WO2015081368A1 - Process for producing refined nickel and other products from a mixed hydroxide intermediate - Google Patents
Process for producing refined nickel and other products from a mixed hydroxide intermediate Download PDFInfo
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- WO2015081368A1 WO2015081368A1 PCT/AU2014/001087 AU2014001087W WO2015081368A1 WO 2015081368 A1 WO2015081368 A1 WO 2015081368A1 AU 2014001087 W AU2014001087 W AU 2014001087W WO 2015081368 A1 WO2015081368 A1 WO 2015081368A1
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- nickel
- leach
- solution
- cobalt
- process according
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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
- 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
- C22B23/0407—Leaching processes
- C22B23/0446—Leaching processes with an ammoniacal liquor or with a hydroxide of an alkali or alkaline-earth metal
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- 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
- This invention relates to a process for the refining of an impure nickel containing intermediate, to produce a refined nickel metal, preferably a solid metallic nickel powder.
- the process may also involve the recovery of a nickel and cobalt containing mixed sulphide precipitate, a copper precipitate and/or a zinc precipitate, whilst rejecting manganese and magnesium into the leach residue.
- sulphur is recovered as ammonium sulphate.
- the process relates to the processing of a mixed hydroxide intermediate, preferably a nickel-cobalt-manganese-magnesium hydroxyl-sulphate intermediate, which may also contain zinc and copper.
- a mixed hydroxide intermediate preferably a nickel-cobalt-manganese-magnesium hydroxyl-sulphate intermediate, which may also contain zinc and copper.
- Such intermediates are also known as Mixed Hydroxide Product (or Precipitate) or "MHP" or as referred to herein as a “mixed hydroxide intermediate”.
- Nickel containing intermediates produced by addition of an alkali reagent are commonly referred to as mixed hydroxide precipitates (or products) or MHP, particularly when they contain significant quantities of cobalt and manganese and minor quantities of zinc and cobalt, as when they are derived from nickel laterite acid leach solutions or nickel sulphide acidic pressure oxidation leach solutions.
- MHP mixed hydroxide precipitates
- Such mixed hydroxide intermediates typically contain 3% to 5% sulphur in the form of sulphate (9 to 15% sulphate), so can more properly be termed a mixed hydroxy-sulphate or basic sulphate.
- U.S Patent 1 ,091 ,545 describes a process for producing a nickel hydrate product with magnesia, from a purified solution produced from acid leaching of nickel silicate ore.
- Canadian Patent 618,826 describes a process that includes producing a nickel and cobalt intermediate product using an alkaline reagent, from a purified solution produced from pressure acid leaching of a lateritic nickel ore.
- the nickel and cobalt containing intermediate product may be re-leached in ammonia compounds.
- U.S. Patent 2,899,300 includes a description for producing a mixed nickel/cobalt intermediate, using magnesia and provides an analysis, but does not give an indication of a suitable refining route.
- U.S. Patent 3,466,144 describes a process which includes producing a nickel-cobalt- manganese containing intermediate product using an alkaline reagent, from a purified solution produced from pressure acid leaching of a lateritic nickel ore, followed by refining of the intermediate by leaching in ammonium sulphate with ammonia added. No information is given on the leaching conditions that may be employed.
- Patent Application WO 01/6298 in the name of Anaconda Nickel Limited describes a process which includes leaching a MHP in ammoniacal ammonium sulphate solutions of approximately 500 to 650 g/L ammonium sulphate concentration.
- the nickel in solution is reasonably dilute, such that its concentration is increased by evaporation of part of the water from the solution.
- the solution then undergoes a nickel-cobalt separation by solvent extraction, before hydrogen reduction of separate nickel and cobalt solutions.
- a bleed of the nickel-free ammonium sulphate solution is taken and treated with lime, to form gypsum and magnesium sulphate to enable the ammonia to be recovered by distillation.
- Magnesium sulphate is removed from the leach circuit in this manner, as indicated by Figure 4 of the Anaconda specification.
- the process described suffers the disadvantages of a low nickel tenor, requiring steam for concentration.
- U.S. Patent 6,171 ,564 also in the name of Cominco Engineering Services Ltd also describes a process which includes leaching a nickel/cobalt hydroxide, also including a second ammonia leaching stage, where the nickel/cobalt hydroxide is derived from processing a laterite ore and contains manganese.
