US3900312A - Reduction of aluminum chloride by manganese - Google Patents

Reduction of aluminum chloride by manganese Download PDF

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Publication number
US3900312A
US3900312A US297695A US29769572A US3900312A US 3900312 A US3900312 A US 3900312A US 297695 A US297695 A US 297695A US 29769572 A US29769572 A US 29769572A US 3900312 A US3900312 A US 3900312A
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United States
Prior art keywords
manganese
aluminum
chloride
elemental
liquid
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Expired - Lifetime
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US297695A
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English (en)
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John Christopher Terry
Alfred Lippman
Roger Frank Sebenik
Jr Harry Gordon Harris
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Toth Aluminum Corp
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Toth Aluminum Corp
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Publication date
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Priority to US297695A priority Critical patent/US3900312A/en
Priority to DE19732348450 priority patent/DE2348450A1/de
Priority to IT29602/73A priority patent/IT995540B/it
Priority to ZA737706A priority patent/ZA737706B/xx
Priority to AT849873A priority patent/ATA849873A/de
Priority to AU61004/73A priority patent/AU482513B2/en
Priority to IS2178A priority patent/IS948B6/is
Priority to BE136454A priority patent/BE805797A/xx
Priority to NO3948/73A priority patent/NO134304C/no
Priority to OA55037A priority patent/OA04493A/xx
Priority to IL43428A priority patent/IL43428A/en
Priority to NL7314252A priority patent/NL7314252A/xx
Priority to JP48116256A priority patent/JPS4974109A/ja
Priority to RO7376351A priority patent/RO67591A/ro
Priority to GB4812073A priority patent/GB1419450A/en
Priority to HUAI229A priority patent/HU167894B/hu
Priority to ES419700A priority patent/ES419700A1/es
Priority to FR7336935A priority patent/FR2202946B1/fr
Priority to BR8093/73A priority patent/BR7308093D0/pt
Priority to DD174088A priority patent/DD108324A5/xx
Priority to AR250546A priority patent/AR201746A1/es
Application granted granted Critical
Publication of US3900312A publication Critical patent/US3900312A/en
Anticipated expiration legal-status Critical
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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
    • C22B34/00—Obtaining refractory metals
    • C22B34/10—Obtaining titanium, zirconium or hafnium
    • C22B34/12—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08
    • C22B34/1263—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining metallic titanium from titanium compounds, e.g. by reduction
    • C22B34/1277—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining metallic titanium from titanium compounds, e.g. by reduction using other metals, e.g. Al, Si, Mn
    • 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
    • C22B21/0038—Obtaining aluminium by other processes
    • C22B21/0053—Obtaining aluminium by other processes from other aluminium compounds
    • C22B21/0061—Obtaining aluminium by other processes from other aluminium compounds using metals, e.g. Hg or Mn
    • 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
    • C22B34/00—Obtaining refractory metals
    • C22B34/10—Obtaining titanium, zirconium or hafnium
    • C22B34/12—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08
    • C22B34/1263—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining metallic titanium from titanium compounds, e.g. by reduction
    • C22B34/1268—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining metallic titanium from titanium compounds, e.g. by reduction using alkali or alkaline-earth metals or amalgams
    • C22B34/1272—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining metallic titanium from titanium compounds, e.g. by reduction using alkali or alkaline-earth metals or amalgams reduction of titanium halides, e.g. Kroll process
    • 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
    • C22B5/00—General methods of reducing to metals
    • C22B5/02—Dry methods smelting of sulfides or formation of mattes
    • C22B5/04—Dry methods smelting of sulfides or formation of mattes by aluminium, other metals or silicon
    • 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
    • C22B5/00—General methods of reducing to metals
    • C22B5/02—Dry methods smelting of sulfides or formation of mattes
    • C22B5/06—Dry methods smelting of sulfides or formation of mattes by carbides or the like

