US3502553A - Process and apparatus for the electrolytic continuous direct production of refined aluminum and of aluminum alloys - Google Patents

Process and apparatus for the electrolytic continuous direct production of refined aluminum and of aluminum alloys Download PDF

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US3502553A
US3502553A US476460A US3502553DA US3502553A US 3502553 A US3502553 A US 3502553A US 476460 A US476460 A US 476460A US 3502553D A US3502553D A US 3502553DA US 3502553 A US3502553 A US 3502553A
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aluminum
vessel
alloy
bath
liquid
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Hans Gruber
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    • 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
    • C25C3/06—Electrolytic production, recovery or refining of metals by electrolysis of melts of aluminium
    • C25C3/24—Refining
    • 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
    • C25C3/36—Alloys obtained by cathodic reduction of all their ions

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  • This invention relates to processes and apparatus for the continuous and direct production of refined aluminum and of aluminum alloys by electrolysis of a molten bath consisting of fluorides with aluminum dissolved therein.
  • a production unit consisting of two vessels that are not directly connected together but are connected by one or more channels. These two vessels and the connecting channels are filled with liquid aluminum alloy, forming the cathode in the first vessel and the anode in the second vessel.
  • electrodes can be used which consist of metal or carbon compounds of one or more metals.
  • a process is already known by which, in a first step, crude aluminum is produced and, in a second step, pure aluminum is extracted out of this crude aluminum by a second electrolysis.
  • impurities accumulate in the crude aluminum because purer aluminum is taken off. After a relatively short production period, a substantial part of the crude aluminum must be taken out, or the production unit has to be cut off.
  • the crude aluminum to be taken out with its high content of iron and other impurities is of very low quality.
  • an electrolytic cell for the production of crude aluminum is directly connected with an electrolytic cell working according to the three layer system.
  • An aluminum alloy forms the bipolar connection.
  • the aluminum alloy cannot be kept with a constantly uniform composition.
  • the production units of the invention may be composed of various structural parts, for example, the first vessel is one part and the second vessel together with a drawroom, out of which the alloy can be taken, is another structural part. Between these two parts, one or several channels are arranged providing a connection for the liquid alloy which is in the vessels.
  • the channels may be inclined relatively to the horizontal or vertical with respect to the opposite wall of the other vessel. They may be of different cross-sections in order to further the mixing and the circulation of the liquid bipolar alloy.
  • the first vessel has no common wall separating it from the second vessel, it is impossible that undesired electric current can flow from the liquid bath of the first vessel towards the liquid bath of the second vessel.
  • the distance between the two vessels and by this the thermal insulation of each vessel can be prearranged. Thereby it is impossible that the electrolyte of the first vessel can influence the electrolyte and the refined aluminum within the second vessel. Uniform and constant thermal conditions may be maintained despite great differences of temperatures of the baths of the two vessels.
  • Alloying metal for example copper
  • Contact pins supplying current into the anode in the first vessel, need not be pulled out or placed in higher positions because they are produced of copper or of aluminum-copper alloy.
  • This alloy is, for example, purified by segregation and thus, without the greater part of its impurities, can be taken out of the draw-room, designed for that purpose in the second vessel.
  • Copper electrodes of appropriate dimensions and temperature yield only small amounts of metal to the bath. By these measures, the proportion of copper in the liquid aluminum-copper alloy can exactly be adjusted within a large range.
  • compounds of copper can be supplied to the bath in the first vessel.
  • copper oxide can be supplied to the bath.
  • other metals can also be fed into the liquid alloy such as, for example, manganese, nickel, titanium, and these may perhaps also be fed into the bath in the second vessel.
  • aluminum can be taken out in determined quantity by distilling it out of the liquid aluminum-copper alloy under reduced pressure with appropriate apparatus.
  • the tem peratures at the respective working zones can be influenced.
  • the channels can be used to heat the related production unit or to keep it at a determined temperature, without connecting the electrodes with an outer circuit.
  • the new process refined aluminum and aluminum alloy, each with determined uniform quality, can be produced even if the raw materials used for the process are not pure.
  • the first vessel is filled with a bath of fluorides into which bath raw alumina or roughly prepared alumina have been brought.
  • the new process it is suflicient to purify the aluminous ore, such as bauxite, so that the content of iron and titanium compounds have been brought down to values that are still six times higher than those in the alumina conventionally used for the production of aluminum.
  • Iron, titanium and silicon are taken in by the aluminum-copper alloy and they are removed from it after segregation as far as necessary.
