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WO2002048042A1 - Enrichissement en solides d'hydroxydes par contact de precipite - Google Patents

Enrichissement en solides d'hydroxydes par contact de precipite Download PDF

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Publication number
WO2002048042A1
WO2002048042A1 PCT/AU2001/001609 AU0101609W WO0248042A1 WO 2002048042 A1 WO2002048042 A1 WO 2002048042A1 AU 0101609 W AU0101609 W AU 0101609W WO 0248042 A1 WO0248042 A1 WO 0248042A1
Authority
WO
WIPO (PCT)
Prior art keywords
process according
feed liquor
cobalt
nickel
precipitate
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/AU2001/001609
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English (en)
Inventor
Erin Maree Jones
Michael John Miller
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.)
BHP Billiton SSM Technology Pty Ltd
Original Assignee
QNI Technology Pty 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
Application filed by QNI Technology Pty Ltd filed Critical QNI Technology Pty Ltd
Priority to AU2133302A priority Critical patent/AU2133302A/xx
Priority to AU2002221333A priority patent/AU2002221333B2/en
Publication of WO2002048042A1 publication Critical patent/WO2002048042A1/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
    • 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
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G53/00—Compounds of nickel
    • C01G53/04—Oxides
    • 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
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2006/00—Physical properties of inorganic compounds
    • C01P2006/80—Compositional purity
    • 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 provides for a method of precipitating nickel and cobalt hydroxides from acidic solutions by the use of magnesium oxide as an alkaline agent to raise the solution pH coupled with a novel precipitate contact system.
  • the precipitate contact system enhances the quality of the nickel and cobalt hydroxide solids recovered, while also fully utilising the neutralising potential of the magnesium oxide used initially.
  • Magnesium oxide (MgO) is effective in the recovery of nickel and cobalt as hydroxides in hydrometallurgical processes treating acidic sulphate liquors containing nickel and cobalt and other soluble entities derived from pressure acid leaching or bio-leaching of nickel and/or cobalt containing ores and concentrates.
  • MgO is a relatively expensive reagent.
  • the present invention aims to achieve a process with more efficient use of MgO and almost total recovery of nickel and cobalt in one treatment stage.
  • MgO reactive magnesia
  • US Patent 3,466,144 also describes the use of MgO to raise the pH of the acid sulphate solution containing Ni and Co to at least 8.0 to precipitate nickel and cobalt and manganese, if present, from solution but at a temperature of 70°C to 90° C. No quantitative values are given in the description to assess the quality of the recovered mixed hydroxide precipitate so the presence of unreacted MgO is not disclosed.
  • Australian patent 701829 describes the addition of a precalculated (based on stoichiometry) amount of MgO to an acid sulphate liquor containing nickel, cobalt and manganese ions to precipitate a majority of nickel and cobalt and a minority of the manganese present as hydroxides.
  • This process is concerned with minimising the manganese content of the mixed nickel, cobalt hydroxide precipitate rather than total recovery of nickel and cobalt in one process stage. Consequently the process then requires further upward pH adjustment with Ca(OH) 2 to recover the remaining Ni, Co and Mn, which solids are recycled for further treatment to improve the overall recovery of Ni and Co.
  • This patent also refers to a reaction time of at least 1 hour.
  • the present invention aims to overcome or at least alleviate one or more of the difficulties associated with the prior art.
  • the present invention provides a process for the recovery of nickel and cobalt from an acidic sulphate feed liquor containing nickel and cobalt, said process including the steps of:
  • the acidic sulphate feed liquor Prior to contact with magnesium oxide, the acidic sulphate feed liquor preferably undergoes a preliminary neutralization stage to raise the pH of the liquor and to remove some impurities. In a preferred form, essentially all of the feed liquor exiting the neutralization stage is directed to the mixed hydroxide precipitation stage.
  • the feed liquor exiting the neutralization stage may be split into at least two fractions, preferably but not necessarily of approximately equal size. Accordingly, the present invention further resides in a process for the recovery of nickel and cobalt from an acidic sulphate feed liquor containing nickel and cobalt, said process including the steps of:
  • the process of the present invention is useful in a nickel and cobalt recovery processes where nickel and cobalt is recovered from a pressure acid leach process from lateritic ore. It is contemplated that the process of the present invention be may be integrated into such a recovery process, where nickel and cobalt is recovered as a mixed hydroxide precipitate from an acidic sulphate solution with the use of MgO, while utilizing as efficiently as possible the MgO used in the process.
