EP1811062A1 - Procédé de fabrication de métal et dispositif de fabrication par électrolyse du sel fondu - Google Patents

Procédé de fabrication de métal et dispositif de fabrication par électrolyse du sel fondu Download PDF

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Publication number
EP1811062A1
EP1811062A1 EP05790573A EP05790573A EP1811062A1 EP 1811062 A1 EP1811062 A1 EP 1811062A1 EP 05790573 A EP05790573 A EP 05790573A EP 05790573 A EP05790573 A EP 05790573A EP 1811062 A1 EP1811062 A1 EP 1811062A1
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EP
European Patent Office
Prior art keywords
metal
molten
cathode
salt
production
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP05790573A
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German (de)
English (en)
Other versions
EP1811062A4 (fr
Inventor
Masanori c/o TOHO TITANIUM CO. LTD. YAMAGUCHI
Yuichi c/o TOHO TITANIUM CO. LTD. ONO
Susumu c/o TOHO TITANIUM CO. LTD. KOSEMURA
Eiji c/o TOHO TITANIUM CO. LTD. NISHIMURA
Tadashi c/o Sumitomo Titanium Corp. OGASAWARA
Makoto c/o Sumitomo Titanium Corp. YAMAGUCHI
Masahiko c/o Sumitomo Titanium Corp. HORI
Toru c/o Sumitomo Titanium Corp. UENISHI
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Osaka Titanium Technologies Co Ltd
Toho Titanium Co Ltd
Original Assignee
Osaka Titanium Technologies Co Ltd
Toho Titanium Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Osaka Titanium Technologies Co Ltd, Toho Titanium Co Ltd filed Critical Osaka Titanium Technologies Co Ltd
Publication of EP1811062A1 publication Critical patent/EP1811062A1/fr
Publication of EP1811062A4 publication Critical patent/EP1811062A4/fr
Withdrawn legal-status Critical Current

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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
    • C22B34/129—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 by dissociation, e.g. thermic dissociation of titanium tetraiodide, or by electrolysis or with the use of an electric arc
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C3/00—Electrolytic production, recovery or refining of metals by electrolysis of melts
    • C25C3/02—Electrolytic production, recovery or refining of metals by electrolysis of melts of alkali or alkaline earth metals
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C3/00—Electrolytic production, recovery or refining of metals by electrolysis of melts
    • C25C3/26—Electrolytic production, recovery or refining of metals by electrolysis of melts of titanium, zirconium, hafnium, tantalum or vanadium
    • C25C3/28—Electrolytic production, recovery or refining of metals by electrolysis of melts of titanium, zirconium, hafnium, tantalum or vanadium of titanium
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
    • C25C7/02—Electrodes; Connections thereof
    • C25C7/025—Electrodes; Connections thereof used in cells for the electrolysis of melts

