickel is stripped from said resin with sulfuric acid to form a nickel sulfate solution characterized by a nickel to cobalt ratio of at least about 50: 1 suitable for the recovery of substantially pure nickel by electrolysis.
  • the document refers to the recovery of nickel merely by electrolysis, which is a well known method for this specific technology and it also uses the solid/liquid separation.
  • Stream" to D. Krebs is directed to recovery of nickel and cobalt from acidic resin eluate containing Ni and Co, treating the eluate with immiscible organic reagent to selectively absorb the majority of Co, and portion of any copper, zinc and manganese present in the eluate, but it does not mention the recovery of nickel as oxide and the method for separating both metals used therein is by the traditional extraction-by-solvents methods.
  • Laterite Ores By Combination Of Atmospheric And Moderate Pressure Leaching to D. Neudorf, et al., describes a process for leaching laterite ores containing limonite and saprolite. Sufficient mineral acid is added to a slurry of limonite, which is leached at atmospheric pressure to dissolve most of the soluble non-ferrous metals and soluble iron. After adding saprolite the slurry is further leached at a temperature above the normal boiling point and at a pressure above atmospheric pressure for a time sufficient to leach most of the contained nickel in the saprolite and to precipitate most of the iron in solution.
  • nickel and/or cobalt can be recovered by several types of methods, without defining which would be the best one for the recovery, apart from the fact that it uses the traditional method of autoclave to leach most of the contained nickel in the saprolite ore and to precipitate most of the iron in solution.
  • the present invention deals with a hydrometallurgical process to produce nickel as hydroxide, oxide or cathode and produce cobalt preferably as sulfides.
  • the present invention is particularly adequate to process eluate containing nickel and cobalt.
  • Eluates are solutions obtained from elution of ionic exchange resins, loaded (charged) in the RIP (resin- in-pulp) process of ionic exchange, to recover nickel and cobalt from effluent pulps in acid leaching. Following nickel and cobalt recovery in a RIP circuit, they are separated from each other via a continuous ionic exchange process, after which the nickel eluate is formed to produce nickel as nickel oxide by a pyrohydrolysis process, which is the key stage of the invention.
  • Figure 1 is a prior art schematic representation flowchart for RIP (resin-in- pulp).
  • Figure 2 is a schematic representation of the invention.
  • the present invention in accordance with Figure 2, refers specifically to a hydrometallurgical process seeking to recover nickel and cobalt.
  • the present invention replaces the conventional extraction-by-solvents methods used so far in the prior art as shown in Figure 1 to recover nickel and/or cobalt.
  • the use of pyrohydrolisis to produce nickel oxide and to regenerate acid with the use of the continuous ion exchange technology to separate nickel and cobalt contained in the eluate obtained in the previous RIP (resin-in-pulp) stage provides specific characteristics to the present invention.
  • IONEX has a unique valve that allows one to easily change flows, switching from a loading step to a elution step faster and easily. This new method allows one to separate nickel and cobalt, using different loading (charging) and elution times.
  • Eluate obtained in the previous RIP operation contains high concentrations of nickel and cobalt, which must be separated through continuous ionic exchange and countercurrent systems.
  • Nickel and cobalt are separated through the use of ionic exchange resins for selective nickel recovery.
  • the resin adsorbs all or most of the nickel dissolved in solution, leaving all or most of the remaining cobalt in solution with impurities.
  • Cobalt is then precipitated as sulfide, hydroxide or carbonates, and nickel is eluted from the resin and recovered in a wide-range of different products, as precipitate in the form of hydroxide, oxide via pyrohydrolysis, with HCI regeneration or electro-recovered as cathode nickel.
  • the present process leads to expectations of efficient recovery of metals of interest, selective removal of low concentrations of metal ions, such as cobalt, preferably in excess of other metals, high loading (charging), high mechanical resistance which reduces friction-caused losses, swift elution, and minimal or no loss due to organic material contamination.
  • metal ions such as cobalt
  • Pyrohydrolysis may be regarded as a key stage in the present invention.
