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WO2006103085A1 - Procede et appareil de production d'aluminium - Google Patents

Procede et appareil de production d'aluminium Download PDF

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Publication number
WO2006103085A1
WO2006103085A1 PCT/EP2006/002949 EP2006002949W WO2006103085A1 WO 2006103085 A1 WO2006103085 A1 WO 2006103085A1 EP 2006002949 W EP2006002949 W EP 2006002949W WO 2006103085 A1 WO2006103085 A1 WO 2006103085A1
Authority
WO
WIPO (PCT)
Prior art keywords
alumina
aluminiumsulphide
melt
bubble column
reactor
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.)
Ceased
Application number
PCT/EP2006/002949
Other languages
English (en)
Inventor
Dietrich Willem Van Der Plas
Yanping Xiao
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.)
Novelis Koblenz GmbH
Original Assignee
Aleris Aluminum Koblenz GmbH
Corus Aluminium Walzprodukte GmbH
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 Aleris Aluminum Koblenz GmbH, Corus Aluminium Walzprodukte GmbH filed Critical Aleris Aluminum Koblenz GmbH
Priority to AU2006228730A priority Critical patent/AU2006228730B2/en
Priority to DE602006014108T priority patent/DE602006014108D1/de
Priority to EP06723909A priority patent/EP1863953B1/fr
Priority to AT06723909T priority patent/ATE466974T1/de
Priority to CA2603095A priority patent/CA2603095C/fr
Publication of WO2006103085A1 publication Critical patent/WO2006103085A1/fr
Anticipated expiration legal-status Critical
Priority to NO20075476A priority patent/NO20075476L/no
Ceased legal-status Critical Current

Links

Classifications

    • 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
    • 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
    • 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
    • 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
    • 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
    • C25C3/18—Electrolytes

