WO2009114903A1 - Procédé permettant de récupérer du nickel et/ou du cobalt de minerais de latérite à teneur en fer élevée - Google Patents

Procédé permettant de récupérer du nickel et/ou du cobalt de minerais de latérite à teneur en fer élevée Download PDF

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Publication number
WO2009114903A1
WO2009114903A1 PCT/AU2009/000317 AU2009000317W WO2009114903A1 WO 2009114903 A1 WO2009114903 A1 WO 2009114903A1 AU 2009000317 W AU2009000317 W AU 2009000317W WO 2009114903 A1 WO2009114903 A1 WO 2009114903A1
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Prior art keywords
nickel
cobalt
iron
solution
process according
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PCT/AU2009/000317
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English (en)
Inventor
Houyuan Liu
Omar Yesid Caceres Hernandez
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Bhp Billiton Ssm Development Pty Ltd
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Priority claimed from AU2008901412A external-priority patent/AU2008901412A0/en
Application filed by Bhp Billiton Ssm Development Pty Ltd filed Critical Bhp Billiton Ssm Development Pty Ltd
Publication of WO2009114903A1 publication Critical patent/WO2009114903A1/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
    • 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
    • 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
    • C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0407—Leaching processes
    • C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
    • C22B23/043—Sulfurated acids or salts thereof
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • 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
    • 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
    • C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
    • C22B3/32—Carboxylic acids
    • C22B3/326—Ramified chain carboxylic acids or derivatives thereof, e.g. "versatic" acids
    • 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
    • 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
    • C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the present invention relates to a new method for recovering nickel and cobalt from less weathered or partially oxidised laterite ore which contains substantial amount of ferrous ions (Fe +2 ).
  • the present invention provides a new process for treating less weathered or partially oxidised laterite ore which contains a substantial proportion of its iron component in ferrous form, and which involves acid leaching, oxidation of ferrous ions (Fe +2 ) to ferric ions (Fe +3 ) and precipitation of ferric ions at atmospheric pressure. This may lead to the manufacture of nickel and cobalt- containing intermediate products such as hydroxides, carbonates and sulphides and/or the final products of ferronickel, metallic nickel or cobalt powders and nickel or cobalt cathodes.
  • Laterite nickel and cobalt ore deposits generally contain oxidic type ores, limonites, which are normally found at the top layer of ore body, and silicate type ores, saprolites which are normally found at the bottom layer of ore body, as two layers in the same deposit, separated by a transition zone.
  • the state of iron in limonite and saprolite are either ferric ions (Fe +3 ) and/or ferrous
  • US Patent. No. 5,571 ,308 (BHP Minerals International, Inc) describes a process for heap leaching of high magnesium containing laterite ore such as saprolite.
  • US patent no. 6,312,500 (BHP Minerals International, Inc) also describes a process for heap leaching of laterites to recover nickel, which is particularly effective for ores that have a significant clay component such as nickel-containing smectite and nontronite (greater than 10% by weight).
  • the counter-current heap leach proposed by US patent no. 6,312,500 (BHP Minerals International, Inc) precipitated significant amount of dissolved iron as hydroxides inside the heap to decrease acid consumption and Fe/Ni concentration ratio in the Product Leach Solution (PLS).
  • Australian provisional application 2007902546 teaches the use of ion exchange resins (IX resin), which have much less affinity to ferrous ions than nickel and cobalt ions to treat heap leach PLS.
  • the nickel was selectively loaded by resin and the ferrous ions (Fe +2 ) was expelled into raffinate.
  • the Ni-containing elution was neutralized with neutralizers such as MgO, soda ash or acoustic soda to produce nickel hydroxide as intermediate product for ferronickel manufacture.
  • the present invention aims to find an economic and effective process for the recovery of nickel and/or cobalt from lateritic ores, particularly those laterite ores which are less weathered or partially oxidised that include a substantial proportion of iron in its ferrous state.
  • the present invention provides a process for the recovery of nickel and cobalt from sulfate solutions that contain nickel and/or cobalt in solution together with other soluble impurities such as iron.
  • the process is suitable for the recovery of nickel and/or cobalt from the resultant product leach solution (PLS) of an acid leach process such as heap leach, atmospheric or pressure leach process, or a combination of such processes, where a nickel and/or cobalt containing lateritic ore has been processed.