  • chloride acid regeneration is an environmental necessity. In many hydrometallurgical processes, it is essential to recover the leaching agent (HCl, Cl 2 , FeCl 3 ), since discarding it with dissolved metals is economically and ecologically unacceptable.
  • the second major advantage is the economic savings obtained in acid regeneration, as reagents' operation cost is minimized. High recovery (roughly 99%) of high-purity acid is common, and this is vitally important if the objective is to sell chloride acid.
  • NiCl 2 a concentrated NiCl 2 solution can be produced. This solution can undergo pyrohydrolysis, generating NiO and HCl, or undergo electrolysis, generating metallic nickel and chloride gas. In order to obtain metal from NiO, oxide must be reduced with H 2 at a 750 0 C temperature.
  • electrolysis has some drawbacks: chloride necessary for HCI production is generated in small amounts in many anodes, and it must be carefully collected and treated. Electric power generation is costly and its efficiency is only 35%. Pyrohydrolysis produces nickel oxide in one single stage, but it also simultaneously produces chloride gas, which is absorbed in water. Metal reduction can be carried out in a separate furnace, with H 2 stoichiometric addition. In such cases, granular nickel oxide is preferred, because in its fine form it can agglomerate around the reduction furnace. Nickel pyrohydrolysis occurs at relatively high temperatures, above 12TC.
  • Thermodynamic data reveal that, if the temperature drops down to 700°C, reverse NiO reaction occurs, generating NiCl 2
  • the exact temperature depends on the HCI/H 2 O ratio in the gas. In partial HCI high pressure, reverse reaction forming NiCl 2 occurs at temperatures above 700°C.
  • the present invention refers, specifically, to a hydrometallurgical process for recovery of nickel and cobalt, as follows: a. apply to a pulp resulting from lateritic ore leaching, nickel oxidate, cobalt oxidate or a mixture with nickel and cobalt as metals of interest, and other secondary metals regarded as impurities such as manganese, magnesium, calcium, aluminum, iron and chromium; b. possible pH adjustment aided by acid or base, so as to best fit metal solubilization/precipitation performance and, simultaneously, an optimal and selective loading of nickel and cobalt in the resin; c.
  • leached pulp contacts ionic exchange resin, in a RIP process, to obtain resin loaded with nickel and cobalt plus an impurity-bearing raffinate d.
  • loaded resin is separated from pulp via screening; e. nickel and cobalt eluted from resin, to form eluate bearing nickel soluble salt and cobalt soluble salt as well as impurities; f. possible reduction of soluble impurity species or use of cementing/complexation techniques, in order to avoid resin adsorption in next stage; g. eluate obtained contacts ionic exchange resin, to load nickel in resin and remaining cobalt in raffinate, so as to secure nickel-cobalt separation; h.
  • nickel-bearing resin is separated from raffinate concentrate in cobalt; i. nickel-bearing resin is eluated in acid solution, wherein a feature of the invention is in the fact that nickel and cobalt are separately recovered, in which cobalt is precipitated as sulfide, hydroxide or carbonates and nickel is eluted from the resin and recovered in a wide-range of different products, as precipitate in the form of hydroxide, electro-recovered as cathode nickel or as nickel oxide via pyrohydrolysis at relatively high temperatures, above about 727°C, with HCT regeneration.
  • RIP resin-in- pulp
  • Leaching may occur under atmospheric conditions and at temperature below 100 0 C or under high pressure and at high temperature.
  • RIP is a three-stage circuit.
  • nickel and cobalt are selectively recovered in mechanically stirred or in air-stirred (pachuca) vats.
  • Resins suggested for this type of use are those in iminodiacetic and picolylamine groups.
  • Contact between resin and pulp occurs in countercurrent, with intermediate sieves between the vats, for the sake of phase separation.
  • Effluent resin in the first adsorption vat is withdrawn from the circuit, taken to removal of aggregate solids, and transferred to the elution circuit.
  • Elution of resin-loaded metals that can occur selectively and in multiple stages must occur with sulfuric, chloride or nitric acid, at a concentration range of 50g/L - 150g/L approximately.
  • Regeneration is the stage wherein the eluted resin is placed in contact with a reagent (such as soda or limestone), to be regenerated and resume calcium or sodium forms.
  • a reagent such as soda or limestone

