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US20090056502A1 - Hydrometallurgical process for recovery of nickel and cobalt - Google Patents

Hydrometallurgical process for recovery of nickel and cobalt Download PDF

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Publication number
US20090056502A1
US20090056502A1 US12/197,403 US19740308A US2009056502A1 US 20090056502 A1 US20090056502 A1 US 20090056502A1 US 19740308 A US19740308 A US 19740308A US 2009056502 A1 US2009056502 A1 US 2009056502A1
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United States
Prior art keywords
nickel
cobalt
resin
recovery
pulp
Prior art date
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Abandoned
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US12/197,403
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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 SA
Vale Canada Ltd
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Vale Canada Ltd
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Publication date
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Priority to US12/197,403 priority Critical patent/US20090056502A1/en
Publication of US20090056502A1 publication Critical patent/US20090056502A1/en
Assigned to VALE S.A. reassignment VALE S.A. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: BERNI, TIAGO VALENTIM, MENDES, FLAVIA DUTRA
Abandoned legal-status Critical Current

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    • 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.
  • Main methods can be chemical or physical-chemical. Examples of the former are chemical oxidation and chemical precipitation. Examples of the latter are adsorption in activated coal, ionic exchanger and extraction via solvents. There are also physical, electro-chemical and biological methods.
  • 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.
  • 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 picolylarnine 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, Rohin & 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 calciun 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 ftnctional 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 lateritic 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
  • Enhanced productivity The continuous ionic exchange system provides more efficient and productive recovery, if compared to non-continuous systems, given its real countercurrent configuration. Previous experiences with processes such as lysine, potassium, salt and antibiotic production have shown that production can increase in the 5% to 10% range when the IONEX system is used. Enhanced productivity generates further recoveries and increased revenue.
  • the continuous ionic exchange systems offers stronger reliability based on fewer mobile mechanical parts, if compared to the other systems.
  • Non-continuous systems need countless automatic valves, and mobile resin beds needs a carrousel-type systems and flexible connections. Higher reliability leads to more availability, which, in turn, is conducive to additional production and lower maintenance cost.
  • the internal disk is the only mobile component in the IONEX system. Systems with numerous automatic valves and carrousel systems with a rotary platform to physically move the resin's bed are eliminated.
  • 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.
  • WO 01/29276A1 “Resin-In-Pulp Method For Recovery Of Nickel And Cobalt From Oxidic Ore Leach Slurry” to W.
  • Duyvesteyn, et al. refers to a process for the recovery of nickel and cobalt from nickeliferous oxide ore leach slurry by ion exchange. It also teaches that nickel and/or cobalt are recovered by known processes. Thus, the proposed process fails in recovering precipitated cobalt and nickel as oxide with HCl regeneration.
  • WO 962/0291 “Recovery Of Nickel And Cobalt From Laterite Ores” to W. 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 solidaiquid separation.
  • WO 2007/087698 “Hybrid Process Using Ion Exchange Resins In The Selective Recovery Of Nickel And Cobalt From Leaching Effluents” to R. Costa, et al. (and the present co-inventor) is directed to a hybrid process using ion exchange resins in the selective recovery of nickel and cobalt of leaching effluents that is comprised of the steps of processing the. laterite ore, which is then treated through leaching (either atmospheric or under pressure), considering solutions from the solid-liquid separation step of existing plants already in operation as well, in a way that the downstream process comprises an ion exchange hybrid circuit. Even though the document is related to the recovery of nickel and cobalt, it still mentions the solid-liquid separation and does not suggest stages of obtaining nickel oxide.
  • WO 2006/069416 “Extraction Of Nickel And Cobalt From A Resin Eluate 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.
  • 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.
  • RIP reactive-in-pulp
  • FIG. 1 is a prior art schematic representation flowchart for RIP (resin-in-pulp).
  • FIG. 2 is a schematic representation of the invention.
  • the present invention in accordance with FIG. 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 FIG. 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 HCl 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. Indeed, this stage generates the end product—nickel as oxide—and chloride acid is regenerated in order to be reused in the process, preferably in elution of the loaded (charged) resin.
  • 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.
  • Some hydrometallurgical processes have metal oxide as the desired end product and HCl regeneration as the byproduct.
  • 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° C. temperature.
  • 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 HCl/H 2 O ratio in the gas. In partial HCl 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:
  • RIP resin-in-pulp
  • Leaching may occur under atmospheric conditions and at temperature below 100° 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 50 g/L-150 g/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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US12/197,403 2007-08-29 2008-08-25 Hydrometallurgical process for recovery of nickel and cobalt Abandoned US20090056502A1 (en)