- This process clearly has a number of disadvantages. Separation of cobalt and magnesium from nickel requires two solvent extraction processes. Nickel must be concentrated to a level suitable for metal recovery by a third solvent extraction process. Water must be evaporated from the leach liquor so that it is at a suitable concentration for recycling to the nickel/cobalt hydroxide leach.
- U.S. Patent 5,976,218 in the name of Henkel Corporation describes a process that includes leaching a nickel/cobalt hydroxide in an ammonia - ammonium carbonate solution, with a titratable ammonia level of between 40 and 100 g/L.
- the nickel tenor of this solution is around 10 g/L. It is followed by an oxidation step to precipitate manganese and ensure cobalt is in the three plus (3+) oxidation state, then a nickel solvent extraction step to separate nickel and cobalt and concentrate the nickel for subsequent electrowinning.
- Cobalt is recovered by selective precipitation or solvent extraction. Like the above described patents this process suffers disadvantages of having low nickel concentration, and requiring a nickel-cobalt separation by solvent extraction. Water balance is maintained by steam stripping to recover ammonia and carbon dioxide from a bleed stream.
- Patent 5,976,2108 downstream process steps included an oxidation step to precipitate the remaining manganese and oxidise cobalt to the three plus (3+) oxidation state, nickel solvent extraction to separate nickel and cobalt and concentrate the nickel for subsequent electrowinning and cobalt and zinc recovery by precipitation.
- Extraction of nickel in the ammonia-ammonium sulphate leach was relatively modest at around 90%, requiring a further acid leaching treatment to increase recovery.
- Ammonia was recovered by a lime boil, a two stage process, requiring lime and steam, so that water could be bled from the leach circuit.
- This process has the disadvantages of the processes described previously and in addition requires an additional acid leaching step to achieve high nickel recovery.
- Nickel concentrations in the leach solution are less than 30 g/L, meaning further concentration steps are required for economic recovery of a final nickel product
- Cobalt must be separated from nickel by a solvent extraction step
- this process has been modified to produce a leach solution with a nickel concentration feeding reduction in excess of 100 g/L.
- Nickel was reduced by hydrogen under pressure, to produce nickel metal powder containing 1 1 g/t magnesium and 16 g/t manganese.
- the build-up of magnesium and manganese was controlled by bleeding contaminated ammonium sulphate solution from the process.
- This patent is silent on methods by which the contaminated bleed solution is treated to dispose of the magnesium and manganese and recover the ammonium sulphate.
- this process too suffers from a number of disadvantages, including: 1 .
- the present invention provides a process for producing refined nickel metal free of manganese impurities from a mixed hydroxide intermediate that may generally contain significant quantities of magnesium and manganese. It also provides a process for producing copper sulphide, mixed cobalt-nickel-zinc sulphide and ammonium sulphate products, free from unacceptable levels of magnesium and manganese contamination.
- the present invention aims to overcome one or more of the difficulties or disadvantages identified in the prior art documents.
- a process to produce a refined nickel metal product from a mixed hydroxide intermediate involves ammonia leaching a slurry containing the nickel and recovering the refined nickel product by direct hydrogen reduction of the resultant leach solution under pressure.
- other products may also be recovered from the leach solution, for example cobalt, zinc, copper and other nickel products from the residual nickel remaining in the leach solution, while also recovering ammonia as ammonium sulphate for reuse in the leach process, and/or as a saleable product.
- the process has the advantage of rejecting magnesium and manganese impurities from the liquor stream prior to the recovery of the metal values.
- the mixed hydroxide intermediate product may be produced as an intermediate product in the processing of both nickel laterite and nickel sulphide materials including concentrates. It is also commonly referred to as a mixed hydroxide precipitate (or product), or MHP, but herein is referred to as a "mixed hydroxide intermediate”.
- the mixed hydroxide intermediate may be recovered from a sulphuric acid leaching liquor during the processing of a nickel laterite ore.
- such intermediate products are produced when an alkali reagent such as magnesia or lime is used to raise the pH of an acidic sulphate solution to precipitate a nickel product as a mixed hydroxide intermediate.
- Such intermediates are also recovered from nickel sulphide acidic pressure oxidation leach solutions by the addition of a comparable alkali material.
- a mixed hydroxide intermediate produced from processing a nickel laterite or nickel sulphide ore contains the main element of interest, namely nickel, together with variable quantities of metals such as cobalt, zinc and copper as well as sulphur in the form of sulphates, and impurities such as manganese, magnesium, iron and calcium. Sodium and chlorine, in the form of chloride, may also be present.
