US3860415A - Process for preparing aluminum - Google Patents

Process for preparing aluminum Download PDF

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Publication number
US3860415A
US3860415A US27738372A US3860415A US 3860415 A US3860415 A US 3860415A US 27738372 A US27738372 A US 27738372A US 3860415 A US3860415 A US 3860415A
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United States
Prior art keywords
aluminum
ore
silicon
kyanite
alloy
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English (en)
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Marcelian F Gautreaux
John H Mccarthy
Walter E Foster
Donald O Hutchinson
Frederick W Frey
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Ethyl Corp
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Ethyl Corp
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Priority to US05277383 priority Critical patent/US3860415A/en
Priority to US344213A priority patent/US3860416A/en
Priority to CA175,617A priority patent/CA985911A/en
Priority to GB3422473A priority patent/GB1415475A/en
Priority to DE2337339A priority patent/DE2337339C3/de
Priority to NO298773A priority patent/NO136542C/no
Priority to AU58743/73A priority patent/AU477098B2/en
Priority to CH1120673A priority patent/CH594737A5/xx
Priority to FR7328187A priority patent/FR2194790B1/fr
Priority to SE7310665A priority patent/SE404032B/xx
Priority to JP8721573A priority patent/JPS4953514A/ja
Priority to US05/484,397 priority patent/US3954443A/en
Application granted granted Critical
Publication of US3860415A publication Critical patent/US3860415A/en
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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
    • C22B21/00—Obtaining aluminium
    • C22B21/02—Obtaining aluminium with reducing
    • 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
    • C22B21/00—Obtaining aluminium
    • C22B21/0007—Preliminary treatment of ores or scrap or any other metal source
    • 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