  • PLS product leach solution
  • the process is particularly applicable to the processing of laterite ores that are less weathered or partially oxidised laterite ores, and as a result have a substantial proportion of the iron present in its ferrous state.
  • the present invention resides in a process where the ferrous ions in solution are oxidised to ferric ions and precipitated as a ferric hydroxide such as ferric hydroxide, ferrihydrite, goethite or para-goethite.
  • the present invention resides in a process where the ferrous ions are continuously oxidised or oxidised progressively in more than one step, resulting in precipitation of the iron firstly as a ferric hydroxide or ferrihydrite, and then following further oxidation at higher temperatures, as goethite or para-goethite.
  • the present invention resides in a process for the recovery of nickel and/or cobalt from an acidic sulfate solution that also contains iron, wherein a substantial proportion of the iron present is in the ferrous state, said process including the steps of: a) oxidising the majority of the ferrous ions in the sulfate solution to ferric ions to precipitate iron as a ferric hydroxide, ferrihydrite, goethite or para-goethite; b) separating the precipitated iron from the solution; and c) recovering the nickel and/or cobalt from the resultant solution.
  • the invention resides in a process wherein the step of oxidising the majority of the ferrous ions in the sulfate solution includes progressively or continuously oxidising the ferrous ions to ferric ions, by: a) oxidising the ferrous ions to ferric ions at ambient temperature and atmospheric pressure to initially precipitate iron as ferric hydroxide or ferrihydrite; and b) further oxidising the remaining ferrous ions to ferric ions at higher temperatures and atmospheric pressure, to precipitate the iron as goethite or para-goethite.
  • the step of oxidising the ferrous ions to ferric ions is conducted in a progressive or continuous manner.
  • oxidation of the sulfate solution will take place at atmospheric pressure and ambient temperature at a pH of from 1 to 3 by sparging the solution with air or a mixture of air and sulfur dioxide under pressure.
  • the iron will precipitate as ferric hydroxide or ferrihydrite under those conditions.
  • the temperature of the reaction may then be elevated to be in the range of from 50°C to 90°C and the solution neutralised as the acid is consumed, such that the pH will be within the range of from 2.0 to 4.5. This will precipitate the majority of any remaining iron as goethite or para-goethite under these conditions.
  • the pH may be raised progressively, first to a range of 2.0 to 3.5, and then to a range of 3.5 to 4.5 to progressively precipitate the iron, firstly as iron hydroxide or ferrihydrite, which is precipitated at lower pH and temperature conditions, and then as goethite or para-goethite at the elevated temperatures. At the higher pH conditions, of 3.5 to 4.5, other impurities such as aluminium and chromium will precipitate with the iron.
  • limestone (calcium carbonate) soda ash, acoustic soda, magnesium carbonate or magnesium oxide are used to assist in neutralising the solution as acid is produced with ferric iron precipitation, and to stabilise the pH within the range of from 2.0 to 4.5.
  • Any nickel and/or cobalt that is co-precipitated with the iron following the precipitation step may be recycled to the acidic PLS and processed to recover any entrained nickel and cobalt.
  • the solution is suitably the product leach solution (PLS) from a heap leach, an atmospheric leach, a pressure leach or a combination of any one of these processes, wherein the ore that is being processed is a less weathered or partially oxidised laterite ore.
  • PLS product leach solution
  • any copper that is present in the PLS may be removed either prior to or subsequent to the iron precipitation steps in order to avoid detrimental effects on the subsequent specification of the final nickel and/or cobalt products.
  • the copper may be removed by an ion exchange process by selecting a resin that is selective for copper in preference to other ions such as iron, nickel and cobalt.
  • any copper present in the product leach solution may be removed by contacting the PLS with an ion exchange resin to selectively absorb any copper present from the solution leaving the nickel and cobalt in the raffinate.
  • any copper present in the PLS may be removed by treating the PLS with an organic reagent in a solvent extraction process to selectively extract any copper present leaving the nickel and cobalt in the raffinate.
  • the copper may be removed from the resultant iron free solution by treating the solution to an ion exchange or solvent extraction process. The copper is removed prior to nickel and cobalt recovery processing.