  • the final metal in the second vessel is refined aluminum.
  • pure or raw alumina is, for example, dissolved in a fluoride bath. Then this bath, saturated with alumina, is poured upon the bath in the first vessel by means of a large crucible, similar to the working process in German Patent No. 718,189.
  • the prepared fluoride bath, saturated with alumina is poured, the bath which is already in the first vessel and having less alumina, is pushed upwards through a shaft or behind a separting wall which leaves free passage for the bath at its lowermost part, so that it cannot mix with the bath being poured in.
  • the old bath flows over a spillway into a second crucible, by means of which it is poured upon the bath in another first vessel or into a cell, which produces aluminum according to the conventional process.
  • the insulating crust on the bath in the vessel is preserved, except a narrow opening through which to pour in the new bath.
  • the plant is mechanized in its greater part.
  • the copper having been part of the anode in the first vessel and being used for the liquid alloy can be impure, without this becoming disadvantageous for the final aluminum.
  • the impurities go into the liquid aluminumcopper alloy, they can be taken out of it without disturbing the course of production.
  • Impurities in the raw alumina so far as they accumulate within the electrolyte of the first vessel (for example, in case the raw material has extraordinarily great quantities of calcium or of vanadium) are separated from the electrolyte in a separate apparatus before they reduce the solubility of the alumina in the electrolyte or its conductivity. This manner of working does not reduce the productiveness of the units as is the case with conventional processes.
  • the production units of the invention do not need collector bars in their bottoms, as are used in producing primary or refined aluminum by conventional processes. Therefore, the losses of voltage related with the bottoms are eliminated as well as the strain and wear resulting from the flow of current. Thus, less enegy, material, fluoride bath, and work are spent than are necessary in conventional processes for changing used-up bottoms for new bottoms.
  • the protecting casings around the anodes in the first vessel and the contact pins, supplying the current into these electrodes consist for example of an aluminumcopper alloy, that has a higher melting temperature than temperature existing at the anodes within the fluoride bath or they consist of copper.
  • the anodes still have their complete original cross-section down in the fluoride bath.
  • one of the hot workings at the furnace is eliminated, in case of vertically as well as laterally inserted contact pins, because these parts of the electrical connections remain in the electrodes and melt and drop into the aluminum-copper alloy. Because conducting the current under the surface of the bath becomes more favorable, the losses of voltage in the anodes are reduced.
  • the efliciency of the current becomes more favorable, because by means of the channels the surface of the anodic metal regularly, locally and continuously is supplied from the first vessel with fresh alloy having a high proportion of aluminum.
  • This is not possible with the conventional three layer process because the aluminum from the depth of an aluminum-copper alloy has to be brought upwards to the electrolyte.
  • the layer of the alloy is relatively high and the least mobile, and that part of the alloy. which is least hot and in the cell in its region, least warm. This is also not possible when a cell for the production of primary aluminum is directly connected together with a cell working the three layer process without the connecting channels.
  • the conventional electrodes consisting of baked carbon or of graphite
  • these metal anodes for example, are designed with vertical shafts for the exhaust of the gases at the anode, for automatic charging of alumina, or to insert liquid fluoride bath with alumina in it.
  • the second vessel from a metal cathode of appropriate dimensions and current load, practically no metal is transported by diffusion against the flow of current into the aluminum that is below this cathode.
  • the consumption of baked carbon and of graphite electrodes becomes less when using metal electrodes, for example also when these are put in to keep the exact quantity and composition of the aluminum-copper alloy, because the current efiiciency and the voltage of the production unit can be adjusted to their optimal values and constantly maintained there.
  • the metal electrodes for example, consist of aluminum, chromium, cobalt, copper, manganese, nickel or of titanium or of their alloys with one another or with other metals.
  • FIGURE 1 is a diagrammatical vertical cross-section through an apparatus for effecting the process of the invention.
  • FIGURE 2 is a top plan view of the apparatus shown in FIG. 1, empty and omitting the electrodes.
  • the illustrated production unit is mainly composed of three structural parts: a first vessel 1, a second vessel 2, and channels 4 connecting these vessels.
  • the vessels and the channels each consist of a metal casing 15 with an insulating layer 16 and a lining 17 consisting of alumina and magnesium oxide refractories.
  • a wall 5 which leaves free passage at least at one place at the bottom thereof, separates a draw-room 3 from the portion of the room opposite the channels 4.
  • the alloy can be taken from said draw-room.