  • Figure 1 is a flow sheet showing preferred process steps of a broader nickel and cobalt extraction process, and the process of the invention should not be considered to be limited thereto.
  • FIG. 1 illustrates a process where essentially all the acidic sulphate feed liquor exiting the secondary neutralization step (17) is directed to a mixed hydroxide precipitation/wash stage.
  • An alternative arrangement where the acidic sulphate feed liquor exiting the secondary neutralization step is divided into two fractions is illustrated in Figure 2.
  • the preliminary and subsequent processing steps described with reference to Figure 1 are also applicable to the embodiment of the invention described with reference to Figure 2, although those steps are not specifically referred to in Figure 2.
  • the nickel and cobalt containing raw materials undergo a beneficiation step.
  • the function of the beneficiation step is to produce a high grade, high density under-flow for feeding into the pressure acid leach autoclave, with minimal loss of nickel and cobalt values.
  • Beneficiation takes advantage of the ore mineralogy to concentrate the nickel and cobalt values into a concentrate.
  • Nickel and cobalt tend to concentrate in fractions from the ore that are in the order of 30-70 microns, whereas the coarse size fractions are dominated by low grade siliceous waste material.
  • the beneficiation process consists of scrubbing the crushed run of mine ore, then extracting the finer material containing the nickel and cobalt using screens, cyclones and attritioning stages.
  • the fine materials containing the nickel and cobalt values are collected as a slurry, then thickened to a manageable under-flow before being sent to a slurry storage stage ahead of the pressure acid leach circuit.
  • Low grade rejects from the beneficiation stage are returned to the mine.
  • the slurry from the beneficiation stage undergoes pressure acid leach to efficiently leach the nickel and cobalt from the beneficiated ore.
  • nickel and cobalt is first leached from a laterite slurry (1) containing nickel and cobalt with sulphuric acid (3) at elevated pressures, to create an acid sulphate liquor containing both nickel and cobalt and numerous impurities.
  • a residue releach stage (9) uses excess acid from the pressure acid leach stage to recover precipitated nickel and cobalt returned from recycle streams produced at later stages of the recovery process.
  • High acid leach coming from the pressure acid leach reactors may leach the nickel and cobalt from solids produced following later acid neutralization steps (shown by recycle arrow (4)).
  • the more refractory elements in the recycle streams notably silica, alumina and haematite leach to a lesser extent than the nickel and cobalt, but these solids will generally pass unreacted through the residue releach and neutralization stage and may be separated as waste solids.
  • the acidic sulphate slurry may then undergo a primary neutralisation step, wherein the function of this step is to neutralise excess acid from the solutions discharged from the pressure acid leach and to efficiently remove iron, aluminium and other impurities from the slurry.
  • This may be achieved with the injection of air and air/SO 2 mixtures (8) into the slurry, typically in a series of stirred tank reactors (6).
  • An alkaline reagent, such as ground limestone slurry (2) may be used for pH control. Typically, the limestone is ground to about 75 microns.
  • This primary neutralisation step is typically conducted in three stages.
  • the excess acid is removed by using an alkaline reagent such as ground limestone, aiming for a target pH of 1.8 to 2.0.
  • Air may be injected into the nickel and cobalt containing slurry to sparge excess CO 2 .
  • a mixture of air and SO 2 (8) is injected into the nickel and cobalt containing slurry.
  • Trace levels of ferric iron in solution catalyse the oxidation of SO 2 to form Caro's acid H 2 SO 5 , which then oxidises ferrous iron to ferric iron.
  • the ferric iron is precipitated by the addition of further ground limestone to bring the pH up to between 2.5 to 3.5. This simultaneously precipitates some of the aluminium and chromium from the slurry.
  • the nickel and cobalt containing slurry and associated solids may then be treated in a counter current decantation circuit to remove low grade solids.
  • the counter current decantation circuit separates low grade solids from the nickel and cobalt containing slurry in a series of thickeners (10). Slurry and associated solids from the primary neutralisation stage are fed to the first thickener, while barren wash solutions (11) from a later manganese removal stage is added to the final thickener. This counter current flow of the liquor from the primary neutralisation stage and the wash solution from later stages provides efficient use of wash water, and also ensures that the tailings slurry contains only low levels of soluble nickel and cobalt, with minimal dilution of the product liquor. The final underflow, including iron residue becomes the final process tailings (12), while the product liquor containing the nickel and cobalt values, then undergoes a secondary neutralization step.