  • the nickel and cobalt may be recovered from the resultant solution, substantially free of iron and copper ions, by precipitation as a mixed nickel/cobalt hydroxide, a mixed nickel/cobalt carbonate, a mixed nickel/cobalt sulfide, or as a high grade hydroxide or oxide or carbonate, sulfide, metallic cathode or powders with purification/separation by multi-stage neutralisation, solvent extraction or ion exchange.
  • the solution is generally neutralised with magnesium oxide, soda ash or caustic soda at a pH of from 7 to 10 and a temperature of from ambient to 80°C.
  • the process of the present invention provides a method for treating the ferrous ion content in a product leach solution (PLS), particularly a PLS resulting from the sulfuric acid heap leaching, atmospheric or pressure leaching or combinations thereof, of less weathered or partially oxidised laterite ore.
  • PLS product leach solution
  • Such ore will generally have a higher content of ferrous iron when compared to the fully oxidised laterites where the iron generally exists in its ferric state.
  • the PLS which is an acidic sulfate solution resulting from the sulfuric acid leaching of the ore, is initially oxidised at ambient temperature and atmospheric pressure and at a pH of from 1 to 3, which oxidises the ferrous to ferric and precipitates the iron as ferric hydroxide or ferrihydrite, under these temperature and pH conditions.
  • the oxidation preferably is initiated by aerating the PLS with air under pressure, however a combination of air and sulfur dioxide could be used.
  • the sulfate solution is then continuously oxidised, or progressively oxidised in stages, preferably with aeration in iron neutralisation/precipitation agitation tanks such that the temperature is allowed to raise to be in the range of from 50°C to 90°C and as acid is consumed, the pH will rise, following the oxidation of ferrous ions to ferric ions as shown in Eq. 1.
  • a neutraliser such as a limestone slurry, is used to stabilize the pH in the range of from 2.0 to 3.5.
  • the pH may also progressively raise up to 4.5 in order to complete precipitation of the iron and clean other impurities such as aluminium and chromium. Under these temperatures and pH conditions, iron will precipitate as goethite or para- goethite, as shown in Eq. 2, which entrains less water and has better settling and filtration behaviour than ferric hydroxide.
  • One particular advantage of developing a system to precipitate iron as goethite or para-goethite rather than ferric hydroxide or ferrihydrite, is that goethite or para-goethite is better crystallised and less water is entrained, which improves the solid/liquid separation behaviour and less nickel loss.
  • the neutralising agent is limestone (calcium carbonate), but may be soda ash, acoustic soda, magnesium carbonate, magnesium oxide, or any other agent suitable to assist in neutralising and stabilising the pH of the acid sulfate solution.
  • the nickel/cobalt may be recovered by any conventional means such as hydroxide, carbonate or sulfide precipitation, ion exchange, or solvent extraction.
  • a preferred means is to further neutralise the nickel/cobalt containing resultant solution with another neutralising agent, such as magnesium oxide, soda ash, or acoustic soda to raise the pH to about 7 to 10 and to precipitate the mixed nickel/cobalt hydroxide from the resultant solution.
  • another neutralising agent such as magnesium oxide, soda ash, or acoustic soda to raise the pH to about 7 to 10 and to precipitate the mixed nickel/cobalt hydroxide from the resultant solution.
  • the temperature of the resultant solution for this precipitation step may be from ambient to 80 °C.
  • the mixed nickel cobalt hydroxide is an intermediate product that may be used for products such as ferro-nickel, nickel or cobalt powder, nickel or cobalt cathode, or, may be recovered as a high-grade hydroxide or oxide, sulfide, metallic cathode or powders with purification by multi-stage neutralisation/precipitation.
  • the PLS obtained from either a heap leach, atmospheric leach, pressure leach or a combination of such leach processes may include quantities of copper, the presence of which may have detrimental effects on subsequent nickel and cobalt recovery and quality of final products.
  • the PLS may be treated by an ion exchange or solvent extraction process in order to remove any copper present.
  • the copper may be removed from the PLS by a preliminary ion exchange or solvent extraction process prior to iron removal.
  • the copper may be removed from the resultant solution by ion exchange or solvent extraction subsequent to iron removal but before nickel and cobalt recovery.
  • the preferred preliminary ion exchange resins for copper IX are Amberlite IRC748, Bayer TP207 or DOW 4195, but other suitable resins with selectivity for copper may be used.