  • ABSTRACT A process for producing aluminum from raw aluminum silicate ore, especially kyanite, including crushing and grinding a natural or raw mined kyanite ore to a desired particle size, beneficiating the ore to form a kyanite concentrate, compacting the concentrate [52] 75/5 75/68 56 32 along with a carbon reductant into agglomerates such as briquettes, pellets or other suitable form and to a 21/00, 1 3/ g gg g desired size, carbothermically reducing the ore com- 260/448 pacts in an electric arc furnace into an aluminumsilicon alloy, comminuting the aluminum-silicon alloy into a desired particle size, hydroaluminating the [56] References Clted aluminum-silicon alloy particles with hydrogen and UNITED STATES PATENTS propylene to form tripropylaluminum and di
  • the silicon rich residue from the hydroalumination reaction is conducted to a furnace wherein lime, silicon-dioxide and iron, if necessary, are added to produce ferro-silicon alloy.
  • the present invention is in the field of aluminum extraction and reduction and particularly relates to a direct-reduction process for producing aluminum from a raw or natural aluminum silicate ore such as kyanite and sillimanite.
  • alumina Al- O is first extracted from bauxite ore and the alumina is then electrolytically reduced in molten cryolite (sodium aluminum fluorides) to free aluminum metal.
  • molten cryolite sodium aluminum fluorides
  • Bauxite comprises 45 to 60 percent aluminum oxide, 3 to 25 percent iron oxide, 2.5 to 18 percent silicon oxide, 2 to 5 percent titanium oxide, up to one percent other impurities, combined with 12 to 30 percent water of crystallization.
  • the ore varies greatly in the proportions of its constituents, and in color and consistency.
  • Gibbsite, boehmite and diaspore are the hydrated aluminum oxide minerals normally found in bauxite.
  • the Bayer process for producing alumina basically involves a caustic leach at elevated temperature and pressure, followed by separation of the resulting sodium aluminate solution, and selective precipitation of the alumina.
  • the European Bayer in which the approximate conditions of leaching are at a pressure of 210 pounds per square inch, a temperature of 390F, a caustic concentration of 400 grams per liter, and a digestion time of 2 to 8 hours to effect solution of the monohydrate mineral boehmite; and
  • the American Bayer in which a pressure of about 60 pounds per square inch, a temperature of about 290F, a caustic concentration of 170 grams per liter, and a digestion time ofone-half to one hour are used to dissolve the trihydrate mineral gibbsite.
  • the pregnant solution is separated from the red mud tailings by countercurrent decantation and filtration.
  • the liquor is cooled until it becomes supersaturated, then seeded with crystals of aluminum trihydrate.
  • About one-half of the alumina in solution is precipitated in a 36 to 96 hour period.
  • the precipitate is then filtered, washed and calcined at 2,000F to obtain the final product.
  • Caustic soda is regenerated in the precipitation step and, together with the unprecipitated alumina, is recycled to the digesters.
  • the finely divided residue resulting from leaching contains Fe O TiO and a complex sodium aluminum silicate compound, the latter representing a loss of soda and alumina.
  • the quantity discarded in the residue is related to the silica content of the bauxite. Approximately 1.1 units of alumina and 1.2 units of soda are lost for each unit of silica in the ore.
  • the bauxite must contain less than 8 percent silica. Approximately four long dry tons of bauxite are required to produce two short tons of alumina, which upon electrolysis yields slightly more than 1 short ton of aluminum.
  • the Bayer process requires soda ash, lime for causticizing the soda ash and fuel oil, gas or coal.
  • Bayer-Hall process Some modifications of the Bayer-Hall process have been made in order to utilize bauxite ores containing 12 to 15 percent silica.
  • the ore is first subjected to a Bayer leach.
  • the resulting red mud which contains a complex sodium aluminum silicate compound, is sintered with limestone and soda ash, then leached with water to recover alumina and soda.
  • the brown mud residue has a composition, on a dry basis, somewhat similar to that of portland cement. This process requires additional costs in capital investment, raw materials and processing, and the upper limit ofsilica for use in the process is about 15 percent.
  • BayerHall process Another disadvantage of the BayerHall process is its necessity for an adequate, dependable and long-range supply of alumina requiring discovery of new sources of raw materials and the solution of numerous mining and metallurgical problems. Problems of the process include the need for improving efficiency and development of methods for utilizing tailings. Mechanical beneficiation of low-grade bauxites is hampered by the high loss of alumina in removing iron and silica. A need therefore exists for a direct reduction process that frees aluminum from crude feed material and which material is readily available.
  • alumina is extracted commercially from high-iron bauxites by the Pedersen smelting process.
  • bauxite, limestone, coke and iron ore are smelted in an electric furnace to produce pig iron and a calcium aluminate slag containing 30 to 50 percent alumina.
  • the slag is leached with sodium carbonate solution, and the alumina trihydrate is precipitated by carbon dioxide.
  • Aluminum-containing metal feed e.g., bauxite reduced with coke
  • gaseous AlCl or the tribromide
  • the gaseous subhalide monoochloride or monobromide
  • Aluminum is recovered in a molten, substantially pure state.
  • the aluminum trihalide is recirculated to produce additional mono-halide. Severe temperature conditions, problems of handling hot metal, and the corrosive nature of the gases create many difficulties in operating the process.
  • bauxite is partially reduced with carbon in an electric furnace, then it is further reduced with carbon to produce a mixture of aluminum and aluminum carbides. The aluminum is separated and the aluminum carbide recycled. Little or no commercial success has been achieved with this process.
  • Such processes include the treatment of alumina with aluminum sulfide and carbon at an elevated temperature; hydrogen reduction of alumina at above 100 atmospheres and above 400C; reaction between alumina and aluminum carbide at l,980C; and electrolytic reduction of complex organoaluminum compounds such as NaF2Al(C H)
  • Another process comprises chlorinating alumina containing materials in a reactor to yield aluminum trichloride and reacting the aluminum trichloride with manganese to yield aluminum and manganese chloride.
  • the present invention is particularly adapted to overcome the disadvantages, problems and difficulties of these prior art processes.
  • Another object of the present invention is to provide a process for producing substantially pure aluminum which is more economical than prior art processes.
  • Still another object of the present invention is to provide a process for producing aluminum wherein little or none of the materials used therein is lost in processing.
  • a further object of the instant invention is to provide a new direct reduction process for aluminum which also provides a ferro-silicon alloy as a second principal product thereof.
  • the present invention provides a process for producing substantially pure aluminum from mined aluminum silicate ore, especially kyanite ore and comprises the following basic steps:
  • the mined kyanite ore is crushed and ground in suitable equipment to a particle size of about 600 microns to about 44 microns and preferably less than about 500 microns or about -35 mesh.
  • the ground kyanite ore is beneficiated to form a kyanite concentrate.
  • a kyanite-quartz flotation process is preferred.
  • the ground kyanite ore is subjected first to a scrubbing and desliming process in which various micas are primarily removed.
  • the ground kyanite ore is then subjected to a combination magnetic separation and flotation treatment and tabling if desired.
  • the kyanite is non-magnetic.
  • the ground kyanite ore is then subjected to a reductive roast and further magnetic separation to remove residual iron species.
  • the particular beneficiation selected will vary with the type of ore.
  • the kyanite concentrate is then compacted into agglomerates.
  • Briquettes of from about 1 inch X 1 /2 inches X /1 inch to about 2 inches X 2 inches X 1 inch formed in suitable briquetting or like equipment utilizing suitable binders have been found to be particularly satisfactory. In some instances it may be desired to compact ore-carbon pellets, briquettes, or other suitable agglomerates.
  • the aluminum-silicon alloy is then comminuted to a particle size of from about 150 microns to about 10 microns.
  • a powder with a medium particle size of about microns is particularly desirable.
  • the alloy may be cast and ground to the desired size, blown from the melt, or comminuted by water spray.