- the process of the present invention provides a process where a refined nickel metal product may be recovered from the mixed hydroxide intermediate by mixing the mixed hydroxide intermediate with a sulphide containing material having reductant properties, most preferably as ground nickel matte, or nickel containing sulphide or concentrate, which in general are impure nickel containing sulphide intermediate products from smelting, selective precipitation or concentration processes.
- a sulphide containing material having reductant properties most preferably as ground nickel matte, or nickel containing sulphide or concentrate, which in general are impure nickel containing sulphide intermediate products from smelting, selective precipitation or concentration processes.
- the combined sulphide containing reductant material / mixed hydroxide intermediate is formed into a slurry and leached under pressure with ammonia to dissolve any nickel, cobalt, copper and zinc while rejecting the majority of the manganese and magnesium.
- the nickel in the solution is treated, preferably with the addition of hydrogen at elevated temperature and pressure to reduce the nickel to a metallic nickel product, most preferably a metallic nickel powder.
- the copper, cobalt and zinc may also be recovered in additional sulphiding recovery stages.
- a process for the recovery of a refined nickel metal product from a mixed hydroxide intermediate that has been produced from the processing of a nickel laterite or sulphide ore including the steps of:
- the metallic nickel product is a metallic nickel powder.
- the mixed hydroxide intermediate is washed with water, preferably desalinated water, or water containing low levels of dissolved salts, prior to forming the intermediate slurry, so as to substantially or partially remove any calcium, sodium and chloride that may be present.
- the washing particularly has the advantage of partially removing some magnesium and sulphate sulphur while converting the remaining magnesium to a less reactive hydroxide form.
- the washed mixed hydroxide intermediate is then formed into an aqueous intermediate slurry.
- this step is achieved by the addition of ammonium sulphate at atmospheric pressure, either in the form of a solution or slurry dosed with ammonium sulphate crystals and preferably containing thiosulphates and polythionates, which enables partial reductive leaching of oxidised manganese, cobalt and nickel.
- the ammonium sulphate or at least a part of the ammonium sulphate used is recycled from the barren solution following the ammonia pressure leach step, while the ammonium sulphate crystals are recycled from a cobalt and zinc sulphiding recovery stage.
- the ammonium sulphate solution or slurry preferably has low titratable ammonia, in the range of 0 to 20g/L before addition of the mixed hydroxide intermediate.
- the intermediate slurry is then mixed with a sulphide containing material, such as ground nickel matte or nickel containing mixed sulphide ahead the ammonia pressure leach step, or it may be mixed during the ammonia pressure leach step.
- a sulphide containing material such as ground nickel matte or nickel containing mixed sulphide ahead the ammonia pressure leach step, or it may be mixed during the ammonia pressure leach step.
- the preferred ratio of mixed hydroxide to matte can vary over a wide range, depending largely on availability of feedstocks and economic considerations. Ratios of up to 1 part nickel in mixed hydroxide intermediate to 1 part nickel in matte or mixed sulphide are preferred, to avoid having to add external reductants, which can be expensive and make process chemistry more difficult to control.
- the ammonia used in the ammonia pressure step is preferably in the form of a gas, liquid or aqueous solution.
- the pressure leach step is preferably conducted at a temperature of from 70 to 120°C and a pressure of from 600 to 1000 kPag in the presence of oxygen and carbon dioxide. This will produce a high concentration of nickel in the leach solution, typically 70 to 1 15 g/l.
- the manganese is oxidised to form an insoluble manganese containing residue.
- the carbon dioxide is absorbed into the ammonia solution and reacts with magnesium to form an insoluble basic magnesium carbonate compound, and to enhance magnesium and manganese precipitation.
- reductants such as metal sulphides, thiosulphates or polythionates are also included into the ammonia pressure leach solution so as to maximise leaching of nickel and cobalt from the mixed hydroxide intermediate.
- the leach slurry will undergo a solid/liquid separation step after this first stage of ammonia pressure leaching, where the leach solution is sent for downstream processing, while the partially leached solids are subjected to a second stage ammonia pressure leach. Air is preferably added to this second stage leach. After a further solid/liquid separation, the first and second stage leach solutions are combined for further processing.
- a third stage ammonia pressure leach of the remaining solids is included with the leach solution added to that of the final and second stage leach.
- the barren ammonia liquor from this stage may be recycled to the atmospheric leach stage in forming the intermediate slurry, or to the ammonia pressure leach step.