  • the copper may then be stripped from the resin by sulfuric acid and rejected if in small quantities. If there is sufficient copper in the PLS to economically justify recovery, the copper removal step may be a solvent extraction step, using reagents such as LIX84, or LIX984, followed by electrowinning or cementation to recover the copper.
  • Figure 1 illustrates profiles of Fe To tai, Fe +2 , Fe +3 and pH in PLS tank with aeration.
  • Figure 2 illustrates a concentration profile of Fe and Ni in counter-current heap leach.
  • Figure 3 illustrates a concentration profile of ferrous with aeration inside agitation tanks
  • Figures 4 to 6 are flowsheets of preferred embodiments of the invention.
  • FIGS 5 and 6 represent alternative embodiments to this general flowsheet.
  • the run of mine ore (1 ) which is preferably a less weathered or partially oxidised laterite ore, and has a substantial proportion of iron in its ferrous state, is acid leached in a heap leach process with sulfuric acid (2).
  • the ore may be treated by other acid leach processes such as atmospheric or pressure leach processes or combinations thereof. This produces a product leach solution pond (3) which is sparged with air (4) under pressure.
  • This initial sparging with air is conducted at atmospheric pressure and ambient temperature, and at a pH of from about 1 to 3.
  • the ferrous iron will be oxidised to ferric iron, and the iron will be precipitated as a ferric hydroxide or ferrihydrite.
  • the ferric hydroxide- or ferrihydrite-containing slurry is transferred to agitation tanks and continued to be sparged with air (5) and the pH will rise as the acid is consumed to a pH of from 2.0 to 3.5.
  • the pH is stabilised with a neutraliser such as calcium carbonate (6).
  • the temperature is maintained in the range of 50 °C to 90 °C.
  • ferric iron precipitation (8) is discharged and the overflow solution is continued to be aerated by the addition of air (9), and the pH of the solution would generally rise to a pH of from about 3.5 to 4.5 with calcium carbonate (10).
  • the temperature would remain to be within the range of from 50 °C to 90 °C. This would generally precipitate remaining ferric ion as goethite or para- goethite and other impurities such as aluminium and chromium at the higher pH.
  • any nickel and/or cobalt co-precipitated with the iron may be recirculated (1 1 ) to the acidic PLS pond (3) to enable recovery of the nickel and/or cobalt.
  • the resultant solution (12), which is now substantially free of iron is then further neutralised, for example with magnesium oxide (13) to precipitate the nickel and/or cobalt as a mixed nickel/cobalt hydroxide (27).
  • This is conducted at a temperature, preferably in the range of from ambient to 80 °C, and at a pH of from about 7 to 10.
  • the nickel barren solution which has a pH in the range of from 7 to 10 following nickel and/or cobalt recovery, is recirculated to the leach process (14).
  • FIG. 5 illustrates an alternative embodiment wherein copper is removed by either ion exchange or solvent extraction (15) prior to iron precipitation.
  • the copper is rejected as waste, or if there is sufficient copper present, it is converted to a copper product (16).
  • the nickel, cobalt, ferrous iron and any other acid soluble impurities will remain in the raffinate, whereby it will then be subjected to the continuous and/or progressive oxidation and neutralisation steps to oxidise the ferrous to ferric ions and precipitate the iron as ferric hydroxide, ferrihydrite, goethite or para-goethite in the manner described with reference to Figure 4.
  • Any nickel that is co-precipitated with the iron may be recirculated (17) and redissolved in the raffinate at a pH of about 1 , and at a temperature of from ambient to 80 °C.
  • the nickel and cobalt is recovered as a mixed nickel cobalt sulfide (18) following the addition of hydrogen sulfide, sodium sulphide or sodium bisulphide (19).
  • the nickel and cobalt barren solution may then be recirculated (20) to the initial leach step.
  • Figure 6 illustrates a process similar to that of Figure 5, except that the nickel and cobalt is recovered from the solution in a solvent extraction (SX) process (21 ) using a solvent such as Versatic Acid.
  • the cobalt is then stripped from the nickel and cobalt leach solution using a solvent such as Cyanex 272 (22) and then stripped from the cobalt leach solution with sulfuric acid (23) and recovered as a cobalt product (24).
  • nickel is then recovered from the cobalt barren solution by nickel electrowinning (25).
  • the spent electrolyte (26) is recycled back to Ni/Co SX (21 ) as the strip solution. With this process nickel is recovered as nickel cathode.