Definitions

  • the present invention relates to the production of metal from a chloride thereof, and in particular, relates to a method for producing calcium metal by molten-salt electrolysis and to a method for producing metal, including a method for producing titanium metal, by using the calcium metal, and relates to an apparatus therefor.
  • titanium metal which is a simple substance
  • Kroll method in which titanium tetrachloride is reduced by molten magnesium to obtain sponge titanium
  • various kinds of improvements have been made to reduce the cost of production.
  • the Kroll method is a batch process in which a set of operations is repeated noncontinuously, there is a limitation to its efficiency.
  • a method in which titanium oxide is reduced by calcium metal in molten salt to obtain titanium metal directly see WO99/064638 and Japanese Unexamined Patent Application Publication No.
  • the calcium metal generated in the molten-salt electrolysis has a tendency to reverse react with chlorine gas generated in the electrolysis reaction to again form calcium chloride.
  • production efficiency is deteriorated.
  • the present invention has been completed in view of the above circumstances, and an object of the present invention is to provide a method for production of metal by molten-salt electrolysis, in which metal calcium used for reducing, such as an oxide or chloride of titanium metal, is produced, and in which titanium metal can be obtained by using this metal calcium efficiently at low cost.
  • the method for production of metal by molten-salt electrolysis of the present invention is a method for production of metal by molten-salt electrolysis which is performed by filling molten salt of calcium chloride in an electrolysis vessel having a anode and a cathode, one electrode (the anode or cathode) is arranged surrounding the other electrode, the cathode has at least one hole communicating the inner area surrounded by the cathode with the outer area, and the molten salt flows through the communicating holes from one area including the anode (the inner area or outer area) to the other area.
  • the present invention since one electrode of the positive or cathode is surrounding the other electrode and the molten salt flows from the area including the anode to the other area through the communicating holes arranged on the cathode, the calcium metal generated on the surface of the cathode during the molten salt electrolysis always flows to the area not including the anode, and the calcium metal is precipitated and accumulated at the electrolysis bath surface of the area. Therefore, the back reaction with chlorine gas generated on the surface of anode can be avoided, and calcium metal can be produced at high efficiency.
  • the apparatus for production of metal by molten-salt electrolysis is an apparatus for production of metal by molten-salt electrolysis having a anode and a cathode in a electrolysis vessel, one electrode of the cathode or anode being arranged surrounding the other electrode, the cathode having at least one hole communicating an inner area surrounded by the cathode with an outer area, molten salt of calcium chloride being supplied to the area including the anode, the molten salt of calcium chloride flowing to the other area through the communicating hole, and the molten salt of calcium chloride containing calcium metal generated at the cathode is extracted from the other area.
  • a titanium tetrachloride supplying pipe is arranged in the inner area in which calcium metal is generated by molten-salt electrolysis, and titanium tetrachloride in the gas phase is supplied through the titanium tetrachloride supplying pipe to generate titanium metal.
  • titanium tetrachloride is supplied to the calcium metal generated in the inner area by molten-salt electrolysis, they are reacted with each other to generate titanium metal. Therefore, it is not necessary that calcium metal be once recovered and be sent to a titanium producing process, and titanium metal can be obtained in the production process of calcium metal.
  • the back reaction of calcium metal and chlorine gas generated during the molten-salt electrolysis of calcium chloride can be reduced, and calcium metal can be efficiently produce at low cost. Furthermore, by directly supplying titanium tetrachloride, titanium metal can also be obtained.
  • FIG. 1 shows a conceptual cross sectional diagram of the first embodiment of the present invention.
  • Reference numeral 1 is an electrolysis vessel, and an electrolysis bath 2 consisting of calcium chloride (melting point 780°C) is filled in the vessel.
  • the electrolysis bath 2 is heated to a temperature above the melting point of calcium chloride by a heater (not shown) to be maintained in a molten state.
  • Reference numeral 3 indicates a anode.
  • Reference numeral 4 indicates a cylindrical cathode, which is arranged surrounding the anode 3.
  • Plural communicating holes are formed at a lower part of the cathode 4, and the molten salt can be moved between the inner area and the outer area of the cathode. Since the communicating holes are formed at the lower part of the cathode, the upper part of the cathode can function as a division wall.
