US3876415A - Concentration of nickel values in oxidized ores - Google Patents

Concentration of nickel values in oxidized ores Download PDF

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US3876415A
US3876415A US32309173A US3876415A US 3876415 A US3876415 A US 3876415A US 32309173 A US32309173 A US 32309173A US 3876415 A US3876415 A US 3876415A
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ore
chloride
temperature
nickel
stage
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Malcolm Charles Evert Bell
James Alexander Evert Bell
Ramamritham Sridhar
Herman Frederik Bakker
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Huntington Alloys Corp
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International Nickel Co Inc
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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
    • C22B23/02—Obtaining nickel or cobalt by dry processes
    • C22B23/021—Obtaining nickel or cobalt by dry processes by reduction in solid state, e.g. by segregation 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

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  • ABSTRACT Concentrates of nickel and/or cobalt are continuously recovered from oxide ores containing same by preheating the ore to at least about 850C. then mixing the ore with at least one chloride selected from the group consisting of alkali metal chlorides.
  • alkaline earth metal chlorides and iron chlorides and holding the mixture at a temperature between about 900C. and 1100C. in a hydrogen-containing atmosphere having a reducing potential equivalent to a COzCO ratio between about 1:2 and 4:1 to convert and concentrate a preponderant part of the nickel and/or cobalt to the metallic state and recovering the metallic concentrate.
  • the present invention pertains to the treatment of nickeliferous oxide ores, and more particularly to the beneficiation of nickel-containing oxide ores.
  • Nickel-containing oxide ores form the largest known reserve of nickel values.
  • these ores are not amenable to conventional beneficiation techniques. as are sulfide ores; and, in most instances, the entire mass of the ore must be hydrometallurgically, pyrometallurgically or vapometallurgically treated to recover the nickel values. Treatment of the entire ore mass is expensive in terms of both capital and operating costs.
  • Nickeliferous oxide ores are not amenable to conventional beneficiation techniques since nickel is present in the ore merely as a dilute substitutional constituent and not as a separate and distinct mineral. Most frequently, oxide ores are a mixture of a highly weathered (or laterized) portion and a less weathered portion. The more weathered portion of oxide ores'can contain up to about 50 percent iron, or even more, and nickel is associated with phases rich in iron or magnesium. In less weathered ore, nickel is contained in silicate minerals. The very nature of these ores is such that they do not respond to physical separation techniques such as flotation or magnetic separation and must be chemically and/or pyrometallurgically treated to concentrate the nickel values.
  • Nickel has been recovered from nickeliferous lateritic ores by smelting the entire mass of the ore in the presence of controlled amounts of reductant to pro prise a ferronickel product. ln a very similar process. nickeliferous lateritic ores are smelted in the presence of a controlled amount of reductant and in the presence of calcium sulfate to produce a ferronickel matte from which nickel can be subsequently recovered. Nickel-containing limonite has been hydrometallurgically treated by leaching with sulfuric acid at elevated temperatures and pressures to selectively dissolve the nickel values, and the resulting pregnant leach solution is treated for nickel and cobalt recovery.
  • Nickel has also been recovered from nickel-bearing lateritic ores by selective reduction followed by leaching with an ammoniacal ammonium carbonate solution from which nickel and cobalt values were recovered. All these processes have in common the same shortcoming, i.e., the entire mass of the ore must be treated to recover the nickel values.
  • nickeliferous oxide ores can be treated in a special manner to place the ore in a condition where nickel values contained therein can be concentrated by physical means to provide a high-grade concentrate which contains at least about percent of the nickel values.
  • Another object of the present invention is to provide a process for continuously concentrating nickel values contained in nickel-bearing lateritic ores.
  • the invention also contemplates providing a process for treating nickel-containing oxide ores on a continuous basis to provide a high-grade nickel concentrate.
  • the present invention contemplates a continuous process for beneficiating nickeliferous oxide ores to produce high-grade nickel concentrates.
  • the nickeliferous oxide ore is preheated to a temperature above about 850C.
  • the preheated ore is mixed with at least one chloride selected from the group consisting of alkali metal chlorides, alkaline earth metal chlorides and iron chlorides, and the mixture is held at a temperature between about 900C. and l,l0OC. in a hydrogen-containing atmosphere having a reducing potential equivalent to a carbon monoxide to carbon dioxide ratio (CO:CO between about 1:2 and 4:1 to produce metallized particles with a preponderant part of the nickel and/or cobalt values being concentrated therein.