Definitions

  • the manganese reduces the liquid aluminum chloride and forms essen- [56] References Cited tially elemental aluminum and manganese chloride.
  • the temperature range is between 180600C and the pressure range is 15-450 psia.
  • the primary object of the present invention is to produce a metal by direct reduction of a chloride of that metal by a reductant metal which is in the solid state during the reaction.
  • a still further important object of the present invention is to produce silicon by reducing SiCl in either liquid or gaseous state by manganese or aluminum in solid state.
  • FIG. I shows in diagrammatic form an apparatus for carrying out the invention when the metal chloride is gaseous
  • FIG. 2 shows in diagrammatic form an apparatus for carrying out the invention in a batch process when the metal chloride is liquid
  • FIG. 3 shows in diagrammatic form a further appara tus for carrying out the invention in a batch process when the metal chloride is liquid;
  • FIG. 4 shows in diagrammatic form an apparatus for carrying out the invention in a continuous process when the metal chloride is liquid.
  • the instant invention has extremely broad applicability.
  • the scope of the invention deals with reacting a fluid metal chloride with a solid reductant powder.
  • the most important criteria is that the reductant metal powder is in solid form and the metal chloride be in fluid form at the temperature and pressure that the process is carried out at.
  • Table I shows the various melting points (M.P.) and boiling points (B.P.),of various metals and their chlorides as well as their free energies at 298K', 500K and 700K. From this Table, one skilled in the artcan dey duct the operating parameters for carrying out the instant inventive process.
  • any I i TABLE I Properties of Metals and Metal Chlorides I Metal AF,, Kcal/gmolc Metal M.P..K B.P..K Chloride M.P..K B.P..l ⁇ ' 298K 5()(lK 7()()K Aluminum(Al) 931.7 260( AICL, 465.6 720 -l53.() l44.5 1 38.6 Beryllium (Be) 1556 3243 BeCl 678 (S20)- ('l()2.9) 96.6) Calcium (Ca) 1124 1760 CaCl.
  • FIG. 1 diagrammatically shows a low temperature gaseous AlCL, apparatus, a reactor 26 and AlCL, generator 22 are integrated in one horizontal inch alumina tube 19. Each section'ofthe tube 19 is separated by pyrex wool 28 and an 8-inch void space 24.
  • the AlCl generator section 22 contains a l inch long bed of aluminum pellets.
  • the reactor sec: tion 26 contains a /2-inch long bed of 5 grams of manganese.
  • the condenser 32 is a 2-inch diameter mild steel pipe 5 inches long which is connected to the ceramic tube with a packing 'gland30 and has a conduit 34 and valve 36 for vcnting' any gases.'The reactor and generator sections of the tube are heated separately with resistance wire 20.
  • Chlorine vapor from source l0 is passed d vija conduit 12 through a rotometer 14 to measure the flow rate which is controlled by valve 16 and is passed through conduit 18 into the aluminum pellets in generator 22 to generate AlCl at 300C.
  • the AICL then passes through the bed of Mn in reactor 26 which ranges in particlesize from 45 to 300 microns (all on 325 mesh).
  • the particle size of the Mn was chosen for a size distribution of high surface area'to ensure good gas-solid contact. Runs were typically made for 2 hours with 5 grams of Mn at 300 to 600C and an AlCl flow rate or 3 grams/hour with the following results:
  • the process could be carried out in conventional gassolid reactors and combinations thereof.
  • the MnCl could be removed from the aluminum product by vaporization as an MnCI -AICL, gas complex or by dissolving in liquid AICL, or another solvent.
  • the reaction could be stopped at any degree of Al production and the aluminum then produced separated from the Mn by means such as aluminum subhalide distillation, zinc extraction, zone freezing, or differential vaporization.
  • EXAMPLE 11' A simplified diagram of a low-temperature liquid AICL, laboratory apparatus is shown in FIG. 2.
  • a batch reactor 40 is designed to effectively contact Mn metal granules with liquid AICL, in a continuously agitated vessel.
  • the apparatus is designed to operate for various lengths of time at l80600C and 14.7-450 psia, with approximately 30-60 grams Mn and 120-450 grams AlCl charge.
  • the reactor 40 contains a 2 [2-inch diameter alumina tube 58 which is housed in a 3-inch diameter stainless steel pipe 60 and heated externally by resistance wires 62.
  • a stainless-steel stirrer 56 and shaft 54 along with a motor 50 is mounted in place on the top flange 46 with a packing gland 48.
  • the charge is introduced thro ugh conduit 44.
  • a pressure gauge 52 is mounted on conduit 42. Following the reaction period, the unreacted AICL, is boiled off through conduit 64, valve 66, into condenser 68 which is vented by conduit 70 and valve 72.
  • the liquid AlCl serves as a solvent to dissolve the solid MnCl that is formed at the reaction interface along with the aluminum, thus resulting in a A porous aluminum microstructure, through which liquid AlCl gains ready access to the unreacted manganese within.
  • porosity namely, the volume of the MnCl and aluminum products would greatly exceed that of the substrate dense manganese so that a tendency would exist for the film of solid reaction products or of the porous aluminum to expand away from the manganese and to thereby add to the porosity.