  • a bath supplying pipe 6 is arranged at an inner part of the cathode 4, and calcium chloride which is a raw material of the molten-salt electrolysis is continuously supplied therethrough.
  • An extracting pipe 7 is arranged at an upper and outer part of the cathode 4 to extract calcium metal.
  • the molten calcium metal which is moved to the outside of the cathode 4 and floats up, and the calcium chloride in which calcium metal is precipitated, are continuously extracted by the extracting pipe 7.
  • the molten calcium metal and the calcium chloride having precipitated calcium metal are both extracted and can be used in a reduction reaction of titanium oxide or titanium chloride using molten salt, for example.
  • chlorine gas is generated at the surface of the anode 3 and is emitted out of the system.
  • the chlorine gas can be used in a chlorination reaction of titanium ore or the like.
  • Fig. 2 shows a conceptual cross sectional diagram of the second embodiment of the present invention.
  • Reference numeral 1 is an electrolysis vessel, and an electrolysis bath 2 consisting of calcium chloride (melting point 780°C) is filled in the vessel.
  • the electrolysis bath 2 is heated to a temperature above the melting point of calcium chloride by a heater, which is not shown, so as to be maintained in a molten state.
  • Reference numeral 3 indicates a anode which is unified with the electrolysis vessel.
  • Reference numeral 4 is a cylindrical cathode, and it is immersed at the central part of the electrolysis vessel 1.
  • Plural communicating holes are formed at a lower part of the cathode 4, and the molten salt can be moved between the outer area and the inner area of the cathode. Since the communicating holes are formed at the lower part of the cathode, an upper part of the cathode can function as a division wall.
  • a bath supplying pipe 6 is arranged at an outer part of the cathode 4, and calcium chloride which is a raw material of the molten-salt electrolysis is continuously supplied therethrough.
  • An extracting pipe 7 is arranged at an upper and inner part of the cathode 4 to extract calcium metal.
  • the molten calcium metal which is moved to the inside of the cathode 4 and floats up, and the calcium chloride in which calcium metal is precipitated, are continuously extracted by the extracting pipe 7.
  • the molten calcium metal and the calcium chloride having precipitated calcium metal are both extracted and can be used in a reduction reaction of titanium oxide or titanium chloride using molten salt, for example.
  • chlorine gas is generated at the surface of the anode 3 and is emitted out of the system.
  • the chlorine gas can be used in a chlorination reaction of titanium ore or the like.
  • Fig. 3 shows a conceptual cross sectional diagram of the third favorable embodiment of the present invention. Explanations of reference numerals 1 to 8 are omitted since they are similar to those for Fig. 2.
  • inert gas is injected from the bottom part of the inner area of the cathode 4 through an inert gas supplying pipe 9.
  • a gas-lift effect occurs by the injection of the inert gas, and upward flow occurs in the inner area of the cathode 4.
  • Accompanied by this effect a flow from the outer area to the inner area occurs.
  • calcium metal generated on the surface of the cathode 4 can be moved into the inside the cathode in a short time, and a loss by the back reaction with chlorine gas which is generated in the outer area of the cathode can be reduced.
  • Fig. 4 shows a conceptual cross sectional diagram of the fourth favorable embodiment of the present invention. Arrangement of reference numerals 1 to 8 is omitted since they are similar to those in Fig. 2. Differing from the above-mentioned embodiments, an oblique communicating hole inclining in a vertical direction is formed at a side wall of the cathode 4, as shown in Fig. 4. In addition, as shown in Fig. 9, which is a conceptual cross sectional diagram in which the cathode 4 is seen from above, the communicating holes are inclined uniformly from the normal line direction of the cylindrical electrode also in the horizontal direction. Furthermore, the cathode 4 is arranged so as to be rotatable.
  • the molten salt By rotating such a cathode 4, the molten salt can be forcibly moved from the outer area of the cathode 4 to the inner area.
  • calcium metal generated on the outer surface of the cathode 4 can be moved into the inner area of the cathode in a short time, and a loss by the back reaction with chlorine gas which is generated in the outer area of the cathode can be reduced.