  • the liquid aluminum alloy 8 that also fills the lower part of the channels 4.
  • the Ways into and out of the channels are located beneath the surface of the alloy.
  • the fluoride bath 9 of the first vessel 1 therefore has no bath-to-bath connection with the fluoride bath in the second vessel 2.
  • the openings are also under the surface of the aluminum alloy in the lower part of the separating wall that leaves free passage at several places to the draw-room 3 for the alloys only.
  • the alloy is under protective baths 11, 12.
  • the layer of refined aluminum 13 is the layer of refined aluminum 13.
  • the electrodes 6 consist of carbon electrodes, copper electrodes, and aluminum-copper electrodes.
  • the fluoride bath 9 belonging to the first vessel is composed of fluorides of aluminum, barium, calcium and sodium, and further of alumina dissolved in this bath.
  • the liquid aluminum-copper alloy 8 consists of one-third copperthe balance in this example being aluminum and small amounts of other metals.
  • the aluminum is previously produced in the first vessel, whereas the copper comes from the copper electrodes and from the aluminum-copper electrodes.
  • the fluoride bath 10 in the second vessel 2 in this example is composed of the same fluoride as are in the first vessel. Converted by calculation to the composition of fluoride of aluminum, the bath in the second vessel has 50% of the aluminum fluoride, whilethe total content of fluorides in the bath is kept at 50%, and the bath is free of oxides. This process is working with warm aluminum-copper alloy. Contrary to conventional methods, it is avoided that parts are deposited on the bottom below the alloy in the second vessel, hampering the efiiciency of the production.
  • the liquid alloy is always kept at such a temperature that it is possible to effect production without difficulties with a composition range, for example, of 62% copper, with a balance of aluminum, plus silicium, plus iron, and small amounts of other metals.
  • a composition range for example, of 62% copper, with a balance of aluminum, plus silicium, plus iron, and small amounts of other metals.
  • 32% copper it is possible to work with good efliciency and without difliculties with an alloy having as much as 11% silicon plus iron, the rest being aluminum plus small amounts of other metals.
  • the large constant caloric capacity of the production unit eliminates also that in the first and in the second vessels 1 and 2 crusts are formed narrowing unfavorably the upper portion of the baths.
  • the reason for this is that the casing and the contact pins for the continuous anode take an essential part of the electric current at the most downward part of this anode. Therefore, at the beginning of the production process also, coking of the carbonaceous mass of the anode has to take place only in a relatively shorter part, compared with the conventional method of aluminum production.
  • Impurities brought in with the supplied material are separated from the liquid alloy 8 within the draw-room 3.
  • the separated and segregated material is taken out.
  • the purified aluminum-copper alloy 8 stays with the production unit or it is brought to further manufacturing units.
  • the draw-room 3 alternatively can be arranged at another place in the production unit, or it can be connected with the unit by channels.
  • the alloy In order to avoid that the liquid alloy 8 takes in gas, or that it become superficially oxidized when in the channels 4 or in the draw-room 3, the alloy is below a protective layer of, for example, molten salts 11, 12, with which the channels and/or the draw-room have been filled similar to the working process in German Patent 718,189.
  • the first and second vessels 1, 2 can be charged, for starting the production, with molten fluoride baths 9, 10 that have been previously purified, in order to keep low quantity of gas occlusion by the aluminum-copper alloy 8 and by the refined aluminum 13 from the start.
  • Undesired side-reactions can occur, due to incoming oxygen, nitrogen or hydrogen, the latter for example, originating from humidity adhering to unmolten salts in the first as well as in the second vessel.
  • the rooms to be filled with the alloy can wholly or partly be lined with copper or an aluminum-copper alloy, which are taken in by the liquid alloy after the remainder of the humidity has been driven out of the furnace brick lining, rammed paste, etc., at high temperature.
  • gases are brought into the fluoride bath by surface skin owing, to oxidation of metal, as is the case with conven tional methods.
  • the refined aluminum 13 has therefore substantially less gas occlusion that usual. Consequently, the periods for de-gassing in the melting furnaces are shorter or can be eliminated and flawless rolling blocks can be cast.
  • the circulation of the liquid alloy can be checked and influenced (for example, by narrowing the cross-section of the free passage in one of the chan tels). They are covered when the production is runnmg.