  • Example 1 Ferrous ions oxidation and ferric ions precipitation at ambient temperature inside PLS storage tank
  • the column leaching PLS in store tank contained 1 ,910 mg/L Ni and 24,606 mg/L total iron which included 17,966 mg/L Fe +2 and 6,640 mg/L Fe +3 .
  • the pH was measured as 2.20 at ambient temperature. Pressure air was sparged into the tank to oxidise ferrous to ferric ions. With aeration the original clear PLS was turn to colloid.
  • the concentrations of total iron, ferrous ion and ferric ion dropped and the pH increased. This indicated that ferrous ion was oxidized to ferric and then precipitated. As acid was consumed during this conversion according to Eq. 1 , a part of original existing ferric ion was also precipitated. These reactions approached equilibrium after 24 hours. No nickel loss occurred during ferrous oxidation/precipitation as shown in the horizontal nickel line in Figure 1.
  • Example 3 Ferrous ions oxidation and ferric ions precipitation at temperature range of 50 0 C -90 °C and pH 2.0-3.5 inside agitation tanks
  • heap leaching PLS was fed into a series of agitation tank namely CSTR (Completely Stirred Tank Reactor).
  • the reaction temperature was controlled in the range of 50-90 °C.
  • Aeration was applied in tank to oxidize ferrous to ferric.
  • the pH was controlled in the range of 2.5-3.5 with limestone slurry to precipitate ferric ions as goethite or para-goethite.
  • Figure 3 illustrates the concentration profiles of total feed iron, total out iron, feed ferrous and out ferrous. It was observed that more than half of the ferrous ions were converted to ferric ions and almost all ferric ions were precipitated. The nickel loss in this iron neutralization/precipitation operation was less than 3%.
  • the obtained ferric ion-free nickel/cobalt solution can be used to produce the mixed nickel/cobalt hydroxide precipitation (MHP) or mixed nickel/cobalt sulphide precipitation (MSP) with conventional neutralization and sulfidation respectively. It also can be used as feed solution for SX process in which the organic reagent can separate nickel and cobalt from ferrous ions and other impurities, or an ion exchange process for the recovery of nickel and/or cobalt.
  • MHP mixed nickel/cobalt hydroxide precipitation
  • MSP mixed nickel/cobalt sulphide precipitation
  • the iron-precipitated slurry was sent to thickener for solid/liquid separation.
  • the overflow of thickener was mixed with MgO slurry in a series of agitation tanks (CSTR) to precipitate nickel and cobalt as mixed hydroxide precipitation (MHP) at pH7-10. No extra heat was provided for this unit operation so that the reaction temperature was around 30-60° C.
  • the MHP slurry was fed to thickener for solid/separation separation.
  • the thickener underflow was sent to a pressure frame filter to produce MHP cake.
  • Table 2 shows the chemical composition of MHP cakes.
  • the Ni/Fe concentration ratio of MHP is flexible by controlling the iron precipitation efficiency depending upon the specification of final product e.g. ferronickel.

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Abstract

L'invention concerne un procédé permettant de récupérer du nickel et/ou du cobalt à partir d'une solution de sulfate qui contient également du fer, une proportion substantielle de fer étant contenue à l'état ferreux. Le procédé susmentionné comprend les étapes qui consistent: a) à oxyder la majorité des fers ferreux dans la solution de sulfate afin que les ions ferriques précipitent le fer sous forme d'hydroxyde ferrique, de ferrihydrite, de goethite ou de para-goethite; b) à séparer le fer précipité de la solution; et c) à récupérer le nickel et/ou le cobalt à partir de la solution obtenue.