- the combined leach solutions containing nickel, cobalt, copper and zinc is first treated to remove copper from the solution before recovery of the nickel, cobalt and zinc.
- the copper may be separately precipitated from the solution in a copper boil process. In this process it is also preferred to adjust the titratable ammonia to nickel molar ratio in the leach solution to the range of 1.8 to 2.2 : 1 , most preferably around 2 : 1 , so as to ensure a minimal amount of cobalt is recovered as metal in the downstream nickel reduction step.
- Copper may also be removed from solution by other techniques such as precipitation with a suitable sulphiding reagent, such as hydrogen sulphide.
- the leach solution preferably undergoes oxydrolysis where it is oxidised with air and heated to remove any remaining thiosulphate, polythionate and sulphamate compounds to avoid potential contamination of nickel and ammonium sulphate products.
- the leach solution then flows to the hydrogen reduction step where hydrogen is added to the solution under pressure at elevated temperature, so as to reduce the nickel to a nickel metal powder.
- Nickel may be recovered by powder/solution separation techniques and the nickel powder formed into other forms such as briquettes.
- cobalt and zinc in particular, may be recovered from the leach solution together with any residual nickel that may remain in the leach solution.
- a suitable sulphiding agent such as hydrogen sulphide, sodium hydrosulphide, sodium sulphide or ammonium sulphide is added to the leach solution following the step of the metallic nickel powder recovery, to recover the cobalt, zinc and any residual nickel as a mixed cobalt/nickel/zinc sulphide product.
- the zinc may advantageously be recovered in a two-stage sulphiding process where the zinc is recovered first in the sulphiding process as a zinc sulphide product, and then the cobalt and any residual nickel recovered in a second stage of the sulphiding process as a mixed nickel/cobalt sulphide product.
- the process also has the advantage that any excess ammonium sulphate formed during this process, may be recovered by crystallisation of ammonium sulphate from the solution.
- steam is used to evaporate the water to enable crystallisation.
- At least a portion of the recovered ammonium sulphate crystals may then be recycled, for use in the atmospheric leach step while forming the intermediate slurry, or the ammonia pressure leach step.
- Figure 1 is a schematic flowsheet of the overall process of a preferred embodiment of the invention.
- Figure 2 is a schematic flowsheet of the leaching phase of the process described in Figure 1.
- Figure 3 is a schematic flowsheet of the product recovery phase of the process described in Figure 1.
- Mixed hydroxide intermediate 100 is water washed 110 using desalinated water 120, to remove or partially remove contaminants. These include magnesium, calcium, sulphate, chloride, and sodium components.
- the water wash can consist of the washing of a filter cake on a filter, re-pulping of the mixed hydroxide intermediate in water to give a "water leach", a combination of these, or other techniques such as continuous counter-current decantation.
- Multiple stages of water washing have been found to be beneficial as has extended leaching times of up to several days. Multiple contacts are especially advantageous for calcium removal, as calcium will continue to leach out of the mixed hydroxide intermediate, constrained only by its solubility limit.
- the washed mixed hydroxide intermediate 140 is initially leached 150 in an ammonium sulphate solution consisting of liquor recycled from the third stage pressure leach 160, dosed with ammonium sulphate crystals 170.
- This leach liquor 190 typically contains 0 to 20 g/L of titratable ammonia, 500 to 600 g/L of ammonium sulphate, and 3 to 6 g/L of thiosulphate and polythionates, enabling reductive leaching of oxidised manganese and cobalt.
- the ammonium sulphate crystal dosing 180 and mixed hydroxide intermediate leaching 150 may be carried out in a combined step.
- the resultant mixed hydroxide intermediate leach slurry 200 is forwarded to the first stage ammonia pressure leach 210 where it is mixed with ground nickel matte 220.
- washed mixed hydroxide intermediate 145 may be directly blended with ground nickel matte 220 ( Figure 2), or the nickel matte 205 in matte grinding step 215 as shown in Figure 1 , ahead of first stage ammonia pressure leach.
- Air 230 and ammonia 240 are added to leach the nickel matte - mixed hydroxide intermediate blend to produce a high nickel concentration in solution - typically 70 to 1 15 g/L, and oxidise manganese to form an insoluble manganese containing leach residue.
- Carbon dioxide which is naturally in air at a concentration of 0.04% by volume or 0.06% by mass, is absorbed into the ammonia solution and reacts with magnesium to form an insoluble basic magnesium carbonate compound. Carbon dioxide can also be added to the leach to enhance magnesium precipitation.