  • the aluminumsilicon alloy particles are transferred to a suitable reactor and treated with propylene and hydrogen and a sodium catalyst under desired temperatures and pressures to form tripropylaluminum (TNPA) and dipropylaluminum hydride (DNPAH).
  • TNPA tripropylaluminum
  • DNPAH dipropylaluminum hydride
  • the TNPA and DNPAH are pyrolyzed or decomposed in an inert diluent such as a hydrocarbon oil in a suitable reactor to form aluminum powder, propylene and hydrogen.
  • an inert diluent such as a hydrocarbon oil
  • propane is produced in the pyrolysis and most of it is vented off and recovered.
  • the recycle gas stream is compressed back to the hydroalumination reactor and propane is separated out during compression. Propylene and hydrogen purged from the process after they are reacted are transferred to the hydroalumination reactor.
  • the aluminum powder is filtered and washed with a light hydrocarbon or oil such as hexane and then dryed and compacted into a desired form or shape.
  • a light hydrocarbon or oil such as hexane
  • the diluent oil is separated from the wash and preferably recycled to the decomposition step. The process can also be ended here.
  • the aluminum powder compacts are then melted and fluxed with chlorine gas or metal chlorides and fluorides, and then cast into pigs, sows or other desired shapes.
  • a flux comprised of sodium chloride, potassium chloride and cryolite is especially beneficial, but other suitable fluxes may be used.
  • chlorine gas is bubbled into the molten metal.
  • an inert gas carrier such as nitrogen is used.
  • a most preferred fluxing gas is chlorine plus carbon monoxide and nitrogen.
  • silicon residue which is filtered from the hydroalumination product, is heated in a suitable furnace with calcium oxide, silicon dioxide and if needed, additional iron to produce a ferro-silicon alloy of a desired ratio of silicon and iron.
  • the alloy is separated from slag and cast into chills, pigs, sows, or other desired shapes.
  • the minus 35 ore is then beneficiated via flotation circuits for the removal of various micas, pyrites and quartz sand. Iron oxides are reduced in a rotary kiln and separated from the kyanite concentrate with high intensity magnets. Garnet is also removed during magnetic separation. Process waters from the beneficiation process are recycled.
  • the kyanite concentrate is prepared, it is then briquetted to provide a suitable furnace feed.
  • Pillow shaped briquettes of a size of about 2 inches by 2 inches by 1 inch are prepared. Agglomeration of the finely ground kyanite is necessary for good furnace operation.
  • fume from the electric arc furnace is recycled to the briquetting oper ation where it is used as a binder and subsequently fed back into the arc furnace. Slag from the furnace is also recycled to the briquetting operation. Reducing agents are mixed with the ore and slag prior to briquetting. Coke and coal fines are used.
  • the fixed carbon in the reducing agents should supply about 90-l 10 percent of the theoretical carbon required to reduce the ore and preferably 95-105 percent.
  • the fixed carbon content of the carbon feed is about 12% wood, coal and 28% coke.
  • the briquettes or pellets of kyanite concentrate are then transferred to an electric arc furnace for reduction to an aluminum-silicon alloy.
  • Aluminum-silicon alloy is tapped from the furnace and cast into suitable molds.
  • the cast alloy is then comminuted to a conventional size for hydroalumination.
  • the large castings may be transferred directly to a large crusher or impact mill where they are reduced to 6 inch lumps, or they may be broken up by a concrete breaker, jack hammer or other suitable equipment to lumps or pieces of about 6 inches.
  • the small pieces of alloy are then submitted to secondary crushing techniques in conventional equipment until they are reduced to particles of about A inch.
  • the small particles of crushed alloy are fed to a ball mill and further reduced to about a l00 mesh powder.
  • the ground alloy is then conveyed to a hydroalumination reactor for further processing.
  • a tripropylaluminum (TNPA) hydroalumination process is used to separate aluminum from the silicon in the alloy.
  • Hydroalumination may be carried out in a continuous process, wherein hydrogen and propylene and some TNPA and a suitable catalyst, e.g. sodium, are continuously introduced into a hydroalumination reactor along with a stream of alloy to produce tripropylaluminum (TNPA) anddipropylaluminum hydride (DNPAH). After a suitable residence time in the reactor TNPA and DNPAH product is filtered or centrifuged and is transferred to a pyrolysis or decomposition reactor.
  • TNPA tripropylaluminum
  • a preferred hydroalumination step several reactors are used with alloy being fed to the first one or two at a controlled rate under controlled conditions.
  • Propane formed in the pyrolysis step, as well as during the hydroalumination operation, is vented and used for fuel.
  • Depletion of free aluminum in the alloy is in excess of
  • silicon residue from the hydroalumination reaction is removed from the TNPA via suitable filtration, e.g. a horizontal leaf filter, and transferred to a furnace for making ferro-silicon alloy.
  • the pyrolysis or decomposition of the TNPA- DNPAH mixture is carried out in a series of reactors in an inert hydrocarbon medium. Hydrogen and olefin (propylene) as well as by-product paraffin (propane) produced are transferred to the hydroalumination reactor. Propylene recovery is in excess of 90%. Most ofthe propane produced is vented off and recovered. The recycle gas stream is compressed back to the hydroalumination reactor and propane is separated out during compression.
  • Aluminum is produced in the form of powder in the oil slurry.
  • the aluminumoil mixture is filtered, with the aluminum being separated therefrom, washed with hexane and dryed.
  • the oil or inert hydrocarbon and alkyl bottoms mixture is recycled to the pyrolysis reactor after flashing the hexane-oil-alkyl mixture. Substantially all of the hexane is recovered.
  • the hexane-wet aluminum powder is dried in any suitable manner, e.g. in steam-tube dryers. Vaporized liquids are condensed and recycled to the wash recovery operation. Oxygen exposure of the fresh aluminum surface is minimized during the washing and drying operations.
  • the dry aluminum powder is briquetted and fed to a conventional melting furnace. Fluxing is desirable and a flux composition of 60% sodium chloride and 40% cryolite, by weight, produces excellent results. A gas flux, such as chlorine, or any other suitable flux may be used. Molten pure aluminum from the melting furnace is cast into suitable ingots. A direct chill ingot casting machine is preferable, but other casting apparatus may be used.
  • ferrosilicon alloy is also produced as co-product.
  • Silicon residue powder from the filtration or centrifugation of the TNPA is mixed with iron, normally in the form of steel turnings, quartz and limestone and fed into a slag resistance furnace or other suitable furnace to produce a ferro-silicon alloy.
  • Molten ferro-silicon alloy is tapped from the furnace periodically and cast into suitable containers for further handling as desired.
  • Slag produced from the ferro-silicon furnace is also cast and subsequently crushed to particles of about 1 inch. The crushed and ground slag is then preferably recycled to the kyanite briquetting plant, but may be disposed of if desired.
  • the hydroalumination reaction for producing aluminum alkyls is an exothermic one and some of the simultaneous reactions proceed at a faster rate than others.
  • the reaction also produces paraffins. In a commercial operation, it is necessary that the rate of reaction be sufficiently fast to minimize the size of equipment needed and to reduce paraffin formation.
  • TEA triethylaluminum
  • TIBA triisobutylaluminum
  • TNPA is the preferred intermediate, over TEA and TIBA, in the aluminum process described herein.
  • This invention is particularly directed to the use of aluminum silicate ores which contain substantial amounts of aluminum and silicon. Economically, the raw ore should contain at least 20% or a sillimanite group mineral.
  • Kyanite, sillimanite and andalusite are the principal minerals comprising the sillimanite group of ores or minerals.
  • a kyanite ore is defined as any aluminum silicate ore which contains 20% or more of a mineral having equal parts A1 and SiO
  • a kyanite concentrate is defined as a kyanite ore which has been beneficiated to remove substantial amounts of impurities or materials other than kyanite.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Metallurgy (AREA)
  • Manufacturing & Machinery (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
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  • Manufacture And Refinement Of Metals (AREA)
  • Refinement Of Pig-Iron, Manufacture Of Cast Iron, And Steel Manufacture Other Than In Revolving Furnaces (AREA)
US05277383 1972-08-02 1972-08-02 Process for preparing aluminum Expired - Lifetime US3860415A (en)