  • reaction lies in the increase in boiling point of the AlCl MnCl liquor as the reaction proceeds due to increased concentration of MnCl- This permits use of beneficial higher temperatures for the reaction up to 600C instead of being limited by about 352.5C, the critical temperature of pure AlCl This increased temperature factor thus can be used to readily compensate for any decreasing AlCl concentration due to increase of MnClcontent as the reaction progresses. Additional MnCl or other soluble metal salts, could be added as needed to establish optimum conditions.
  • An advantage of the liquid AICL, process lies in the ease of separation of the products formed.
  • the density decreases from about 7.4g/ml for Mn to 2.7g/ml for A1.
  • the finished product can be readily separated by utilization of the vast difference in density.
  • the product could be carried out of a continuous reactor in the liquor stream at appropriate velocity leaving Mn-containing particles behind; or conventional gravity separation devices could be employed, with recycling of the Mn-contaiining particles.
  • all the manganese could be replaced with aluminum in the reactor or series of reactors to obviate the need for separation :of the aluminum from an intermediate.
  • the product aluminum can be cleansed of adherent MnCl by a wash of fresh liquid AlCl in which the MnCl is soluble in AlCl to 50% by weight MnCl the two salts can be readily separated by crystallization, sublimation or by evaporation of the AICI Water or organic solvents can also be used to remove any resid ual MnCl or AlCl
  • the AlCl which is left on the surface of the aluminum can be removed readily by sublimation or evaporation.
  • the MnCl can be removed from AICL, liquor by evaporating the latter with its 180C atmospheric boiling point versus 1190C for the boiling point of MnCl. or the MnCl can be crystallized out of a hot concentrated solution of MnCl and AlCl by reducing the temperature.
  • the AICIa, after removal of the MnCl can be reused.
  • An unexpected advantage of the reaction with liquid AICI is the formation of the aluminum over the surface of the manganese metal in a manner that does not block reaction. This affords the opportunity of cutting short the reaction at any desired time and still being temperature of the aluminum metal canbe brought slightly over its melting point to cause the aluminum to flow from the particles and be collected. leaving the residue of manganese metal with a slight film of high melting point manganesealuminum alloy at theinterface. The manganese. residue is returned to the reactor or if the particle size is very small, it can be agglomerated first.
  • Agitation of an abrasive or impact nature can cause the aluminum coating to separate for collection. Furthermore, more unreacted manganese will be exposed.
  • the aluminum can be separated from the manganese by conventional methods such as subhalide or zine extraction.
  • This particular aspect of the invention may be practiced in many forms. Firstly, it is amenable to many conventional solid-liquid contactors, reactors and flow arrangements such as fluid, static and moving bed reactors, batch reactors, and cyclone and tube transport reactors, all in concurrent, countercurrent, semicontinuous or batch arrangements. Agitation may be performed by stirrers, flow or recirculation of slurry, vibrators, shakers, or the recycling of an inert gas or liquid AlCl rotating or tumbling drums with or without flights, grinding balls, or other obvious means.
  • FIG. 3 is a schematic diagram illustrating an apparatus for performing the process of the present invention in a batch-wise manner.
  • the process uses a noncorrosive metal or ceramic lined steel reactor 80 having heating means such as electric heating coils 82 for control of the temperature necessary to maintain the AlCl in a liquid state and provide other heat demands.
  • the reactor is charged with AICL, and manganese from the top through charge and discharge port 84. Generally, an excess of AlCl will be present to keep the reactants in the form of a solid-liquid slurry.
  • the reactor is sealed and heated to reaction temperature.
  • the AICL At temperature (l80-600C), the AICL, is liquid and exhibits a vapor pressure of l-45O psia depending on the exact reactor temperature and composition of the liquor.
  • the mixture of reactants is maintained at temperature and pressure until all of the manganese has been consumed to form aluminum metal and MnCl
  • the mixture is meehanically. stirred by a blade 88 attached to a shaft 86, powered by a motor (not shown) to enhance contact and reduce reaction time.
  • any excess AlCl is removed by opening the reactor and bleeding off the AlCl;, as a gas through conduit 90 and valve 92. Removal can be enhanced by pulling a vacuum on the reactor and/or by increasing the temperature.
  • the aluminum and MnClare discharged as solids and subsequently separated by means such as melting, vaporization, or solvent extraction.
  • EXAMPLE IV An apparatus for performing the process of the present invention in a continuous manner is illustrated in FIG. 4.
  • the process uses a corrosion-resistant or ceramic-lined steel counter-current reaction tower 100 having heating means 102 for maintaining the AlCl;,- MnCl solution in the liquid state at from l80-600C 8 and 15-450 psia.
  • Granular solid manganese is continuously introduced from the top at input port 104 and AICL, is continuously introduced from the bottom at input port 106 in the countercurrent reactor.