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

Abstract

La présente invention concerne un processus hydrométallurgique pour produire du nickel comme hydroxyde, oxyde ou cathode et pour produire du cobalt de préférence sous forme de sulfures. La présente invention est notamment appropriée pour traiter un éluat contenant du nickel et du cobalt. Les éluats sont des solutions obtenues à partir de l'élution de résines échanges d'ions, chargées dans le procédé d'échange ionique de résine en pulpe (RIP), pour récupérer du nickel et du cobalt à partir de pulpes d'effluents dans la lixiviation de l'acide. Après récupération du nickel et du cobalt dans un circuit de résine en pulpe, ceux-ci sont séparés l'un de l'autre par un procédé continu d'échange ionique, après quoi l'éluat de nickel est formé pour produire du nickel comme oxyde de nickel par un processus de pyrohydrolyse.
PCT/CA2008/001508 2007-08-29 2008-08-27 Processus hydrométallurgique de récupération distincte du nickel et du cobalt à l'aide de résines échangeuses d'ions Ceased WO2009026693A1 (fr)

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US96861907P 2007-08-29 2007-08-29
US96861407P 2007-08-29 2007-08-29
US60/968,614 2007-08-29
US60/968,619 2007-08-29

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Cited By (2)

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WO2010037169A1 (fr) * 2008-10-01 2010-04-08 The University Of Queensland Procédé pour l’extraction de matériau minier
WO2013120131A1 (fr) * 2012-02-14 2013-08-22 Bhp Billiton Ssm Development Pty Ltd Production d'un produit de nickel de haute qualité

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FR2925349A1 (fr) * 2007-12-20 2009-06-26 Applexion Procede de separation sequence multicolonnes d'un derive metallique ionique
AU2012212348B2 (en) * 2011-02-01 2016-08-18 Vale S.A. Direct purification of a nickel laterite leaching effluent
JP6009218B2 (ja) * 2011-05-24 2016-10-19 ローム アンド ハース エレクトロニック マテリアルズ エルエルシーＲｏｈｍ ａｎｄ Ｈａａｓ Ｅｌｅｃｔｒｏｎｉｃ Ｍａｔｅｒｉａｌｓ ＬＬＣ アルファ粒子放射体除去
WO2013096070A1 (fr) 2011-12-20 2013-06-27 Freeport-Mcmoran Corporation Systèmes et procédés de récupération de métal
US9068247B2 (en) 2012-05-01 2015-06-30 Dow Global Technologies Llc Nickel and cobalt recovery using continuous ion exchange
CN103553155B (zh) * 2013-11-12 2016-08-31 金川集团股份有限公司 一种处理红土矿中间产物的方法
CN111777245A (zh) * 2019-04-04 2020-10-16 中国科学院过程工程研究所 一种从硫酸镍萃余液中回收硫酸钠的方法
WO2024235328A1 (fr) * 2023-05-18 2024-11-21 中伟新材料股份有限公司 Procédé d'élimination d'impuretés d'une suspension de lixiviation d'hydroxyde métallique brut, procédé d'élimination d'impuretés d'hydroxyde métallique brut, et procédé de préparation de sulfate
EP4524109A4 (fr) * 2023-07-26 2025-10-15 Pt Qmb New Energy Mat Méthode de préparation d'une solution de sulfate de nickel-cobalt-manganèse de qualité batterie à partir d'une matte à faible teneur en nickel
CN117222765A (zh) * 2023-07-31 2023-12-12 青美邦新能源材料有限公司 一种从红土镍矿中绿色低成本提取镍钴的方法

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US4320099A (en) * 1980-07-28 1982-03-16 Inco Limited Process for nickel removal from concentrated aqueous cobaltous sulfate solutions
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CA2572420A1 (fr) * 2004-08-02 2006-03-23 Skye Resources Inc. Procede permettant de recuperer du nickel et du cobalt a partir de minerais de laterite par combinaison de lixiviation a pression atmospherique et a pression moderee

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US4214901A (en) * 1979-02-16 1980-07-29 Amax Inc. Hydrometallurgical refining of nickeliferous sulfides
US4320099A (en) * 1980-07-28 1982-03-16 Inco Limited Process for nickel removal from concentrated aqueous cobaltous sulfate solutions
WO1996020291A1 (fr) * 1994-12-27 1996-07-04 Bhp Minerals International Inc. Recuperation du nickel et du cobalt contenus dans des minerais laterises
US5571308A (en) * 1995-07-17 1996-11-05 Bhp Minerals International Inc. Method for recovering nickel from high magnesium-containing Ni-Fe-Mg lateritic ore
WO2002038819A2 (fr) * 2000-11-08 2002-05-16 Hatch Associates Ltd. Procede de regeneration de solutions d'halogenure acide
WO2006029443A1 (fr) * 2004-09-17 2006-03-23 Bhp Billiton Ssm Technology Pty Ltd Production de mattes de ferronickel ou de nickel au moyen d'un procede combine d'hydrometallurgie et de pyrometallurgie
WO2008080209A1 (fr) * 2006-12-29 2008-07-10 Companhia Vale Do Rio Doce Procédé d'obtention de nickel et de cobalt à partir d'un éluat de résine échangeuse d'ions, et produit

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010037169A1 (fr) * 2008-10-01 2010-04-08 The University Of Queensland Procédé pour l’extraction de matériau minier
WO2013120131A1 (fr) * 2012-02-14 2013-08-22 Bhp Billiton Ssm Development Pty Ltd Production d'un produit de nickel de haute qualité
US9481919B2 (en) 2012-02-14 2016-11-01 Cerro Matoso Sa Production of high grade nickel product

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