  • the metallized particles are recovered by physical means, e.g., flotation or magnetic separation, to provide nickel and/or cobalt concentrates.
  • nickeliferous oxide ores can be treated by the process in accordance with the present invention.
  • the nickeliferous oxide material contains large amounts of iron, large amounts of chlorides as consumed and lower grade concentrates are realized. Best results, in terms of reagent cost, nickel recoveries and concentrate grades, are obtained by treating nickeliferous oxide ores that contain, by weight, at least about 1.5 percent nickel, less than about 30 percent iron, and the balance essentially magnesia, alumina, silica, and moisture.
  • Cobalt in the ore is generally recovered to almost the same extent as nickel, and it is understood in the following that reference to nickel also includes cobalt.
  • a salient feature of the process in accordance with the present invention is that the process is conducted on a continuous basis.
  • the process can be conducted in other apparatus, such as in a multi-hearth furnace having rotating rabble arms for conveying ore from one hearth to another, it is advantageous in terms of capacity, process control and mechanical simplicity, to employ a rotary furnace.
  • a single rotating furnace in which preheating and segregating zones are established can be employed but it is advantageous, for reasons described herein, to employ two rotating furnaces in tandem with one serving as a preheating and/or partial pre-reduction furnace while the other functions as a segregation furnace.
  • One advantage of carrying out the process in two or more stages is to minimize the gas flow through the segregation vessel or the segregation portion of a vessel so that any chloride unavoidably lost from the process is concentrated in a small amount of off gas.
  • This gas can be more economically treated to recover its chloride content thereby eliminating environmental pollution and to provide chloride for recycle thereby lowering the costs of the process.
  • the process in accordance with the present invention minimizes the amount of diluting combustion gases entering the reaction vessel or zone of the reaction vessel in which the segregation process is being carried out.
  • This objective can be achieved in part by minimizing the heat require ments during the segregation part of the process, by using a two-stage process in which dehydration, calcining and heating of the ore to the process temperature is carried out in one reactor or portion of a reactor.
  • the chloride and a reductant, such as particulate carbon are then added to a second vessel or distinct portion of the first vessel, to initiate the segregation part of the process.
  • a still further method of decreasing the gas flow during the segregation reaction period is to preheat the combustion air to this reaction vessel or zone thereof, or to utilize oxygenfor the combustion of the fuel.
  • Another further method of decreasing the heat requirements and concomitant flow of combustion products during the segregation stage is to preheat and dehydrate the chloridizing agent and preheat the reductant before their introduction to the segregation stage.
  • FIG. 1 there is depicted rotating furnaces A and B with the discharging end of furnace A and charging end of furnace B communicating with housing C.
  • Heating furnace A is operated to preheat the nickeliferous oxide ore to predetermined tempera tures while rotary furnace B functions as a segregating furnace. Since the construction of rotary furnaces A and B are similar in most respects, like parts will be given like reference numerals except where there is a substantial difference in construction or function.
  • Rotary furnaces A and B comprise cylindrical steel shells l1 lined with a suitable refractory 12. Rotary furnaces A and B are elevated at a slight angle from the horizontal to facilitate the flow of particulate material from one end to the other. Rotary furnace A which functions as a preheating furnace, can be equipped with internal lifters to further facilitate the flow of particulate material through the furnace and to improve gas-solid contact between the particulate material and the furnace atmosphere. Motors 13 operate via pinion gears 14 which mesh with ring gears 15 to rotate furnaces A and B about their longitudinal axis. Steel tires 16, that are mounted on shells 11 and that ride on thrust bearings 17, stabilize rotary furnaces A and B.
  • the charging end of furnace A communicates with flue system 18 for discharging flue gases.
  • the flow of such gases can be controlled by damper 19.
  • Fresh ore is fed to furnace A from hopper 20 via conveyer 21.
  • the discharge end of furnace A communicates with housing C, and an arrangement of baffles or slides 22 and 23 function to transfer preheated particulate material from furnace A to furnace B.
  • the discharge end of furnace A is equipped with burner 24 which combusts fuel and air to generate heat for preheating particulate ore in furnace A. It will be noted that the products of combustion from burner 24 flow countercurrent to the flow of ore through furnace A to thereby provide more efficient heat exchange.
  • Burner 24 can be operated either with theoretical air or an excess of a free-oxygencontaining gas or with a deficiency of oxygen, producin g a gas of controlled reduction potential. If the burner is operated under reducing conditions, air is admitted by side pipes at points downstream of the burner to combust the remaining combustibles in the gas and thereby obtain maximum fuel efficiency.