  • the primary purpose of the secondary neutralisation step is to remove the remaining iron, aluminium and other impurities from the acidic sulphate feed liquor containing the nickel and cobalt that exits the counter current decantation circuit. This is generally achieved by increasing the pH of the liquor with finely ground limestone (16) and simultaneously oxidising the iron in solution using injected air (15). The reactions may be completed in a series of agitated vessels (14) with air sparging. Generally, iron, aluminium and gypsum are precipitated and the solids are collected in a clarifier (42). Some solids may be recirculated and returned to the first vessel of the secondary neutralization step to undergo further neutralisation which assists in solid precipitation, especially for gypsum.
  • the remainder of the solids is returned to the residue releach circuit (9) by flow (4) to recover nickel and cobalt co-precipitates.
  • the purified acidic sulphate feed liquor containing the nickel and cobalt is then sent to the mixed hydroxide precipitation/wash circuit.
  • the incoming acidic sulphate feed liquor (17) is contacted with magnesium oxide, preferably in a slurry form (18) to precipitate the nickel and cobalt as a mixed hydroxide precipitate.
  • Figure 1 illustrates essentially all of the acidic sulphate feed liquor exiting the secondary neutralization step being transferred to the mixed hydroxide precipitate/wash circuit.
  • the acidic sulphate feed liquor geneally has a pH of approximately 4.0 to 5.0, preferably about 4.5 when exiting the secondary neutralization step.
  • the pH of the incoming feed liquor is raised to approximately 7.5 to 8.5, and most preferably about 8.2.
  • the nickel and cobalt and some manganese will precipitate as hydroxides together with some unreacted magnesium oxide to form a mixed hydroxide precipitate.
  • the mixed hydroxide precipitate is collected as a solid or thickened slurry in a mixed hydroxide precipitate clarifier (20).
  • the incoming stream of the acidic sulphate feed liquor generally has a pH of about 4.5, which is sufficient to leach the magnesium oxide from the mixed hydroxide precipitate. Simultaneously, this will precipitate some additional nickel and cobalt from the incoming acidic sulphate liquor.
  • Nickel precipitation has a buffering effect upon the pH, and the final pH of the mixed hydroxide wash stage will be in the range of from 6.5 to 7.5. This is dependent on the initial nickel tenor following from the secondary neutralisation step, and the level of magnesium oxide in the mixed hydroxide precipitate.
  • the solids remaining after the mixed hydroxide wash are collected in a clarifier (24), and the liquor is returned to the mixed hydroxide precipitation stage for precipitation of the bulk of the nickel and cobalt values with magnesium oxide slurry.
  • the solids collected following the mixed hydroxide wash stage are filtered and washed to displace chloride contaminated liquor. After a final re-pulp wash, the solids are filtered in a pressure filter to achieve the lowest practical moisture level and to recover the nickel and cobalt as hydroxides.
  • Overflow liquor following the mixed hydroxide precipitation/wash is sent to a manganese removal stage to precipitate manganese from solution as an inert waste (26).
  • This inert waste can be safely stored as long term tailings.
  • the reactions preferably take place in a series of stirred reactors with a clarifier (41) after the final reaction vessel to collect the solids. Slaked lime is used to raise the pH to a nominal level of about 8.5 or higher. Air sparging is used to oxidize manganese, in which form it is more readily precipitated and forms more stable tailings solids.
  • Figure 2 is an example of how the mixed hydroxide precipitate/wash circuit can be operated to effect contact of the feed liquor and precipitated solids where the acidic sulphate feed liquor exiting the secondary neutralization step is split in a 1 :1 ratio distinct from Figure 1 , where essentially all of the acidic sulphate feed liquor is made to contact the mixed hydroxide precipitates in the mixed hydroxide wash/precipitate circuit.
  • the acidic sulphate feed liquor (31) containing Ni, Co, Mn and Mg typically of pH 4.5 is split into two fractions of approximately equal size.
  • the first fraction (37) is reacted with MgO under pH control in a conventional neutralising process to precipitate maximum nickel and cobalt as well as manganese as hydroxides in reactor vessels (32), (33), (34) and thickener (35).
  • the pH is controlled by the addition of MgO to reach a value of about 8.2.
  • the precipitated thickened solids (42) are removed from the underflow of thickener (35) and brought into contact with the second fraction (38) of the incoming acidic feed liquor in vessel (36).
  • the pH upon contact in this vessel is approximately 6.8
  • the overflow from vessel (36) is either sent to reactor (32) for further precipitation or discarded via stream (39). Variations of the initial split ratio can be effected to obtain the desired result from anywhere from a 1 :100 ratio to a 100:1 ratio.
  • the underflow precipitate from reactor (36) passes to a belt filter (40) and the recovered Ni, Co hydroxide solids pass for further processing to recover nickel and cobalt.
  • the following example provides quantitative information on the quality of the solids recovered from reactor (36) compared with those removed from thickener (35) when the incoming feed liquor was split 1 :1.