Priority Applications (12)

Application Number Priority Date Filing Date Title
US05277383 US3860415A (en) 1972-08-02 1972-08-02 Process for preparing aluminum
US344213A US3860416A (en) 1972-08-02 1973-03-23 Modified aluminum process
CA175,617A CA985911A (en) 1972-08-02 1973-07-04 Aluminum process
GB3422473A GB1415475A (en) 1972-08-02 1973-07-18 Aluminium process
DE2337339A DE2337339C3 (de) 1972-08-02 1973-07-23 Verfahren zur Herstellung von Aluminium durch carbothermische Reduktion von Kyanit
NO298773A NO136542C (no) 1972-08-02 1973-07-24 Fremgangsm}te til utvinning av aluminiummetall og ferrosilicium fra kyanittmalm.
AU58743/73A AU477098B2 (en) 1972-08-02 1973-07-31 Aluminum process
CH1120673A CH594737A5 (enrdf_load_stackoverflow) 1972-08-02 1973-07-31
FR7328187A FR2194790B1 (enrdf_load_stackoverflow) 1972-08-02 1973-08-01
SE7310665A SE404032B (sv) 1972-08-02 1973-08-02 Forfarande for framstellning av aluminium genom karbotermisk reduktion av ett aluminiumkiselmineral, hydroaluminering och pyrolys av bildad aluminiumalkylforening
JP8721573A JPS4953514A (enrdf_load_stackoverflow) 1972-08-02 1973-08-02
US05/484,397 US3954443A (en) 1972-08-02 1974-07-01 Aluminum process