  • the temperature of the liquid aluminum-copper alloy can be adjusted from the first vessel 1. From there, the temperature in the second vessel 2 is especially easily influenced, when a lower working temperature is used for the fluoride bath 10 in the second vessel 2 than in the first vessel 1. Contrary to conventional working processes for the production of primary aluminum with a cathode consisting of aluminum, the new process with the cathode of the heavier aluminum-copper alloy 8 is independent of the density of the fluoride bath 9 in the first vessel 1. The process allows adding substances to the fluoride bath 9, in order to raise the value of its conductivity, or to bring metals into the alloy. Because the second vessel 2 is heated by the alloy 8 from the lower part, there are only small losses of fluoride bath by evaporation.
  • this temperature can be kept at the same magnitude'and the distance between the liquid alloy 8 and the cathode 7 kept constant, by correspondingly adjusting in the first vessel 1 the distance between the electrodes 6 and the liquid alloy 8.
  • the shaft 14 itself consists, for example, of a graphite tube, or within the shaft into the liquid alloy a graphite tube is inserted.
  • a metal tube, the melting temperature of which is at least C. higher than the temperature of the liquid alloy can also be used.
  • a graphite tube inserted into the shaft 14 can serve as an electrode for the outgoing current or for part of it in order to influence the production within the second vessel or to electrically cut it ofl from production.
  • refined aluminum and aluminum alloys can be produced as follows:
  • Crushed bauxite is dried in a story-furnace and at the same time the iron oxides are partly reduced.
  • the dried and hot bauxite next enters a rotary kiln, of which the outgoing gases, together with other gases, are used in the aforementioned story-furnace.
  • the bauxite, mixed with carbonaceous material is exposed to the reducing eflect of a mixture of gases containing carbon monoxide and hydrogen.
  • the hot material the compounds of iron being for the most part reduced to metallic iron, enters through an opening, an otherwise closed large vessel that contains liquid fluoride bath which has been made of cryolite.
  • Carbon electrodes connected with the secondary windings of a three-phase tranformer, extend deep into the fluoride bath which is covered with carbon in surplus.
  • the impure alumina is dissolved in the fluoride bath, whereas the spongy iron accumulates in the lower part of the vessel.
  • the specific heavier parts of the bath with the spongy iron in it flow upwards into a second vessel when liquid fluoride bath, taken out of the electrolysis plant, is poured into the large vessel. After the part of the bath containing the iron thus has been pushed away into the second vessel, direct current is switched onto the electrodes in the large vessel.
  • the carbon bottom of this large vessel is the negative electrode. Electrolysis is continued as long as the iron has practically all been deposited.
  • the part with the iron When adding once more fluoride bath out of the transport crucibles, then the part with the iron also flows through the shaft into the second vessel.
  • the impure bath from the second vessel is electrically heated so that the spongy iron flows together forming liquid iron and can be separated form the bath, that is above the iron. If necessary, this part of the circulating bath can be purified of the calcium oxide accumulated in it by means of known processes and then added into the bath in the large vessel.
  • the bath can by several steps be refined further, by passing it from the first production unit successively into the second and third production units by means of large transport crucibles. It is thus so purified that, since it contains still enough A1 this bath can be put into conventional cells for the production of primary aluminum.
  • these and the channels are filled to a sufliciently high level above the bottom of the walls 5 with aluminum-copper alloy, so that the fluoride baths cannot mix while being poured in.
  • the process can be started with originally impure fluoride bath, during production only pure, high-grade and purest aluminum come out. That is only possible because the working process and the apparatus are designed to secure a highly equalized running of the production units. Due to the process, the resulting aluminum alloy also has uniform composition, because it is continuously adjusted to the desired condition, without the interrupted steps of conventional production.
  • the electrolysis plant is almost fully mechanized, skilled workman and staff may be concentrated at the necessary places, the input of electric current, electrodes, fluoride bath, size of buildings for the plant, and time required are reduced.
  • the new working process is a marked step forward because raw materials for the copper industry can be worked to aluminum-copper alloys in the electrolysis plants of the aluminum industry and because the total input of material and energy is less.
  • a process comprising forming first and second spaced bodies of liquid aluminum alloy, connecting said bodies through liquid aluminum alloy in at least one channel, superposing molten fluoride baths with alumina therein on said bodies and maintaining the baths separate from each other, inserting into the baths electrodes which are spaced from said bodies and which are constituted of carbon compounds of metal, metal alloys and metals, and passing current between the electrodes -via said bodies and the liquid alloy in the channel, the electrodes associated with said first body losing material into said first body, the electrodes associated with said second body being formed of a material of which the melting temperature is at least one hundred degrees centigrade higher than the working temperature at the cathode, refined aluminum being withdrawn from said second body.