  • the solid aluminum product is continuously removed from the bottom at I10 andthc MnCl from the top at 108 and- /or bottom at 1 10, depending on the extent to which it dissolves in the AICI TiCL, AND MAGNESIUM Liquid TiCL, can be reduced by solid powdered magnesium.
  • powdered magnesium and TiCl 4 can be simultaneously charged into a reactor as above discussed, heated to 200-650C at a pressure from 0-676 psia and reacted to give titanium metal comixed, adhering to, or alloyed with unreacted magnesium, if any, and MgCl Under these conditions, magnesium is solid, titanium is solid, MgCl in pure form is solid, and TiCl is liquid if the total pressure is above the vapor pressure of TiCl (critical temperatures 365C).
  • thermodynamics of this reaction is favorable. For example, at 500K the thermodynamics show the reduction reaction to be quite favorable:
  • TiCl AND MANGANESE Liquid or gaseous TiCl can be reduced by solid powdered manganese in accordance with:
  • the tem perature range over which the reaction is favorable is from -30C (the melting point of TiCl to about l600C realizing that above about 1 175C some of the manganese will be in liquid phase due to a Ti-Mn eutectic of that melting point.
  • the preferred pressure range is from 0-676 psia.
  • the critical point of TiCl is 365C and 46 atmospheres; however, at high termperatures, vapor pressure lowering .d'ue to the presence of otheririert metal salts such as NaCl, CaCl- KCL, MgCL. 350,, etc. allows TiCl, to remain in the liquid state.
  • the reaction proceeds favorably with TiCl in the gaseous state. Typical experimental results are shown in EXAMPLE V.
  • Liquid or gaseous SiCl can be reduced by solid powdered manganese in accordance with:
  • the temperature range over which the reaction is favorable is from C (the melting point of SiCl to about 1600C realizing that above about l040C some of the manganese will be in liquid phase due to a Si-Mn eutectic of that melting point.
  • the critical point of SiCl is 234C and 37 atmospheres. Above the critical temperature the SiCl, will bea vapor unless a suitable inert metal salt such as NaCl, CaCl KC], MgCl- BaCl etc, allows SiCl to remain in the liquid state. In addition, the reaction proceeds favorably in the gaseous state.
  • SiCl AND ALUMINUM Liquid or gaseous SiCl can also be reduced by solid powdered aluminum in accordance with:
  • the temperature range over which the reaction is favorable is from 70C (the melting point of SiCl to about 577C realizing that above about 577C the aluminum will be in the liquid phase due to a Si-Al eutectic of that melting point.
  • Above 234C the critical temperature of SiCl SiCl, will be a vapor unless a suitable inert metallic salt such as NaCl, CaCl KCl, MgCl BaCl etc. allows the SiCl to remain in the liquid state.
  • EXAMPLE V The following typical experimental results obtained from the apparatus shown in FIG. 2 demonstrate the production of Ti and Si metals from their respective chlorides.
  • the reactor was charged with 60 grams of -100, +200 mesh electrolytic manganese and 410 grams of reagent grade TiCl The reactor was heated to 336C for 3 hours while agitating with a paddle shaped stirrer at 300 rpm under a TiCl vapor pressure of 425-443 psig. After 3 hours the TiCl was bled from the reactor into a condenser. The hot reactor was then purged with argon and cooled to room temperature. The solid residue in the reactor was removed and analyzed for titanium metal. A total of 3.18 grams of titanium metal was found.
  • the reactor was charged with 60 grams of -l00, +200 mesh aluminum powder and 695 grams of reagent grade SiCl The reactor was heated to 200C for 3 hours while agitating at 1200 rpm with a turbine shaped stirrer under a SiCl vapor pressure of 388 psia. After 3 hours the SiCl was bled from the reactor into a condenser. The reactor was cooled to room temperature at which time the solid residue was removed and analyzed for silicon metal. A total of 2.13 grams of silicon metal was found.
  • the free energies of reaction using manganese as the reductant are A 50" 29.25Kcal and A G 30. IOKcal per mole of Ti formed as calculated from the following stoichiometric reaction:
  • AICL can be continuously removed by throttling TiCl into and out of the system carrying AlCL, with 10 it.
  • the MnCl zproduced by reaction of TiCl with Mn cannot be removed so easily on a continuous basis.
  • inert metallic salts of low volatility, especially metal halides are beneficial in carrying out the reactions above described.
  • the inert metallic salts are used to lower the vapor pressure of the metal chloride, e.g. AICL TiCh, SiCl so that a higher temperature can be reached in the closed reactor at a given pressure.
  • a process for producing aluminum in essentially elemental form comprising the steps of providing aluminum chloride, which chloride is in a liquid phase; providing elemental manganese in solid phase; reacting said liquid aluminum chloride and elemental manganese in a vessel at a pressure and at a temperature up to 350C at which they will maintain their respective phases, the elemental manganese reducing the liquid aluminum chloride and forming essentially elemental aluminum and manganese chloride.
  • reaction is carried out in a temperature range between l350C and pressure range of from 14-450 psia.
  • a process for producing aluminum in essentially elemental form comprising the steps of a. providing aluminum chloride in a liquid phase;