  • Fig. 5 shows a conceptual cross sectional diagram of the fifth favorable embodiment of the present invention. Explanation of reference numerals 1 to 8 is omitted since they are similar to those in Fig. 2. Differing from the above-mentioned embodiments, an agitating fin 10 is arranged at the bottom part of the inner area of the cathode 4. The agitating fin can be rotated via a driving axis to form a flow of molten salt from the bottom to the upper surface. As a result, calcium m 4 can be moved to the inner area of the cathode in a short time, and a loss by the back reaction with chlorine gas which is generated in the outer area of the cathode can be reduced.
  • the present invention since calcium metal is continuously pushed out of the system soon after its generation, the back reaction with chlorine gas can be prevented, and the calcium metal can be efficiently produced.
  • the structure of the apparatus can be favorably simplified.
  • the back reaction of calcium metal and chlorine gas can be efficiently reduced.
  • the material of the negative electrode is not limited in particular as long as the material has conductivity.
  • carbon steel, stainless steel, or material such as copper or the like can be used. From the viewpoint of processing the negative electrode to have a cylindrical shape and forming communicating holes, carbon steel having easy workability is desirable.
  • the electrolysis bath consisting of calcium chloride is required to be maintained at a temperature which is not lower than the melting point of calcium metal (845°C). If the temperature is lower than the melting point of the calcium metal, calcium metal is generated in a solid state at the inner part of the cathode and blocks up the communicating holes, and this interferes with the flow-through of molten salt and calcium metal. On the other hand, if the temperature is much greater than the melting point of calcium metal, evaporation of the electrolysis bath is promoted and solubility of calcium metal in calcium chloride is increased. This is undesirable from the viewpoint of the yield. A range not exceeding 100°C above the melting point of calcium metal is desirable.
  • the temperature of the electrolysis bath can be controlled by using a heating burner immersed in the electrolysis bath. Furthermore, if the burner has a cooling function, this is desirable because the temperature can be freely controlled in a target range. In addition, temperature control can be performed by another means of selection.
  • another salt can be added to calcium chloride.
  • the melting point of the electrolysis bath can be lowered by adding potassium chloride.
  • Potassium chloride added to calcium chloride is desirably in a range from 20 to 80 mass%. By adding potassium chloride in such a range, the melting point of the electrolysis bath can be lowered to 615 to 760°C.
  • Fig. 6 shows a conceptual cross sectional diagram of the sixth desirable embodiment of the present invention.
  • Reference numeral 1 is an electrolysis vessel, an electrolysis bath 2 consisting of calcium chloride is filled therein, and it is heated to a temperature not less than the melting point of calcium chloride by a heater, which is not shown, to be maintained in a molten state.
  • Reference numeral 3 indicates a anode unified with the electrolysis vessel, and a cathode 4 having cylindrical shape is arranged being immersed in a central part of the electrolysis vessel 1. Since the upper and lower parts of the cathode 4 are open, the molten salt can be moved between the outer area and inner area of the cathode. Furthermore, a titanium tetrachloride supplying pipe 11 is arranged in the inner area of the cathode 4.
  • the electrolysis is started by connecting the anode 3 and cathode 4 to a direct current power supply, which is not shown, and at the same time adding titanium tetrachloride 12 through the titanium tetrachloride supplying pipe 11. Calcium metal in a molten state is generated on an outer surface of the cathode 4 by the starting of the electrolysis.
  • titanium tetrachloride 12 floats up in a bubbled state in the electrolysis bath 2, upward-flow occurs in the electrolyte bath 2 by this gas-lift effect, the electrolysis bath runs over from the inner area to the outer area at the upper part of the cathode, and downward-flow occurs in the outer area. In this way, flow in the electrolysis bath occurs along the arrowed line shown in Fig. 6. Calcium metal generated by the electrolysis floats up in the inner area of the cathode and sinks down in the outer area along the flow.
  • the above-mentioned upward-flow of the calcium metal generated in the inner area of the cathode contacts and reacts with the bubbles 12 of the titanium tetrachloride (TiCl 4 + 2Ca ⁇ 2CaCl 2 + Ti), to generate titanium metal.
  • the titanium metal generated is carried to the upper or lower part of the electrolysis bath by the flow of the bath, so as to be recovered by a recovering device, which is not shown.
  • Fig. 7 shows a conceptual cross sectional diagram of the seventh desirable embodiment of the present invention.
  • Reference numeral 1 is an electrolysis vessel, an electrolysis bath 2 consisting of calcium chloride is filled therein, and it is heated at a temperature not less than the melting point of calcium chloride by a heater, which is not shown, so as to be maintained in a molten state.