  • a process as claimed in claim 1, comprising distilling aluminum out of said second body under reduced pressure.
  • a process as claimed in claim 2, comprising adding aluminum to said first body while current is being passed between said electrodes.
  • a process as claimed in claim 3, comprising adding supplemental fluoride bath with alumina therein to the bath associated with said first body while current is being passed between the electrodes.
  • a process as claimed in claim 4, wherein the bath superposed on said first body includes fluorides of aluminum, barium, calcium and sodium.
  • a process as claimed in claim 4, comprising supporting the bodies in vessels which are dehumidified before being loaded.
  • a process as claimed in claim 4, comprising electrically heating said first body and controlling the heat of said second body from said first body.
  • a process as claimed in claim 4, comprising spacing the electrodes from said second body at a greater distance than the electrodes are spaced from said first body.
  • Apparatus for processing aluminum comprising a first vessel adapted for containing liquid aluminum alloy, a second vessel adapted for containing liquid alloy, said vessels being spaced from each other, means defining at least one channel connecting the vessels at lower portions thereof and through which said liquid alloy can flow from one vessel to the other, and electrodes extending downwardly into said vessels to electrolysis positions, said vessels extending above said at least one channel to encompass said electrodes at least in part and to accommodate molten fluoride baths superposed on the liquid alloy, said vessels and means cooperatively isolating the baths from each other, whereby current can flow from one vessel to the other through alloy in said channel.
  • Apparatus as claimed in claim 11, comprising means defining a draw-room in the production unit consisting of said first vessel, said at least one channel and said second vessel and adapted to receive alloy at the lower part thereof and to accommodate a bath of molten salt superposed on the alloy in the draw-room.
  • Apparatus as claimed in claim 13, comprising means defining in said first vessel a vertical shaft of which the lower opening is above said liquid alloy and of which the upper opening serves as a spillway for the liquid bath.
  • Apparatus as claimed in claim 13, comprising means defining a vertical shaft extending down into said alloy and enabling the distillation of aluminum under reduced pressure.

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US476460A 1965-02-16 1965-08-02 Process and apparatus for the electrolytic continuous direct production of refined aluminum and of aluminum alloys Expired - Lifetime US3502553A (en)

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CH213165A CH485027A (de) 1965-02-16 1965-02-16 Verfahren und Vorrichtung zum kontinuierlichen unmittelbaren Erzeugen von Rein-Aluminium und Aluminium-Legierungen durch Schmelzfluss-Elektrolyse

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Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3620942A (en) * 1969-03-19 1971-11-16 Haskett Barry F Natural circulation of cathode metal of electrolytic cell
US3661736A (en) * 1969-05-07 1972-05-09 Olin Mathieson Refractory hard metal composite cathode aluminum reduction cell
US4338177A (en) * 1978-09-22 1982-07-06 Metallurgical, Inc. Electrolytic cell for the production of aluminum
US4392925A (en) * 1980-05-14 1983-07-12 Swiss Aluminium Ltd. Electrode arrangement in a cell for manufacture of aluminum from molten salts
US4504366A (en) * 1983-04-26 1985-03-12 Aluminum Company Of America Support member and electrolytic method
US4664760A (en) * 1983-04-26 1987-05-12 Aluminum Company Of America Electrolytic cell and method of electrolysis using supported electrodes
US4778575A (en) * 1988-01-21 1988-10-18 The United States Of America As Represented By The United States Department Of Energy Electrodeposition of magnesium and magnesium/aluminum alloys
US4882017A (en) * 1988-06-20 1989-11-21 Aluminum Company Of America Method and apparatus for making light metal-alkali metal master alloy using alkali metal-containing scrap
US5254232A (en) * 1992-02-07 1993-10-19 Massachusetts Institute Of Technology Apparatus for the electrolytic production of metals
US5660710A (en) * 1996-01-31 1997-08-26 Sivilotti; Olivo Method and apparatus for electrolyzing light metals
US5855757A (en) * 1997-01-21 1999-01-05 Sivilotti; Olivo Method and apparatus for electrolysing light metals
US20150225864A1 (en) * 2014-02-13 2015-08-13 Phinix, LLC Electrorefining of magnesium from scrap metal aluminum or magnesium alloys
CN104962954A (zh) * 2015-07-30 2015-10-07 江西理工大学 一种熔盐电解制备稀土-铝-铜中间合金的方法及其合金
CN105177632A (zh) * 2015-07-30 2015-12-23 江西理工大学 稀土改性制备铜-铝-稀土中间合金熔盐电解方法及合金
CN106894052A (zh) * 2017-04-19 2017-06-27 新疆大学 一种制备高纯铝的联体‑多级铝电解装置及其使用方法
CN106929688A (zh) * 2017-04-17 2017-07-07 新疆大学 一种利用铝灰渣制备高纯铝的装置与方法
CN109609975A (zh) * 2019-02-01 2019-04-12 孟静 电解原位制备铝合金的方法
CN109797285A (zh) * 2019-04-02 2019-05-24 昆明理工大学 一种氧化铝间接碳热还原制备金属铝的方法

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US2742418A (en) * 1952-08-28 1956-04-17 Ethyl Corp Electrolytic cell for alkali-lead alloy manufacture
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US2953506A (en) * 1958-04-29 1960-09-20 Aluminium Ind Ag Method and apparatus for refining aluminum
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US542057A (en) * 1895-07-02 Son paul hulin
US765001A (en) * 1903-05-09 1904-07-12 Gustave Gin Process of manufacturing vanadium and its alloys.