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US05/484,397 Continuation-In-Part US3954443A (en) 1972-08-02 1974-07-01 Aluminum process

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US (1) US3860415A (enrdf_load_stackoverflow)
JP (1) JPS4953514A (enrdf_load_stackoverflow)
AU (1) AU477098B2 (enrdf_load_stackoverflow)
CA (1) CA985911A (enrdf_load_stackoverflow)
CH (1) CH594737A5 (enrdf_load_stackoverflow)
DE (1) DE2337339C3 (enrdf_load_stackoverflow)
FR (1) FR2194790B1 (enrdf_load_stackoverflow)
GB (1) GB1415475A (enrdf_load_stackoverflow)
NO (1) NO136542C (enrdf_load_stackoverflow)
SE (1) SE404032B (enrdf_load_stackoverflow)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4303204A (en) * 1976-10-28 1981-12-01 Reynolds Metals Company Upgrading of bauxites, bauxitic clays, and aluminum mineral bearing clays
US6072821A (en) * 1997-06-03 2000-06-06 Kanthal Ab Method for heat treating materials at high temperatures, and a furnace bottom construction for high temperature furnaces
CN101775493B (zh) * 2010-01-08 2012-07-04 甘肃紫鑫矿业煤化工有限公司 用红柱石原矿为原料直接还原制备硅钡铝钙钛多元合金的方法
CN103695656A (zh) * 2013-12-04 2014-04-02 台澳铝业（台山）有限公司 一种铝灰回收利用方法
CN104513902A (zh) * 2013-09-30 2015-04-15 林州市林丰铝电有限责任公司 一种铝渣回收方法
CN111167831A (zh) * 2020-01-03 2020-05-19 武翠莲 一种催化分解含铝硅酸盐的方法
US11739395B1 (en) * 2022-05-05 2023-08-29 The United States Of America As Represented By The Secretary Of The Navy Embrittled aluminum alloys for powder manufacturing