  • Reference numeral 3 indicates a anode unified with the electrolysis vessel, a cathode 4 having a cylindrical shape is arranged immersed in a central part of the electrolysis vessel 1. The lower part of the cathode 4 is open, and a hole communicating the outer part and inner part of the cathode is arranged at a side surface of the cathode. These communicating holes are inclined downward of the vertical direction.
  • the communicating holes of the cathode 4 are inclined from the normal line direction of the cylindrica 4 is arranged so as to be rotatable.
  • a titanium tetrachloride supplying pipe 11 is arranged at the lower part of the inner area of the cathode 4.
  • the electrolysis is started by connecting the anode 3 and cathode 4 to a direct current power supply, which is not shown, and at the same time rotating the cathode 4 and adding titanium tetrachloride 12 through the titanium tetrachloride supplying pipe 11. Calcium metal in a molten state is generated on an outer surface of the cathode 4 by the starting of the electrolysis.
  • the electrolysis bath flows from the outer area of the cathode 4 into the inner area by the rotation of the cathode 4, and furthermore, since a downward flow occurs, calcium metal which is generated is gathered in the inner area and flows downward.
  • titanium tetrachloride 12 floats up in bubbled state in the electrolysis bath and contacts with this calcium metal flow, they react to generate titanium metal.
  • the titanium metal generated is carried to the lower part of the electrolysis bath by the flow of the bath so as to be recovered by a recovering device, which is not shown.
  • Fig. 8 shows a conceptual cross sectional diagram of the eighth desirable embodiment of the present invention.
  • Reference numeral 1 is an electrolysis vessel, an electrolysis bath 2 consisting of calcium chloride is filled therein, and it is heated to a temperature not less than the melting point of calcium chloride by a heater, which is not shown, to be maintained in a molten state.
  • Reference numeral 3 is a anode which is unified with the electrolysis vessel, and a cathode 4 having cylindrical shape is arranged being immersed in a central part of the electrolysis vessel 1.
  • the lower part of the cathode 4 is open, and a hole communicating the outer part and inner part of the cathode is arranged at a side surface of the cathode.
  • a titanium tetrachloride supplying pipe 11 is arranged at the lower part of the inner area of the cathode 4.
  • An agitating fin 10 is rotatably arranged at the inner area of the cathode 4.
  • the electrolysis is started by connecting the anode 3 and cathode 4 to a direct current power supply, which is not shown, and at the same time rotating the agitating fin 10 and adding titanium tetrachloride 12 through the titanium tetrachloride supplying pipe 11. Calcium metal in a molten state is generated on an outer surface of the cathode 4 by the starting of the electrolysis.
  • the electrolysis bath flows from the outer area of the cathode 4 into the inner area by the rotation of the agitating fin 10, and furthermore, since a downward flow occurs, calcium metal which is generated is gathered in the inner area and flows downward.
  • titanium tetrachloride 12 floats up in bubbled state in the electrolysis bath and contacts with this calcium metal flow, they react to generate titanium metal.
  • the titanium metal generated is carried to the lower part of the electrolysis bath by the flow of the bath, so as to be recovered by a recovering device, which is not shown.
  • electrolysis of a molten salt of calcium chloride was performed.
  • the temperature of the electrolysis bath consisting of calcium chloride was maintained at 850 ⁇ 5°C, and the temperature of the circular cathode 4 was also maintained at 850 ⁇ 5°C, and they were not particularly being cooled.
  • Molten calcium chloride which is a raw material was continuously supplied to the inside the cathode through the bath supplying pipe 6, and at the same time, the precipitated layer of calcium metal was extracted to the outside of the system through the extracting pipe immersed in the outside the cathode.
  • Calcium metal extracted out of the system was used in a reduction reaction of titanium oxide.
  • chlorine gas generated at the anode was used in a chlorination reaction of titanium ore.
  • Calcium metal was produced corresponding to 80% of theoretical weight calculated from the amount of electricity applied to the cathode and anode.
  • calcium metal can be efficiently produced by the electrolysis of calcium chloride. Furthermore, the calcium metal can be used in the production of titanium metal, without recovery.
EP05790573A 2004-10-12 2005-10-05 Procédé de fabrication de métal et dispositif de fabrication par électrolyse du sel fondu Withdrawn EP1811062A4 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2004297865A JP4247792B2 (ja) 2004-10-12 2004-10-12 溶融塩電解による金属の製造方法および製造装置
PCT/JP2005/018449 WO2006040978A1 (fr) 2004-10-12 2005-10-05 Procédé de fabrication de métal et dispositif de fabrication par électrolyse du sel fondu