US1490504A (en) * 1922-05-20 1924-04-15 Aluminum Co Of America Electrode
US1782616A (en) * 1927-07-04 1930-11-25 Alais & Froges & Camarque Cie Electrolytic apparatus for refining aluminum and for like processes
US2552423A (en) * 1947-11-30 1951-05-08 Glazunov Alexandre Process for the direct production of refined aluminum
US2742418A (en) * 1952-08-28 1956-04-17 Ethyl Corp Electrolytic cell for alkali-lead alloy manufacture
US2919234A (en) * 1956-10-03 1959-12-29 Timax Associates Electrolytic production of aluminum
US3063930A (en) * 1956-12-27 1962-11-13 Montedison Spa Valveless pump, particularly for fused salts or metals
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Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3620942A (en) * 1969-03-19 1971-11-16 Haskett Barry F Natural circulation of cathode metal of electrolytic cell
US3661736A (en) * 1969-05-07 1972-05-09 Olin Mathieson Refractory hard metal composite cathode aluminum reduction cell
US4338177A (en) * 1978-09-22 1982-07-06 Metallurgical, Inc. Electrolytic cell for the production of aluminum
US4392925A (en) * 1980-05-14 1983-07-12 Swiss Aluminium Ltd. Electrode arrangement in a cell for manufacture of aluminum from molten salts
US4504366A (en) * 1983-04-26 1985-03-12 Aluminum Company Of America Support member and electrolytic method
US4664760A (en) * 1983-04-26 1987-05-12 Aluminum Company Of America Electrolytic cell and method of electrolysis using supported electrodes
US4778575A (en) * 1988-01-21 1988-10-18 The United States Of America As Represented By The United States Department Of Energy Electrodeposition of magnesium and magnesium/aluminum alloys
US4882017A (en) * 1988-06-20 1989-11-21 Aluminum Company Of America Method and apparatus for making light metal-alkali metal master alloy using alkali metal-containing scrap
US5254232A (en) * 1992-02-07 1993-10-19 Massachusetts Institute Of Technology Apparatus for the electrolytic production of metals
US5660710A (en) * 1996-01-31 1997-08-26 Sivilotti; Olivo Method and apparatus for electrolyzing light metals
US5855757A (en) * 1997-01-21 1999-01-05 Sivilotti; Olivo Method and apparatus for electrolysing light metals
US10017867B2 (en) * 2014-02-13 2018-07-10 Phinix, LLC Electrorefining of magnesium from scrap metal aluminum or magnesium alloys
US20150225864A1 (en) * 2014-02-13 2015-08-13 Phinix, LLC Electrorefining of magnesium from scrap metal aluminum or magnesium alloys
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CN105177632A (zh) * 2015-07-30 2015-12-23 江西理工大学 稀土改性制备铜-铝-稀土中间合金熔盐电解方法及合金
CN105177632B (zh) * 2015-07-30 2017-06-06 江西理工大学 稀土改性制备铜‑铝‑稀土中间合金熔盐电解方法及合金
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CN106929688B (zh) * 2017-04-17 2018-08-17 新疆大学 一种利用铝灰渣制备高纯铝的装置与方法
CN106894052A (zh) * 2017-04-19 2017-06-27 新疆大学 一种制备高纯铝的联体‑多级铝电解装置及其使用方法
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