  • the process of the present invention which includes both a mixed hydroxide precipitation step and the step of washing the precipitate with further or a second fraction of the acidic sulphate feed liquor has several advantages over using a single magnesium oxide or magnesium oxide/calcium oxide precipitation step.
  • a particular advantage is the magnesium content in the final product compared to a single stage precipitation route. In a single stage precipitation route there is no facility for recovering or removing the magnesium from the final mixed hydroxide precipitate. Excess magnesium oxide remains in the product and represents an inefficient use of a costly reagent, and also adds to expense in down stream processing and transport.
  • the pH of the reaction mixture is lowered so as to remove excess or undissolved magnesium oxide. This is more readily achieved when the nickel and cobalt tenor of the feed liquor is higher and when the mixed hydroxide wash stage accepts essentially all of the feed liquor proceeding to the precipitation stage.
  • a further advantage is a lower manganese content in the final product compared to a single stage precipitation route recovering total nickel and cobalt.
  • Manganese hydroxide is generally regarded as an undesirable contaminant in the hydroxide product.
  • some manganese is precipitated in the process of recovering the nickel and cobalt in the first higher pH precipitation stage.
  • the fraction of nickel and cobalt precipitated in the mixed hydroxide wash stage contains negligible manganese possibly due to the lower reaction pH. This serves to reduce the overall manganese level of the final hydroxide product.
  • a further advantage is that the final nickel and cobalt product has better filterability and product handling characteristics compared to those products precipitated from a single magnesium oxide precipitation. It has been observed that with a single magnesium hydroxide precipitation step, given the level of magnesium hydroxide that remains in the precipitate, the product tends to be slimy, difficult to filter resulting in the need for further additional filtration equipment, resulting in additional operating costs. Mixed hydroxide precipitates produced with high magnesium content were observed to aggregate whereas precipitates with low magnesium content following a secondary wash were free flowing solids with little or no tendency to aggregate in storage.
  • a further advantage is the reduced reagent costs by eliminating the requirement for lime precipitation of nickel and cobalt residual from the solution.
  • Prior art processes which terminate the nickel and cobalt precipitation before completion separate the nickel and cobalt hydroxides from solution and precipitate the remainder of nickel and cobalt along with some of the manganese by using slaked lime.
  • the impure hydroxide produced in this step is recycled to an earlier part the process where it is leached in the highly acidic conditions.
  • the lime that is used in this process is an added process cost because the additional lime is effectively used to neutralise excess acid from the pressure acid leach discharge, whereas the same function can be much more economically performed using limestone or calcrete, which are cheaper reagents for this function.
  • a further advantage is that there is little potential for nickel and cobalt losses as the process of the invention avoids a need to recirculate a proportion of the nickel and cobalt precipitate to the pressure acid leach circuit, which is done in prior art processes to leach further nickel and cobalt from these solids.
  • the process of the present invention eliminates the need to releach further nickel and cobalt using excess acid from the pressure acid leach discharge, and accordingly, eliminates the potential nickel and cobalt losses that could occur.
  • a further advantage is the lower recycle rates to the residue releach circuit, hence lowering circuit flow rate requirements to the bulk of the refining circuit.
  • Residues recycled from a precipitation step using lime as used in the prior art are returned as a slurry, bearing not only nickel, cobalt and manganese values, but also gypsum precipitated in the neutralisation step.
  • This slurry increases the circuit volumetric and flow rate from the pressure acid leach discharge onwards, necessitating larger tankage and pumping requirements.
  • a further advantage is the lower sulphate and chloride levels in the final product by employment of higher pH conditions in the neutralisation step.
  • sulphate and chloride contamination as co- precipitants from solution. This is believed to be due to the rapid precipitation of hydrated metal sulphate and chloride species from solution by employing a higher pH for the bulk of the metals precipitated.
  • the process of the present invention reduces the substitution of sulphate and chloride species in the hydroxy complex, and hence the final hydroxide product.
  • Non-hydroxide species are undesirable components of the final product because of the added downstream costs which would include transport and undesirable reactions for downstream processing stages.
  • sulphate and chloride ions will leach in an ammonia/ammonium carbonate system, rendering the stoichiometric equivalent ammonia irrecoverable by conventional distillation methods.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Metallurgy (AREA)
  • Inorganic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