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US297695A 1972-10-16 1972-10-16 Reduction of aluminum chloride by manganese Expired - Lifetime US3900312A (en)

Priority Applications (21)

Application Number Priority Date Filing Date Title
US297695A US3900312A (en) 1972-10-16 1972-10-16 Reduction of aluminum chloride by manganese
DE19732348450 DE2348450A1 (de) 1972-10-16 1973-09-26 Verfahren zur gewinnung eines metalls
IT29602/73A IT995540B (it) 1972-10-16 1973-10-01 Riduzione di cloruro metallico con metallo in polvere
ZA737706A ZA737706B (en) 1972-10-16 1973-10-02 Reduction of metallic chloride by powered metal
AT849873A ATA849873A (de) 1972-10-16 1973-10-04 Verfahren zum gewinnen von aluminium
AU61004/73A AU482513B2 (en) 1972-10-16 1973-10-04 Reduction of metallic chloride by solid metal
IS2178A IS948B6 (is) 1972-10-16 1973-10-05 Breyting á málmkenndu klóri með duftkenndum málmi
BE136454A BE805797A (fr) 1972-10-16 1973-10-08 Reduction de chlorures metalliques par un metal en poudre
NO3948/73A NO134304C (ja) 1972-10-16 1973-10-11
OA55037A OA04493A (fr) 1972-10-16 1973-10-13 Réduction de chlorures métalliques par un métal en poudre.
IL43428A IL43428A (en) 1972-10-16 1973-10-15 Reduction of metallic chloride by powdered metal
FR7336935A FR2202946B1 (ja) 1972-10-16 1973-10-16
RO7376351A RO67591A (ro) 1972-10-16 1973-10-16 Procedeu de obtinere a aluminiului
GB4812073A GB1419450A (en) 1972-10-16 1973-10-16 Production of aluminium from aluminium chloride
HUAI229A HU167894B (ja) 1972-10-16 1973-10-16
ES419700A ES419700A1 (es) 1972-10-16 1973-10-16 Procedimiento para la produccion de un metal.
NL7314252A NL7314252A (ja) 1972-10-16 1973-10-16
BR8093/73A BR7308093D0 (pt) 1972-10-16 1973-10-16 Processo de reducao de cloreto metalico por metal em po
JP48116256A JPS4974109A (ja) 1972-10-16 1973-10-16
AR250546A AR201746A1 (es) 1972-10-16 1973-10-16 Procedimiento para la produccion de un metal elemental
DD174088A DD108324A5 (ja) 1972-10-16 1973-10-16