PCT/AU2009/000317 2008-03-20 2009-03-19 Procédé permettant de récupérer du nickel et/ou du cobalt de minerais de latérite à teneur en fer élevée WO2009114903A1 (fr)

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AU2008901412A AU2008901412A0 (en) 2008-03-20 Process for the recovery of nickel and/or cobalt from high ferrous content laterite ores
AU2008901412 2008-03-20

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EP2703503A1 (fr) * 2012-09-04 2014-03-05 Canbekte, Hüsnü Sinan Procédé de précipitation du fer à partir de solutions de lixiviation
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WO2014114752A1 (fr) * 2013-01-25 2014-07-31 CANBEKTE, Hüsnü Sinan Procédé de précipitation du fer à partir de solutions de lixiviation
AU2015207917B2 (en) * 2014-07-30 2016-11-03 Guangxi Normal University Two-stage iron removing method for solutions obtained from acid leaching of nickel oxide ores
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CN114058847A (zh) * 2021-11-05 2022-02-18 金川集团股份有限公司 一种镍精矿氯气浸出液的除铁方法
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CN114561542A (zh) * 2022-02-25 2022-05-31 盛隆资源再生（无锡）有限公司 一种提高含铁铜废液中铜回收率的方法
CN115369211A (zh) * 2022-07-01 2022-11-22 李玉峰 一种利用aod炉富集镍的方法
WO2023056505A1 (fr) * 2021-10-05 2023-04-13 Commonwealth Scientific And Industrial Research Organisation Procédé de récupération de métaux de valeur à partir de minerai latéritique contenant du nickel et du cobalt

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EP2703503A1 (fr) * 2012-09-04 2014-03-05 Canbekte, Hüsnü Sinan Procédé de précipitation du fer à partir de solutions de lixiviation
CN102876892B (zh) * 2012-10-30 2013-11-20 杭州蓝普水务有限公司 低铁高镁、高铁低镁红土镍矿用废稀硫酸浸出镍钴的方法
CN102876892A (zh) * 2012-10-30 2013-01-16 杭州蓝普水处理设备有限公司 低铁高镁、高铁低镁红土镍矿用废稀硫酸浸出镍钴的方法
WO2014114752A1 (fr) * 2013-01-25 2014-07-31 CANBEKTE, Hüsnü Sinan Procédé de précipitation du fer à partir de solutions de lixiviation
CN103740931A (zh) * 2014-01-21 2014-04-23 江苏仁欣化工股份有限公司 含镍铁混合溶液针铁矿沉淀铁的方法
AU2015207917B2 (en) * 2014-07-30 2016-11-03 Guangxi Normal University Two-stage iron removing method for solutions obtained from acid leaching of nickel oxide ores
JP7087601B2 (ja) 2018-04-06 2022-06-21 住友金属鉱山株式会社 硫化剤の除去方法及びニッケル酸化鉱石の湿式製錬方法
JP2019181349A (ja) * 2018-04-06 2019-10-24 住友金属鉱山株式会社 硫化剤の除去方法及びニッケル酸化鉱石の湿式製錬方法
CN109022823A (zh) * 2018-07-24 2018-12-18 北京科技大学 一种从红土镍矿酸浸液中均相沉淀分离镍、钴和锰的方法
CN111847528B (zh) * 2020-06-10 2022-10-11 包头昊明稀土新电源科技有限公司 除去废旧镍氢电池中铁的方法
CN111847528A (zh) * 2020-06-10 2020-10-30 包头昊明稀土新电源科技有限公司 除去废旧镍氢电池中铁的方法
CN113151677A (zh) * 2021-04-26 2021-07-23 赣州逸豪优美科实业有限公司 一种硫酸盐无酸浸取钴中间品的方法
CN113151677B (zh) * 2021-04-26 2022-09-09 赣州逸豪优美科实业有限公司 一种硫酸盐无酸浸取钴中间品的方法
WO2023056505A1 (fr) * 2021-10-05 2023-04-13 Commonwealth Scientific And Industrial Research Organisation Procédé de récupération de métaux de valeur à partir de minerai latéritique contenant du nickel et du cobalt
CN114058844A (zh) * 2021-10-26 2022-02-18 广东佳纳能源科技有限公司 中间品除铁的方法
CN114058847A (zh) * 2021-11-05 2022-02-18 金川集团股份有限公司 一种镍精矿氯气浸出液的除铁方法
CN114561542A (zh) * 2022-02-25 2022-05-31 盛隆资源再生（无锡）有限公司 一种提高含铁铜废液中铜回收率的方法
CN114561542B (zh) * 2022-02-25 2024-02-02 盛隆资源再生（无锡）有限公司 一种提高含铁铜废液中铜回收率的方法
CN115369211A (zh) * 2022-07-01 2022-11-22 李玉峰 一种利用aod炉富集镍的方法
CN115369211B (zh) * 2022-07-01 2023-06-23 王泰刚 一种利用aod炉富集镍的方法

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