L'invention concerne un procédé d'extraction de nickel et de cobalt d'une liqueur mère de en sulfate acide contenant du nickel et du cobalt. Ce procédé consiste à: (a) mettre une solution mère de sulfate acide en contact avec de l'oxyde de magnésium pour faire précipiter le nickel et le cobalt sous forme de précipité d'hydroxyde mélangé; puis, (b) mettre en contact le précipité d'hydroxyde mélangé avec une solution mère de sulfate acide pour dissoudre encore une fois l'oxyde de magnésium non réagi dans le précipité d'hydroxyde mélangé, et enfin, faire précipiter le nickel et le cobalt d'addition comme un précipité d'hydroxyde mélangé.
PCT/AU2001/001609 2000-12-13 2001-12-13 Enrichissement en solides d'hydroxydes par contact de precipite Ceased WO2002048042A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
AU2133302A AU2133302A (en) 2000-12-13 2001-12-13 Hydroxide solids enrichment by precipitate contact
AU2002221333A AU2002221333B2 (en) 2000-12-13 2001-12-13 Hydroxide solids enrichment by precipitate contact

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AUPR2072 2000-12-13
AUPR2072A AUPR207200A0 (en) 2000-12-13 2000-12-13 Hydroxide solids enrichment by slurry contact

Publications (1)

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WO2002048042A1 true WO2002048042A1 (fr) 2002-06-20