- the leach slurry 250 undergoes solid-liquid separation 260.
- the first stage leach liquor 270 is forwarded to downstream processes for further purification and nickel recovery 280.
- the partially leached solids 290 are subjected to a second stage ammonia pressure leach 300. Air 310 and ammonia 320 are again added to leach the partially leached solids to produce a high concentration nickel solution. If necessary, mixed hydroxide intermediate leach slurry 330 is added to increase the ammonium sulphate concentration to control the leach chemistry.
- the leach slurry 340 undergoes solid-liquid separation 350.
- the second stage leach liquor 360 is mixed with the first stage leach liquor for downstream processing 280.
- the partially leached solids 370 are subjected to a third stage ammonia pressure leach 380. Air 390 and ammonia 400 are again added to leach any remaining nickel.
- Mixed hydroxide intermediate leach slurry 410 may again be added to increase the ammonium sulphate concentration.
- the third stage leach slurry 420 undergoes solid-liquid separation 430.
- the leach residue solids 440 may be further treated by filtration and washing to produce a final filter cake suitable for either disposal or further treatment for metals recovery.
- the third stage leach liquor 160 is forwarded to the ammonium sulphate crystal dosing tank 180.
- Air may be added as separate streams to each pressure leaching stage as shown in Figure 2, or it may be added in a counter-current manner, such that the exhaust air from the Stage 3 leach becomes the feed air to Stage 2 leach 310 and the exhaust air from Stage 2 leach becomes the feed air for Stage 1 leach 230.
- the combined first and second stage leach liquors 280 are forwarded to Copper Boil 510.
- copper is precipitated from solution as copper sulphide product 520, and titratable ammonia levels are adjusted, by the addition of steam 530 and sulphuric acid 540, to a ratio of around 2 moles of ammonia per mole of nickel, in preparation for nickel reduction.
- the reduction feed solution 550 is forwarded to Oxydrolysis 560 where it is oxidised with air 570 and heated with steam 580 to remove any remaining thiosulphate, polythionate and sulphamate compounds which would otherwise cause product contamination.
- the solution 590 then flows into Nickel Pressure Reduction 600, where hydrogen 610 is added in a batchwise manner to an agitated Autoclave to produce nickel metal powder.
- Nickel pressure reduction discharge 620 undergoes powder - solution separation 630.
- Metallic nickel powder product 640 may be transformed into other forms such as briquettes by drying and compacting in a conventional manner.
- the reduction end solution 650 is then treated with a sulphiding reagent such as hydrogen sulphide 660 in a mixed sulphide precipitation step 665 to produce a mixed cobalt-nickel-zinc sulphide product 670.
- the barren ammonium sulphate solution 680 passes to ammonium sulphate crystallisation 690.
- Steam 700 is used to evaporate the water for crystallisation.
- Crystalliser configurations can include multiple effect evaporators, vapour recompression or a combination of both.
- Ammonium sulphate crystal slurry 710 undergoes crystal - liquor separation or drying 720, with the liquor 730 returned to crystallisation.
- Ammonium sulphate crystal is directed to both product 740 and Ammonium Sulphate Crystal Dosing 750 of Third Stage Leach liquor ahead of mixed hydroxide intermediate leaching.
- Typical assays of the mixed hydroxide intermediate and nickel matte refinery feeds are shown in the table below.
- a typical precipitated nickel sulphide analysis is provided, as this is a feed that may partially or totally substitute the nickel matte.
- compositions of the feeds can vary over a significant range from those presented above.
- Mixed hydroxide intermediates can be highly variable in composition. Iron, aluminium and silicon levels vary depending on the efficiency of upstream impurity removal processes. Manganese and cobalt levels vary depending on their concentration relative to nickel in the feed solution to the hydroxide precipitation step, which ultimately reflects on the ore or concentrate feed composition to the leaching process upstream of the mixed hydroxide precipitation step.
- Nickel matte may have differing levels of iron content, depending on the extent to which iron is removed in the smelter converting process. Copper and cobalt levels can also vary significantly, depending on the concentrate feed to the smelter and the converting process used.
- Mixed sulphide precipitates will have varying levels of cobalt, also depending on the on the ore or concentrate feed composition to the leaching process upstream of the mixed sulphide precipitation step.