Publications (2)

Publication Number Publication Date
EP1811062A1 true EP1811062A1 (fr) 2007-07-25
EP1811062A4 EP1811062A4 (fr) 2009-04-29

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EP05790573A Withdrawn EP1811062A4 (fr) 2004-10-12 2005-10-05 Procédé de fabrication de métal et dispositif de fabrication par électrolyse du sel fondu

Country Status (9)

Country Link
US (1) US20080078679A1 (fr)
EP (1) EP1811062A4 (fr)
JP (1) JP4247792B2 (fr)
CN (1) CN101044268A (fr)
AU (1) AU2005293038A1 (fr)
CA (1) CA2582035A1 (fr)
EA (1) EA011903B1 (fr)
NO (1) NO20072241L (fr)
WO (1) WO2006040978A1 (fr)

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EP2123798A4 (fr) * 2007-02-19 2010-03-17 Toho Titanium Co Ltd Appareil pour produire un métal par électrolyse des sels fondus et procédé pour produire du métal à l'aide de l'appareil
WO2024054655A3 (fr) * 2022-09-09 2024-05-02 Phoenix Tailings, Inc. Systèmes et procédés pour introduire une matière solide et un gaz dans une cellule électrolytique

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JP4193984B2 (ja) * 2003-08-28 2008-12-10 株式会社大阪チタニウムテクノロジーズ 金属製造装置
JPWO2006115027A1 (ja) * 2005-04-25 2008-12-18 東邦チタニウム株式会社 溶融塩電解槽およびこれを用いた金属の製造方法
JP2007063585A (ja) * 2005-08-30 2007-03-15 Sumitomo Titanium Corp 溶融塩電解方法および電解槽並びにそれを用いたＴｉの製造方法
JPWO2008038405A1 (ja) * 2006-09-28 2010-01-28 東邦チタニウム株式会社 金属製造用溶融塩電解槽およびこれを用いた金属の製造方法
JP5226700B2 (ja) 2007-01-22 2013-07-03 マテリアルズ アンド エレクトロケミカル リサーチ コーポレイション イン・サイチュ生成塩化チタンの金属熱還元法
EP2149625B1 (fr) * 2007-05-11 2012-06-27 M Hikari & Energy Laboratory Co., Ltd. Installation de production intégrée sur site
JP2009019250A (ja) * 2007-07-13 2009-01-29 Osaka Titanium Technologies Co Ltd 金属製造方法および装置
CN101649472B (zh) * 2008-08-15 2012-06-06 攀钢集团钢铁钒钛股份有限公司 一种制备金属钛的方法
MD168Z (ro) * 2009-06-04 2010-10-31 Институт Прикладной Физики Академии Наук Молдовы Dispozitiv pentru acoperirea galvanică a suprafeţei interioare a pieselor cilindrice cu un diametru mic şi mijlociu
CN103270198B (zh) 2010-11-18 2017-11-14 金属电解有限公司 电解设备
JP5898686B2 (ja) * 2010-11-18 2016-04-06 メタリシス リミテッド 固体供給原料を電解により還元するための方法及びシステム
CN102517611B (zh) * 2011-12-27 2015-08-26 宁波江丰电子材料股份有限公司 熔盐电解提炼设备及其提炼金属的方法
JP6270446B2 (ja) * 2013-12-06 2018-01-31 東邦チタニウム株式会社 溶融塩電解による金属の製造方法
CN103774180B (zh) * 2014-01-28 2016-03-02 东北大学 一种集氯化-电解为一体的制取金属和合金的装置与方法
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RU2687113C2 (ru) * 2014-06-30 2019-05-07 Тохо Титаниум Ко., Лтд. Способ получения металла и способ получения тугоплавкого металла
CN104668557B (zh) * 2015-02-06 2018-12-28 安徽腾拓新材料科技有限公司 一种金属钙压锭成型设备
WO2016129009A1 (fr) * 2015-02-09 2016-08-18 国立大学法人北海道大学 Procédé de fabrication de vanadium métallique
CN104928721B (zh) * 2015-06-12 2017-09-22 中南大学 一种低价钛氯化物熔盐电解质的制备及精炼装置
CN106835203B (zh) * 2016-12-26 2019-05-31 宝纳资源控股(集团)有限公司 一种熔盐的净化装置及方法
CN107164781A (zh) * 2017-06-05 2017-09-15 攀钢集团研究院有限公司 一种制备超细钛粉的方法
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EA011903B1 (ru) 2009-06-30
AU2005293038A1 (en) 2006-04-20
CN101044268A (zh) 2007-09-26
JP4247792B2 (ja) 2009-04-02
WO2006040978A1 (fr) 2006-04-20
EA200700843A1 (ru) 2007-08-31
JP2006111895A (ja) 2006-04-27
NO20072241L (no) 2007-04-30
EP1811062A4 (fr) 2009-04-29
US20080078679A1 (en) 2008-04-03
CA2582035A1 (fr) 2006-04-20

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