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006069416A1 (fr) * 2004-12-30 2006-07-06 Bhp Billiton Ssm Technology Pty Ltd Extraction de nickel et de cobalt a partir d'un flux d'elution de resine
WO2007087675A1 (fr) * 2006-01-31 2007-08-09 Murrin Murrin Operations Pty Ltd Procede ameliore de recuperation d'un metal de base a partir d'une lixiviation en tas
WO2008003152A1 (fr) * 2006-07-03 2008-01-10 Companhia Vale Do Rio Doce Procédé permettant le contrôle instantané de la précipitation du nickel et du cobalt présents dans un lixiviat par ajustement du ph de la solution
AU2019222853B2 (en) * 2018-09-07 2021-03-18 China Enfi Engineering Corporation Method of nickel-cobalt hydroxide hydrometallurgical extraction from laterite-nickel ore
US20250178922A1 (en) * 2023-06-30 2025-06-05 Pt Qmb New Energy Materials Method for continuously preparing mixed hydroxide precipitate from laterite nickel ore by hydrometallurgy

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2262118A1 (en) * 1974-02-25 1975-09-19 Ministerio Mineria Y Geol Nickel extraction from laterite ores - using a two phase treatment with acid and basic magnesium carbonate
WO1981002153A1 (fr) * 1980-01-31 1981-08-06 Hanna Mining Co Production d'oxyde de magnesium d'un degre eleve de purete et de surface specifique etendue
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
AU6061899A (en) * 1999-02-12 2000-08-17 Pacific Metals Co., Ltd. Process for recovering valuable metals from oxide ore
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

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2262118A1 (en) * 1974-02-25 1975-09-19 Ministerio Mineria Y Geol Nickel extraction from laterite ores - using a two phase treatment with acid and basic magnesium carbonate
WO1981002153A1 (fr) * 1980-01-31 1981-08-06 Hanna Mining Co Production d'oxyde de magnesium d'un degre eleve de purete et de surface specifique etendue
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
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
AU6061899A (en) * 1999-02-12 2000-08-17 Pacific Metals Co., Ltd. Process for recovering valuable metals from oxide ore

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006069416A1 (fr) * 2004-12-30 2006-07-06 Bhp Billiton Ssm Technology Pty Ltd Extraction de nickel et de cobalt a partir d'un flux d'elution de resine
EA010771B1 (ru) * 2004-12-30 2008-10-30 БиЭйчПи БИЛЛИТОН ЭсЭсЭм ТЕКНОЛОДЖИ ПТИ ЛТД. Извлечение никеля и кобальта из смоляного потока элюата
WO2007087675A1 (fr) * 2006-01-31 2007-08-09 Murrin Murrin Operations Pty Ltd Procede ameliore de recuperation d'un metal de base a partir d'une lixiviation en tas
WO2008003152A1 (fr) * 2006-07-03 2008-01-10 Companhia Vale Do Rio Doce Procédé permettant le contrôle instantané de la précipitation du nickel et du cobalt présents dans un lixiviat par ajustement du ph de la solution
US8187360B2 (en) 2006-07-03 2012-05-29 Vanessa Macedo Torres Process for the instantaneous control of precipitation of nickel and cobalt present in the leach liquor, by adjusting the pH of the solution
AU2019222853B2 (en) * 2018-09-07 2021-03-18 China Enfi Engineering Corporation Method of nickel-cobalt hydroxide hydrometallurgical extraction from laterite-nickel ore
US20250178922A1 (en) * 2023-06-30 2025-06-05 Pt Qmb New Energy Materials Method for continuously preparing mixed hydroxide precipitate from laterite nickel ore by hydrometallurgy
US12391574B2 (en) * 2023-06-30 2025-08-19 Pt Qmb New Energy Materials Method for continuously preparing mixed hydroxide precipitate from laterite nickel ore by hydrometallurgy

Also Published As

Publication number Publication date
AUPR207200A0 (en) 2001-01-11
AU2133302A (en) 2002-06-24

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