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US297695A US3900312A (en) 1972-10-16 1972-10-16 Reduction of aluminum chloride by manganese

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US (1) US3900312A (ja)
JP (1) JPS4974109A (ja)
AR (1) AR201746A1 (ja)
AT (1) ATA849873A (ja)
BE (1) BE805797A (ja)
BR (1) BR7308093D0 (ja)
DD (1) DD108324A5 (ja)
DE (1) DE2348450A1 (ja)
ES (1) ES419700A1 (ja)
FR (1) FR2202946B1 (ja)
GB (1) GB1419450A (ja)
HU (1) HU167894B (ja)
IL (1) IL43428A (ja)
IS (1) IS948B6 (ja)
IT (1) IT995540B (ja)
NL (1) NL7314252A (ja)
NO (1) NO134304C (ja)
OA (1) OA04493A (ja)
RO (1) RO67591A (ja)
ZA (1) ZA737706B (ja)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4035180A (en) * 1976-03-16 1977-07-12 Toth Aluminum Corporation Catalytic process for the reduction of aluminum chloride by manganese
US4106928A (en) * 1976-03-15 1978-08-15 Westinghouse Electric Corp. Chlorination process for producing aluminum
US6284316B1 (en) * 1998-02-25 2001-09-04 Micron Technology, Inc. Chemical vapor deposition of titanium
US6433434B1 (en) 1998-02-25 2002-08-13 Micron Technology, Inc. Apparatus having a titanium alloy layer
US20040123700A1 (en) * 2002-12-26 2004-07-01 Ling Zhou Process for the production of elemental material and alloys
US20060183958A1 (en) * 2003-04-01 2006-08-17 Breneman William C Process for the treatment of waste metal chlorides
US20060191372A1 (en) * 2003-07-04 2006-08-31 Jawad Haidar Method and apparatus for the production of metal compounds
EP1999285A1 (en) * 2006-03-27 2008-12-10 Commonwealth Scientific and Industrial Research Organisation Apparatus and methods for the production of metal compounds
US20110091350A1 (en) * 2008-04-21 2011-04-21 Jawad Haidar Method and apparatus for forming titanium-aluminium based alloys
US8834601B2 (en) 2009-12-18 2014-09-16 Commonwealth Scientific And Industrial Research Organisation Method for producing low aluminium titanium-aluminium alloys

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6067603A (ja) * 1983-09-21 1985-04-18 Toho Aen Kk 金属超微粉の処理方法

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US2452665A (en) * 1944-03-31 1948-11-02 Electro Metallurgical Co Process for the separation of metals
US2847205A (en) * 1954-10-13 1958-08-12 Nat Res Corp Production of metals
US3161500A (en) * 1961-08-04 1964-12-15 Aluminium Lab Ltd Protection of graphite surfaces from attack by aluminum monohalide
US3455678A (en) * 1967-01-16 1969-07-15 Ethyl Corp Process for the concurrent production of aif3 and a metallic titanium product

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2452665A (en) * 1944-03-31 1948-11-02 Electro Metallurgical Co Process for the separation of metals
US2847205A (en) * 1954-10-13 1958-08-12 Nat Res Corp Production of metals
US3161500A (en) * 1961-08-04 1964-12-15 Aluminium Lab Ltd Protection of graphite surfaces from attack by aluminum monohalide
US3455678A (en) * 1967-01-16 1969-07-15 Ethyl Corp Process for the concurrent production of aif3 and a metallic titanium product

Cited By (27)