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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100326918A1 (en) * 2007-12-20 2010-12-30 Applexion Multi-column sequenced separation process for separating an ionic metal derivative
US20120298586A1 (en) * 2011-05-24 2012-11-29 Dow Global Technologies Llc Alpha-particle emitter removal
WO2013165735A1 (fr) * 2012-05-01 2013-11-07 Dow Global Technologies Llc Récupération de nickel de cobalt en utilisant l'échange d'ions continu
CN103553155A (zh) * 2013-11-12 2014-02-05 金川集团股份有限公司 一种处理红土矿中间产物的方法
JP2014509349A (ja) * 2011-02-01 2014-04-17 ヴァーレ、ソシエダージ、アノニマ ニッケルラテライト浸出廃液の直接精製
US9481919B2 (en) 2012-02-14 2016-11-01 Cerro Matoso Sa Production of high grade nickel product
US10246789B2 (en) 2011-12-20 2019-04-02 Freeport Minerals Corporation Systems and methods for copper recovery via roasting and leaching
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
CN117295694A (zh) * 2023-07-26 2023-12-26 青美邦新能源材料有限公司 一种低冰镍制备电池级硫酸镍钴锰溶液的方法
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
US20250170496A1 (en) * 2023-07-31 2025-05-29 Pt Qmb New Energy Materials Method for green and low-cost extraction of nickel-cobalt from laterite nickel ore

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* 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

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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
US6350420B1 (en) * 1999-10-15 2002-02-26 Bhp Minerals International, Inc. Resin-in-pulp method for recovery of nickel and cobalt
US6524367B1 (en) * 1997-02-18 2003-02-25 Centro De Investigaciones Para La Industria Minero-Metalurgcia (Cipimm) Hydrometallurgical process for the recovery of nickel and cobalt by ammoniacal leaching
US20060024224A1 (en) * 2004-08-02 2006-02-02 David Neudorf Method for nickel and cobalt recovery from laterite ores by combination of atmospheric and moderate pressure leaching

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US6692719B1 (en) * 2000-11-08 2004-02-17 Hatch Ltd. Process for regeneration of acid halide solutions
JP2008513597A (ja) * 2004-09-17 2008-05-01 ビーエイチピー・ビリトン・エスエスエム・テクノロジー・ピーティーワイ・リミテッド 組み合わされた湿式精錬および乾式精錬の処理によるフェロニッケルまたはニッケルマットの生産
BRPI0605892B1 (pt) * 2006-12-29 2015-09-01 Vale Sa Processo de recuperação de níquel e cobalto a partir de um eluato de resina de troca iônica

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US3839168A (en) * 1971-05-24 1974-10-01 Nickel Le Method for producing high-purity nickel from nickel matte
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
US6524367B1 (en) * 1997-02-18 2003-02-25 Centro De Investigaciones Para La Industria Minero-Metalurgcia (Cipimm) Hydrometallurgical process for the recovery of nickel and cobalt by ammoniacal leaching
US6350420B1 (en) * 1999-10-15 2002-02-26 Bhp Minerals International, Inc. Resin-in-pulp method for recovery of nickel and cobalt
US20060024224A1 (en) * 2004-08-02 2006-02-02 David Neudorf Method for nickel and cobalt recovery from laterite ores by combination of atmospheric and moderate pressure leaching

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7959812B2 (en) * 2007-12-20 2011-06-14 Applexion Multi-column sequenced separation process for separating an ionic metal derivative
US20100326918A1 (en) * 2007-12-20 2010-12-30 Applexion Multi-column sequenced separation process for separating an ionic metal derivative
JP2014509349A (ja) * 2011-02-01 2014-04-17 ヴァーレ、ソシエダージ、アノニマ ニッケルラテライト浸出廃液の直接精製
US20120298586A1 (en) * 2011-05-24 2012-11-29 Dow Global Technologies Llc Alpha-particle emitter removal
US9099208B2 (en) * 2011-05-24 2015-08-04 Rohm And Haas Electronic Materials Llc Alpha-particle emitter removal
US10246789B2 (en) 2011-12-20 2019-04-02 Freeport Minerals Corporation Systems and methods for copper recovery via roasting and leaching
US9481919B2 (en) 2012-02-14 2016-11-01 Cerro Matoso Sa Production of high grade nickel product
WO2013165735A1 (fr) * 2012-05-01 2013-11-07 Dow Global Technologies Llc Récupération de nickel de cobalt en utilisant l'échange d'ions continu
US9068247B2 (en) 2012-05-01 2015-06-30 Dow Global Technologies Llc Nickel and cobalt recovery using continuous ion exchange
CN103553155A (zh) * 2013-11-12 2014-02-05 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
CN117295694A (zh) * 2023-07-26 2023-12-26 青美邦新能源材料有限公司 一种低冰镍制备电池级硫酸镍钴锰溶液的方法
WO2025020123A1 (fr) * 2023-07-26 2025-01-30 青美邦新能源材料有限公司 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
US20250170496A1 (en) * 2023-07-31 2025-05-29 Pt Qmb New Energy Materials Method for green and low-cost extraction of nickel-cobalt from laterite nickel ore
US12403413B2 (en) * 2023-07-31 2025-09-02 Pt Qmb New Energy Materials Method for green and low-cost extraction of nickel-cobalt from laterite nickel ore

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