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2801274B1 (de) * 1978-01-13 1978-08-31 Vaw Ver Aluminium Werke Ag Verfahren zur Herstellung stabiler Pellets fuer den Saeureaufschluss von aluminiumsilikathaltigen Erzen
JPS591777B2 (ja) * 1980-04-22 1984-01-13 三井アルミニウム工業株式会社 アルミニウムの還元製錬法
SE450583B (sv) * 1982-10-22 1987-07-06 Skf Steel Eng Ab Sett att framstella aluminium-kisel-legeringar
CN106077682B (zh) * 2016-07-29 2018-02-16 刘冠华 一种浓缩高纯活性铝粉的装置及方法

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US602976A (en) * 1898-04-26 Guillaume de chalmot
US2755178A (en) * 1952-07-30 1956-07-17 Robert T C Rasmussen Electric smelting process for production of silicon-aluminum alloys
US2757077A (en) * 1953-06-12 1956-07-31 Crucible Steel Co America Method of recovering metallic values from ores containing iron and nickel
US3112179A (en) * 1960-11-30 1963-11-26 Gen Aniline & Film Corp Preparation of iron and nickel carbonyls
US3155493A (en) * 1960-08-12 1964-11-03 Sumitomo Chemical Co Method for manufacturing high purity aluminum
US3535108A (en) * 1969-09-22 1970-10-20 Ethyl Corp Process for producing aluminum

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FR1309217A (fr) * 1961-08-09 1962-11-16 Sumitomo Chemical Co Procédé de préparation d'aluminium de grande pureté
FR1409564A (fr) * 1963-08-30 1965-08-27 Sumitomo Chemical Co Procédé de fabrication des composés d'alcoylaluminium
FR1390445A (fr) * 1964-01-24 1965-02-26 Sumitomo Chemical Co Procédé pour la fabrication de l'aluminium

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US602976A (en) * 1898-04-26 Guillaume de chalmot
US2755178A (en) * 1952-07-30 1956-07-17 Robert T C Rasmussen Electric smelting process for production of silicon-aluminum alloys
US2757077A (en) * 1953-06-12 1956-07-31 Crucible Steel Co America Method of recovering metallic values from ores containing iron and nickel
US3155493A (en) * 1960-08-12 1964-11-03 Sumitomo Chemical Co Method for manufacturing high purity aluminum
US3112179A (en) * 1960-11-30 1963-11-26 Gen Aniline & Film Corp Preparation of iron and nickel carbonyls
US3535108A (en) * 1969-09-22 1970-10-20 Ethyl Corp Process for producing aluminum

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4303204A (en) * 1976-10-28 1981-12-01 Reynolds Metals Company Upgrading of bauxites, bauxitic clays, and aluminum mineral bearing clays
US6072821A (en) * 1997-06-03 2000-06-06 Kanthal Ab Method for heat treating materials at high temperatures, and a furnace bottom construction for high temperature furnaces
CN101775493B (zh) * 2010-01-08 2012-07-04 甘肃紫鑫矿业煤化工有限公司 用红柱石原矿为原料直接还原制备硅钡铝钙钛多元合金的方法
CN104513902A (zh) * 2013-09-30 2015-04-15 林州市林丰铝电有限责任公司 一种铝渣回收方法
CN103695656A (zh) * 2013-12-04 2014-04-02 台澳铝业（台山）有限公司 一种铝灰回收利用方法
CN111167831A (zh) * 2020-01-03 2020-05-19 武翠莲 一种催化分解含铝硅酸盐的方法
US11739395B1 (en) * 2022-05-05 2023-08-29 The United States Of America As Represented By The Secretary Of The Navy Embrittled aluminum alloys for powder manufacturing

Also Published As

Publication number Publication date
CH594737A5 (enrdf_load_stackoverflow) 1978-01-31
SE404032B (sv) 1978-09-18
GB1415475A (en) 1975-11-26
DE2337339A1 (de) 1974-02-14
NO136542C (no) 1977-09-21
AU5874373A (en) 1975-02-06
FR2194790A1 (enrdf_load_stackoverflow) 1974-03-01
DE2337339B2 (de) 1975-05-22
DE2337339C3 (de) 1976-01-08
CA985911A (en) 1976-03-23
FR2194790B1 (enrdf_load_stackoverflow) 1977-05-13
AU477098B2 (en) 1976-10-14
JPS4953514A (enrdf_load_stackoverflow) 1974-05-24
NO136542B (enrdf_load_stackoverflow) 1977-06-13

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