* Cited by examiner, † Cited by third party
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US4106928A (en) * 1976-03-15 1978-08-15 Westinghouse Electric Corp. Chlorination process for producing aluminum
US4035180A (en) * 1976-03-16 1977-07-12 Toth Aluminum Corporation Catalytic process for the reduction of aluminum chloride by manganese
US7443032B2 (en) 1998-02-25 2008-10-28 Micron Technology, Inc. Memory device with chemical vapor deposition of titanium for titanium silicide contacts
US6284316B1 (en) * 1998-02-25 2001-09-04 Micron Technology, Inc. Chemical vapor deposition of titanium
US6433434B1 (en) 1998-02-25 2002-08-13 Micron Technology, Inc. Apparatus having a titanium alloy layer
US8456007B2 (en) 1998-02-25 2013-06-04 Round Rock Research, Llc Chemical vapor deposition of titanium
US6830820B2 (en) 1998-02-25 2004-12-14 Micron Technology, Inc. Chemical vapor deposition of titanium
US6830838B2 (en) 1998-02-25 2004-12-14 Micron Technology, Inc. Chemical vapor deposition of titanium
US6903462B2 (en) 1998-02-25 2005-06-07 Micron Technology, Inc. Chemical vapor deposition of titanium
US6940172B2 (en) 1998-02-25 2005-09-06 Micron Technology, Inc. Chemical vapor deposition of titanium
US20090039517A1 (en) * 1998-02-25 2009-02-12 Micron Technology, Inc. Chemical vapor deposition of titanium
US20050255698A1 (en) * 1998-02-25 2005-11-17 Micron Technology, Inc. Chemical vapor deposition of titanim
AU2003293544B2 (en) * 2002-12-26 2010-03-11 Millenium Inorganic Chemicals, Inc. Process for the production of elemental material and alloys
WO2004060594A1 (en) * 2002-12-26 2004-07-22 Millenium Inorganic Chemicals, Inc. Process for the production of elemental material and alloys
US20040123700A1 (en) * 2002-12-26 2004-07-01 Ling Zhou Process for the production of elemental material and alloys
US6955703B2 (en) * 2002-12-26 2005-10-18 Millennium Inorganic Chemicals, Inc. Process for the production of elemental material and alloys
US20060183958A1 (en) * 2003-04-01 2006-08-17 Breneman William C Process for the treatment of waste metal chlorides
US8562712B2 (en) 2003-07-04 2013-10-22 Commonwealth Sci. and Ind. Res. Org. Method and apparatus for the production of metal compounds
US20060191372A1 (en) * 2003-07-04 2006-08-31 Jawad Haidar Method and apparatus for the production of metal compounds
US20090165597A1 (en) * 2006-03-27 2009-07-02 Commonwealth Scientific And Industrial Research Or Apparatus and Methods for the Production of Metal Compounds
EP1999285A4 (en) * 2006-03-27 2010-05-12 Commw Scient Ind Res Org APPARATUS AND METHODS FOR PRODUCING METAL COMPOUNDS
EP1999285A1 (en) * 2006-03-27 2008-12-10 Commonwealth Scientific and Industrial Research Organisation Apparatus and methods for the production of metal compounds
US8821612B2 (en) 2006-03-27 2014-09-02 Commonwealth Scientific And Industrial Research Organisation Apparatus and methods for the production of metal compounds
US20110091350A1 (en) * 2008-04-21 2011-04-21 Jawad Haidar Method and apparatus for forming titanium-aluminium based alloys
US8632724B2 (en) * 2008-04-21 2014-01-21 Commonwealth Sci. and Ind. Res. Org. Method and apparatus for forming titanium-aluminium based alloys
US9080224B2 (en) 2008-04-21 2015-07-14 Commonwealth Science And Industrial Research Organization Method and apparatus for forming titanium-aluminium based alloys
US8834601B2 (en) 2009-12-18 2014-09-16 Commonwealth Scientific And Industrial Research Organisation Method for producing low aluminium titanium-aluminium alloys

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RO67591A (ro) 1981-08-17
FR2202946A1 (ja) 1974-05-10
DD108324A5 (ja) 1974-09-12
BR7308093D0 (pt) 1974-07-11
NO134304C (ja) 1976-09-15
BE805797A (fr) 1974-04-08
ATA849873A (de) 1976-11-15
AU6100473A (en) 1975-04-10
IL43428A (en) 1976-05-31
NO134304B (ja) 1976-06-08
DE2348450A1 (de) 1974-04-25
IS2178A7 (is) 1973-11-02
ZA737706B (en) 1974-08-28
ES419700A1 (es) 1976-04-16
FR2202946B1 (ja) 1977-09-09
IT995540B (it) 1975-11-20
IS948B6 (is) 1976-08-09
HU167894B (ja) 1976-01-28
IL43428A0 (en) 1974-01-14
GB1419450A (en) 1975-12-31
JPS4974109A (ja) 1974-07-17
NL7314252A (ja) 1974-04-18
AR201746A1 (es) 1975-04-15
OA04493A (fr) 1980-03-30

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