  • furnace B communicates with housing C, and preheated material from furnace A is charged to furnace B via slides 22 and 23.
  • Controlled amounts of chlorides, which can be preheated and dehydrated, from hopper 25 are admixed with preheated ore via screw conveyer 26 and slide 23.
  • particulate carbonaceous reductant is admixed with the ore and the chloride from 27 via screw conveyer 28 and slide 23.
  • the mixture of preheated ore, chloride and particulate carbonaceous reductant are maintained at reducing temperatures in furnace B by combusting fuel and free-oxygen-containing gas in burner 29. Burner 29 is operated so that the atmosphere within furnace B is reducing to nickel chloride and essentially non-reducing to ferrous chloride.
  • the products of combustion from burner 29 flow concurrently with the mixture of preheated ore, chloride and particulate reductant. Concurrent flow of the products of combustion from burner 29 is an advantageous feature of the present invention since any chlorine or hydrogen chloride generated by the decomposition of the alkali metal chloride, alkaline earth metal chloride, or iron chloride is not immediately swept from the furnace but is allowed to reside in furnace B sufficiently long to promote segregation reactions.
  • the discharge end of furnace B communicates with housing 30 that functions as a flue system with damper 31 and as a discharge hopper via valve 32.
  • fresh nickel-containing lateritic ore from hopper 20 is fed to furnace A via screw conveyer 21 and is preheated to a temperature of at least about 850C. as it is conveyed through furnace A countercurrent to the products of combustion generated by burner 24.
  • Preheated ore is discharged on slide 22 to slide 23 while controlled amounts of chloride and particulate carbonaceous reductant advantageously preheated to a temperature up to l,lO0C. are added to slide 23 or directly to the rotating furnace.
  • the mixture of preheated ore, chloride and particulate carbonaceous reductant is introduced into furnace B where a slightly to strongly reducing atmosphere and a temperature between about 900C. and 1,050C., e.g., between 920C.
  • Burner 29 is operated from neutral to strongly reducing depending on the amount of solid carbonaceous reductant that is most advantageously employed for the particular ore being treated.
  • Fuel, free-oxygen-containing gases and chlorides can be injected at a plurality of points along the segregation furnace to provide smooth temperature, reducing potential and chloridizing potential profiles within the segregating furnace.
  • the products of combustion of burner 29 pass concurrently with the ore, chloride and particulate carbonaceous reductant through furnace B and are led to housing 30 to be discharged through flue 31.
  • the mixture of ore, chloride and solid carbonaceous material travels through furnace B to housing 30 where it is fed via feeder 32 to means for cooling the mixture of ore, chloride and solid carbonaceous reductant under non-oxidizing conditions.
  • An important feature of the present invention is the preheating of nickeliferous oxide ores to a temperature of at least about 850C. in an atmosphere non-reducing to partially reducing to nickel oxide before adding chlorides and reductants to the ore.
  • the ore is preheated to a temperature between about 920C. and l,O0OC.
  • the process in accordance with the present invention can be conducted by preheating to lower or higher temperatures before additions of chlorides and solid carbonaceous reductants are made, but either lower nickel recoveries, and/or lower grade concentrates (i.e., less than about 6 percent nickel), and/or greater reagent losses and greater fuel consumption are encountered.
  • At least one chloride of a group lAor group 2A element or iron chloride and aparticulate solid carbonaceous reductant are thoroughly mixed with the preheated ore, and the mixture is maintained at a temperature between about 920C. and l,O50.C. in an atmosphere that is substantially reducing to nickel chloride and substantially non-reducing to ferrous chloride.
  • the chloride reagent is added to the ore in amounts, on a weight basis, between about 3 and 12 percent, advantageously in amounts between about 4 and 8 percent. Smaller amounts of the chloride can be added but nickel recoveries suffer.
  • the chloride can be added in amounts exceeding about 12 percent, but any advantages gained by way of increased nickel recoveries are offset by the production of lower grade concentrates and by increased reagent costs.
  • the best results in terms of nickel recovery and grade of concentrates are obtained when chlorides in amounts between about 4 and 8 percent are added to the preheated nickeliferous oxide ore.
  • solid carbonaceous reductant such as coke, coal, charcoal, fuel oil, wood, and lignite, are added to and admixed with the preheated nickeliferous oxide ore.