- the limits of mixed hydroxide intermediate addition depend primarily on economic drivers. As the level of cobalt in refinery feed increases, an equivalent mass of nickel is typically not reduced and reports to mixed sulphide. As a saleable product, the revenue received for the contained nickel in this stream is less than if sold as nickel metal.
- One variant to overcome this limitation is to add the cobalt hexamine precipitation process, as discussed for instance in U.S. Patent 5,468,281 , into the flowsheet. Zinc may reach an economic limit, as refiners of cobalt-nickel-zinc mixed sulphide typically have limits on zinc levels and/or apply penalties for high zinc feeds. This limitation may be overcome by producing separate zinc sulphide and mixed sulphide products by a two stage sulphiding process. The relative quantities of thiosulphates and polythionates that aid manganese and cobalt dissolution will reduce as the proportion of nickel feed from the mixed hydroxide intermediate increases, but this can be compensated for by the addition of other reductant species.
- Nickel pressure reduction capacity is not compromised because the nickel concentration is maintained, due to the co-processing of feedstocks.
- the manganese from the mixed hydroxide intermediate sequesters arsenic and selenium which may be present in the nickel sulphide matte, allowing reduced quantities of iron to be included in the refinery feed for sequestering these elements.
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AU2014360655A AU2014360655B2 (en) | 2013-12-03 | 2014-11-28 | Process for producing refined nickel and other products from a mixed hydroxide intermediate |
CA2931118A CA2931118C (en) | 2013-12-03 | 2014-11-28 | Process for producing refined nickel and other products from a mixed hydroxide intermediate |
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AU2013904693A AU2013904693A0 (en) | 2013-12-03 | Process for producing refined nickel and other products from a mixed hydroxide intermediate |
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Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN109554540A (en) * | 2018-12-26 | 2019-04-02 | 湖南柿竹园有色金属有限责任公司 | A kind of method of bismuth concentrate wet underwater welding bismuth |
JP2020012184A (en) * | 2018-07-20 | 2020-01-23 | 住友金属鉱山株式会社 | Manufacturing method of nickel powder |
CN111874938A (en) * | 2020-08-04 | 2020-11-03 | 安徽乐橙信息科技有限公司 | Preparation method of magnesium-copper hydroxy sulfate nano flower-like material |
Citations (3)
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GB1067007A (en) * | 1964-07-08 | 1967-04-26 | Sherritt Gordon Mines Ltd | Method of leaching high grade nickel matte |
GB1439380A (en) * | 1972-10-20 | 1976-06-16 | Sherritt Gordon Mines Ltd | Production of nickel powder from impure nickel compounds |
US20070166214A1 (en) * | 2003-04-11 | 2007-07-19 | Anderson Peter A | Reductive ammoniacal leaching of nickel and coblat bearing |
-
2014
- 2014-11-28 WO PCT/AU2014/001087 patent/WO2015081368A1/en active Application Filing
- 2014-11-28 CA CA2931118A patent/CA2931118C/en active Active
- 2014-11-28 AU AU2014360655A patent/AU2014360655B2/en active Active
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB1067007A (en) * | 1964-07-08 | 1967-04-26 | Sherritt Gordon Mines Ltd | Method of leaching high grade nickel matte |
GB1439380A (en) * | 1972-10-20 | 1976-06-16 | Sherritt Gordon Mines Ltd | Production of nickel powder from impure nickel compounds |
US20070166214A1 (en) * | 2003-04-11 | 2007-07-19 | Anderson Peter A | Reductive ammoniacal leaching of nickel and coblat bearing |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2020012184A (en) * | 2018-07-20 | 2020-01-23 | 住友金属鉱山株式会社 | Manufacturing method of nickel powder |
JP7091909B2 (en) | 2018-07-20 | 2022-06-28 | 住友金属鉱山株式会社 | Nickel powder manufacturing method |
CN109554540A (en) * | 2018-12-26 | 2019-04-02 | 湖南柿竹园有色金属有限责任公司 | A kind of method of bismuth concentrate wet underwater welding bismuth |
CN111874938A (en) * | 2020-08-04 | 2020-11-03 | 安徽乐橙信息科技有限公司 | Preparation method of magnesium-copper hydroxy sulfate nano flower-like material |
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CA2931118A1 (en) | 2015-06-11 |
AU2014360655A1 (en) | 2016-06-09 |
CA2931118C (en) | 2023-02-14 |
AU2014360655B2 (en) | 2019-06-27 |
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