  • the carbonaceous reductant is advantageously added to the preheated ore in amounts between about 0.5 and 12 percent by weight of the dried, preheated ore.
  • the mixture of preheated ore, chloride and solid carbonaceous reductant is held at a temperature between about 950C. and 1,050C. in an atmosphere that is reducing to nickel chloride and essentially non-reducing to ferrous chloride.
  • the mixture is held at a temperature between about 970C. and 1,020C. in order to insure high nickel recoveries and high grade concentrates while minimizing mechanical problems associated with sticking and minimizing fuel consumption.
  • at least about percent, and in most instances about percent or more, of the nickel in the ore is reduced from the gaseous state to the metallic state and canbe easily separated from the ore by magnetic separation techniques or, after suitably activating the precipitated metal values, by flotation techniques.
  • residence times between about 0.5 hour and 2 hours are usually sufficient to insure nickel recoveries of at least about 75 percent.
  • the gaseous effluent from the second stage reactor can be cleaned in conventional wet scrubber to remove HC], FeCl and any traces of nickel chloride from the gas.
  • the solution may be neutralized with a base such as limestone, and the calcium chloride-iron chloride solution dried and recycled for use. Alternatively, the solution could be neutralized with reduced ore.
  • test C the hot partially reduced ore was fed to a segregating zone where 3% coke and calcium chloride, both based on the weight of the reduced ore, were added to the ore and the mixture was maintained at The kiln was continuously purged concurrently with 5 1,000C. for 1 hour.
  • Test D was conducted under i ia gaseous mixture of 2 2 and 2- 'fl runs lar conditions except 5% coke along with 5% calcium were Carried out at different gas flowrates- The Product chloride was added to the hot calcined ore. The cooled was allowed to Cool to room temperature and ore from both tests was ground to pass through 325 ground through 200 mesh and magnetically Separated mesh and magnetic concentrates were recovered by at 4800 gauss in a Davis tube. The adverse effects of wet magnetic Separation in a Davis tube at 4800 gauss. high gas flowrates are confirmed by the results reported Th results f t st C and D are summarized in Table in Table l. I]
  • EXAMPLE 11 This example confirms that a portion of the nickel values contained in oxide ores can be prereduced without materially altering nickel recoveries.
  • test C the ore was prereduced at 1,000C. in an atmosphere having a reducing potential equivalent to a CO:CO ratio of 1:4 to reduce about 17% of the nickel values while maintaining 99% of the iron in the oxide state and to expel all structurally bound water.
  • the ore for test D was calcined at 1,000C. to expel all structurally bound water.
  • EXAMPLE 111 This example confirms that higher grade nickel concentrates are recovered from ores having lower iron contents, even though nickel recoveries remain substantially constant.
  • EXAMPLE IV TABLE IV 850 to about 1,1000C; mixing the hot preheated ore which is at a temperature of above about 850C. with at least one chloride selected from the group consisting of alkali metal chlorides, alkaline earth metal chlorides, and iron chloride; maintaining the mixture of ore and chloride at a temperature between about 900C. and 1,100C.
  • a continuous process for beneficiating nickeliferous oxide ores having an iron content of up to about 50% which comprises establishing within at least one rotary furnace a preheating zone and a segregating zone; continuously feeding nickeliferous oxide ores to the preheating zone; preheating the nickeliferous oxide ore to a temperature above 850C. to about 1,100C.
  • preheating zone continuously conveying the preheated nickeliferous oxide ore while hot to the segregating zone; introducing and intimately mixing controlled amounts of a particulate solid carbonaceous reductant and of at least one chloride selected from the group consisting of alkali metal chlorides, alkaline earth metal chlorides, and iron chloride to the preheated ore which is at a temperature above about 850C; maintaining the mixture of preheated ore, chloride and carbonaceous reductant at a temperature between about 900C. and 1,100C.
  • chloride selected from the group consisting of alkali metal chlorides, alkaline earth metal chlorides, and iron chloride
  • nickeliferous ore contains at least about 1.5% nickel and less than about 30% iron.
  • a two-stage process for beneficiaating nickeliferous oxide ores having an iron content of up to about 35 percent which comprises a preheating stage and a segregating stage, said ore being subjected in the segregating stage to an elevated temperature in the presence of a reducing agent and a chloride, the steps comprising preheating the ore containing oxide nickel values to a temperature above about 850C to about 1,100C in a reducing atmosphere to dehydrate, calcine, heat and partially reduce the ore, the reduction potential of said reducing atmosphere being such that not greater than about 50 percent of the nickel values in said ore are reduced, the heat to said preheating-partial reduction stage being provided by a direct heating means; continuously conveying the hot partially reduced nickeliferous oxide ore to the segregating stage, introducing and intimately mixing controlled amounts of a particulate solid carbonaceous reductant and at least one chloride selected from the group consisting of alkali metal chlorides, alkaline earth metal chlorides, and iron chloride to the hot partially reduced

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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4002463A (en) * 1975-04-04 1977-01-11 Financial Mining - Industrial And Shipping Corporation Upgrading the nickel content from low grade nickel lateritic iron ores
US4047934A (en) * 1975-05-07 1977-09-13 Ici Australia Limited Beneficiation of the non-ferrous metal values of oxide-containing materials
FR2396800A1 (fr) * 1977-07-08 1979-02-02 Ici Australia Ltd Procede de traitement de particules de matiere metallifere
US4144056A (en) * 1978-05-04 1979-03-13 Cato Research Corp. Process for recovering nickel, cobalt and manganese from their oxide and silicate ores
US4295878A (en) * 1977-07-08 1981-10-20 Ici Australia Limited Processes of iron segregation
WO1982001381A1 (en) * 1980-10-22 1982-04-29 Baeck Erik G A method for the chlorinating refinement of iron raw materials
US20040109810A1 (en) * 2002-12-04 2004-06-10 Khozan Kamram M Process for producing nickel carbonyl, nickel powder and use thereof
EA007371B1 (ru) * 2005-12-16 2006-10-27 Товарищество С Ограниченной Ответственностью "Горное Бюро" Установка для переработки окисленных никелевых руд
EA012619B1 (ru) * 2008-08-29 2009-10-30 Товарищество С Ограниченной Ответственностью "Горное Бюро" Способ переработки окисленных никелевых руд
CN107663593A (zh) * 2016-07-29 2018-02-06 江学艺 含钴、镍矿的富集方法
CN117721325A (zh) * 2024-02-07 2024-03-19 矿冶科技集团有限公司 一种从红土镍矿中提取镍钴铁的方法

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FI93974C (fi) * 1992-06-18 1995-06-26 Outokumpu Harjavalta Metals Oy Menetelmä sulfidisten, vaikeasti sulatettavien nikkelirikasteiden tai vastaavien seosten hyödyntämiseksi
CA2461624C (en) * 2003-03-27 2005-10-18 Chemical Vapour Metal Refining Inc. Process for producing nickel carbonyl, nickel powder and use thereof
EA200700744A1 (ru) * 2007-04-27 2007-12-28 Товарищество С Ограниченной Ответственностью "Горное Бюро" Установка для переработки окисленных никелевых руд

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US1487145A (en) * 1923-05-25 1924-03-18 Clevenger & Caron Process of recovering values from nickel and cobalt-nickel ores
US2473795A (en) * 1944-05-10 1949-06-21 Nicaro Nickel Company Reduction of ores containing nickel
US2733983A (en) * 1956-02-07 fecij
US2850376A (en) * 1954-12-28 1958-09-02 Int Nickel Co Treatment of nickel-containing laterite ores
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US3272616A (en) * 1963-12-30 1966-09-13 Int Nickel Co Method for recovering nickel from oxide ores
US3311466A (en) * 1963-11-29 1967-03-28 Int Nickel Co Reduction of metal oxides
US3453101A (en) * 1963-10-21 1969-07-01 Fuji Iron & Steel Co Ltd Process for treating nickeliferous ore
US3656934A (en) * 1969-03-28 1972-04-18 Int Nickel Co Rotary kiln reduction of limonitic ores
US3658508A (en) * 1970-02-11 1972-04-25 Sherritt Gordon Mines Ltd Process for controlled reduction roasting of nickeliferous iron oxide ores
US3667933A (en) * 1965-06-23 1972-06-06 Metallgesellschaft Ag Rotary kiln reduction of iron oxides with pneumatic feeding of a portion of the charge
US3701647A (en) * 1969-02-17 1972-10-31 Nippon Mining Co Process for obtaining nickel concentrates from nickel oxide ores
US3725039A (en) * 1970-12-10 1973-04-03 Basic Inc Recovery of nickel concentrates from laterite ores

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FR1160093A (fr) * 1956-10-25 1958-07-07 Renault Traitement des minerais silicatés de nickel
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US2733983A (en) * 1956-02-07 fecij
US1480212A (en) * 1921-07-12 1924-01-08 Lamothe Jacques De Fonds Process of manufacture of ingots of pure nickel from impure oxides of nickel
US1487145A (en) * 1923-05-25 1924-03-18 Clevenger & Caron Process of recovering values from nickel and cobalt-nickel ores
US2473795A (en) * 1944-05-10 1949-06-21 Nicaro Nickel Company Reduction of ores containing nickel
US2850376A (en) * 1954-12-28 1958-09-02 Int Nickel Co Treatment of nickel-containing laterite ores
US2998311A (en) * 1958-08-25 1961-08-29 Int Nickel Co Processing nickel-containing lateritic ores
US3453101A (en) * 1963-10-21 1969-07-01 Fuji Iron & Steel Co Ltd Process for treating nickeliferous ore
US3311466A (en) * 1963-11-29 1967-03-28 Int Nickel Co Reduction of metal oxides
US3272616A (en) * 1963-12-30 1966-09-13 Int Nickel Co Method for recovering nickel from oxide ores
US3667933A (en) * 1965-06-23 1972-06-06 Metallgesellschaft Ag Rotary kiln reduction of iron oxides with pneumatic feeding of a portion of the charge
US3701647A (en) * 1969-02-17 1972-10-31 Nippon Mining Co Process for obtaining nickel concentrates from nickel oxide ores
US3656934A (en) * 1969-03-28 1972-04-18 Int Nickel Co Rotary kiln reduction of limonitic ores
US3658508A (en) * 1970-02-11 1972-04-25 Sherritt Gordon Mines Ltd Process for controlled reduction roasting of nickeliferous iron oxide ores
US3725039A (en) * 1970-12-10 1973-04-03 Basic Inc Recovery of nickel concentrates from laterite ores

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4002463A (en) * 1975-04-04 1977-01-11 Financial Mining - Industrial And Shipping Corporation Upgrading the nickel content from low grade nickel lateritic iron ores
US4047934A (en) * 1975-05-07 1977-09-13 Ici Australia Limited Beneficiation of the non-ferrous metal values of oxide-containing materials
FR2396800A1 (fr) * 1977-07-08 1979-02-02 Ici Australia Ltd Procede de traitement de particules de matiere metallifere
US4295878A (en) * 1977-07-08 1981-10-20 Ici Australia Limited Processes of iron segregation
US4144056A (en) * 1978-05-04 1979-03-13 Cato Research Corp. Process for recovering nickel, cobalt and manganese from their oxide and silicate ores
WO1982001381A1 (en) * 1980-10-22 1982-04-29 Baeck Erik G A method for the chlorinating refinement of iron raw materials
US20040109810A1 (en) * 2002-12-04 2004-06-10 Khozan Kamram M Process for producing nickel carbonyl, nickel powder and use thereof
US7198770B2 (en) * 2002-12-04 2007-04-03 Chemical Vapour Metal Refining, Inc. Process for producing nickel carbonyl, nickel powder and use thereof
EA007371B1 (ru) * 2005-12-16 2006-10-27 Товарищество С Ограниченной Ответственностью "Горное Бюро" Установка для переработки окисленных никелевых руд
EA012619B1 (ru) * 2008-08-29 2009-10-30 Товарищество С Ограниченной Ответственностью "Горное Бюро" Способ переработки окисленных никелевых руд
CN107663593A (zh) * 2016-07-29 2018-02-06 江学艺 含钴、镍矿的富集方法
CN117721325A (zh) * 2024-02-07 2024-03-19 矿冶科技集团有限公司 一种从红土镍矿中提取镍钴铁的方法
CN117721325B (zh) * 2024-02-07 2024-05-14 矿冶科技集团有限公司 一种从红土镍矿中提取镍钴铁的方法

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ZA73533B (en) 1973-10-31
DE2306475C3 (de) 1975-12-04
AU447098B2 (en) 1974-04-11
DE2306475A1 (de) 1973-08-16
CA965961A (en) 1975-04-15
DE2306475B2 (de) 1975-04-24
GB1401718A (en) 1975-07-30
FR2171380A1 (OSRAM) 1973-09-21
AU5151773A (en) 1974-04-11
BR7300943D0 (pt) 1973-09-25
JPS4889121A (OSRAM) 1973-11-21
FR2171380B1 (OSRAM) 1975-10-31

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