Definitions

  • the invention relates to a method for the continuous production of aluminium from alumina comprising a first step of converting alumina (AI 2 O 3 ) into aluminiumsulphide (AI 2 S 3 ) and a second step of separation of aluminium from aluminiumsulphide in a separating reactor. Furthermore, the invention relates to an apparatus for operating the method.
  • Another drawback of the disclosed method is that, in order to perform the separation step of aluminiumsulphide efficiently at a low voltage, in particular by electrolysis using inert electrodes, it is required that a large fraction, preferably all, of the alumina is converted in the sulphidation step into aluminiumsulphide before the reaction components of the sulphidation step are fed into the electrolysis cell.
  • Alumina present in an electrolysis cell operated at a low voltage is not discomposed and settles in the cell as a sludge, which has to be removed. Removal of sludge disturbs the operation of the electrolysis cell and more importantly, brings about the risk of introducing oxygen into the electrolysis cell, which converts aluminiumsulphide back into alumina.
  • the alumina that remains present in the electrolysis cell may dissolve and saturate the electrolyte, thus hindering further dissolution of aluminiumsulphide and subsequent separation of aluminium from aluminiumsulphide.
  • a nearly complete conversion of alumina into aluminiumsulphide reduces the overall efficiency of the process. In practice the conversion rate slows down as the reaction proceeds, and the efficiency of the sulphidation reaction decreases, as the time, the reactor volume, and the amount of sulphidation agents required per unit of aluminiumsulphide increase.
  • a further drawback is that compounds from the separation step, in particular alumina, have to be discarded.
  • alumina comprising a first step of converting alumina (AI 2 O 3 ) into aluminiumsulphide (AI 2 S 3 ) and a second step of separation of aluminium from aluminiumsulphide in a separating reactor, and wherein the separating apparatus is a electrolysis cell, and wherein in the first step in a conversion reactor alumina is dissolved in a molten salt to form a melt and a sulphur containing gas is fed through the melt whereby the sulphur containing gas acts as a reagent to convert at least part of the alumina into aluminiumsulphide and at least part of the melt is used in the second step, and wherein the melt with the dissolved alumina and the aluminiumsulphide is continuously recirculated between the first and the second process step.
  • alumina in the first step in a conversion reactor alumina is dissolved in a molten salt to form a melt and a sulphur containing gas is fed through the melt whereby the sulphur
  • the term “salt” also comprises a mixtures of salts
  • the term “sulphur containing gas” comprises sulphides.
  • the method according to the invention has one or more of the following advantages.
  • the aluminiumsulphide formed is dissolved in the molten salt and can easily be transported to the second, separation, step. So the handling problem of the prior art method is eliminated or at least reduced.
  • Another advantage is that the melt, even with an incomplete conversion of alumina into aluminiumsulphide, is suitable for a variety of separation processes. Any alumina remaining in the melt after separation can be fed back with the molten salt into the first, conversion, step.
  • Another advantage is that the process is operated in a continuous or at least semi- continuous fashion, which to a very large extent eliminates yield losses and operating difficulties that are associated with batch type processes or processes that require frequent standstills or maintenance. Examples of the latter include the present
  • the Hall-Heroult process for the reduction of alumina into metallic aluminium which requires regular replacement of the consumable anodes.
  • the carbon electrodes due to the reduced cell voltage, the carbon electrodes remain inert and can be used for a prolonged time.
  • the Hall-Heroult cell must be designed to dissipate heat, which obstructs more favourable compact cell designs.
  • substantially all the heat that is generated by ohmic losses is absorbed in the conversion from alumina to aluminium, and the cell design can be made much more compact.
  • Yet another advantage connected with the continuous recycling process is that it is not necessary to convert a considerable amount of alumina into aluminiumsulphide. So the time for conversion can be selected such that an optimum can be reached between time for conversion on the one hand and flow of aluminium containing melt back from the separation step into the conversion step on the other hand. Any alumina that is not converted but fed into the separation step as part of the melt, can be fed back into the conversion step and therefore, does not create a waste flow that may have to be discarded.
  • a relevant characteristic of the alumina being dissolved in the melt is that any product from the sulphidation reaction is directly available in the melt, which eliminates the need for a separation of the alumina and aluminiumsulphide containing species.
  • the sulphidation reaction proceeds by direct contact between the sulphidising gas and the melt.
  • the whole gas/liquid interface is used as a contact area for the sulphidation reaction. This is an important advantage over reactions between a gas and particles dispersed in a melt, where only a small fraction of the gas/liquid interface is occupied by gas/particle contact.
  • the melt as described herein comprises a mixture of various, complex ions, similar to what is known from the regular Hall-Heroult process for the reduction of alumina.
  • AI 2 O 3 and AI 2 S 3 need not be present in their molecular form, but also may be present as ionic species that are associated in particular with the dissolution of AI 2 O 3 and AI 2 S 3 .
  • alumina and aluminiumsulphide that are used throughout this description refer to and include these ionic species as well as the molecular form.
  • At least part of the melt may be fed to the electrolysis cell where the salt can act as the electrolyte for the electrolysis.
  • the conditions in the electrolysis cell can be selected such that aluminiumsulphide is decomposed, thereby separating aluminium, while at the same time not decomposing alumina.
  • the melt in the electrolysis cell is lower in aluminiumsulphide content but in practice unchanged in alumina and can be fed back into the conversion reactor. Further, because of the lower cell voltage needed to decompose aluminiumsulphide as compared to the voltage needed to decompose alumina, inert electrodes with a long lifetime can be used.
  • a feature of the invention is also that at least part of the melt with dissolved aluminiumsulfide is fed to the separating reactor and at least part of the melt with dissolved reaction products from the step of separation in the separating reactor is fed into the conversion reactor. At least part of the melt from the conversion reactor is fed to the separating reactor, and at least part of the melt in the separating reactor is fed back into the conversion reactor, wherein feeding and feeding back is done in a continuous process.
  • the method according to the invention is therefore carried out as a continuous process.
  • the prior art process is a batch process. In the first step, all alumina should be converted into aluminiumsulphide, which is then batch-wise fed into the separating apparatus. In particular when the separation takes place in an electrolysis cell, the batch-wise addition of aluminiumsulphide disturbs the electrolysis and changes the operating condition of the cell.
  • An embodiment of the method of the invention is characterized in that the separating apparatus is a multi-pole electrolysis cell.
  • a multi- polar cell which incorporates a series of anodes and cathodes in one single cell.
  • An advantage is a far more compact cell design, thus reducing investment and operational costs.
  • a second advantage is a reduction of ohmic losses, thus contributing to the energy efficiency of the process.
  • the electrolysis cell has a compact design and any heat dissipation to the surroundings is minimised in order to use substantially all of the enthalpy from the ohmic losses as energy input to the sulphidation step.
  • a further embodiment of the method according to the invention is characterized in that the first step and the second step are performed or carried out in a reactor vessel operating as a single reactor.
  • the method of the invention can be carried out in a compact reactor which requires less volume and is less costly, both in construction and in operation, then separate reactors for steps one and two. Also transport problems as mentioned before are further mitigated.
  • a further advantage can be obtained in energy consumption.
  • the conversion of alumina into aluminiumsulphide is an endothermic reaction.
  • the separation of alumina from aluminiumsulphide, in particular in an electrolysis cell is connected with heat generation through energy dissipation in the electrolyte. By supplying this generated heat to the conversion step, a high energy efficiency can be achieved. This is particularly so when at least part of the melt is made to circulate between the two steps using two reactors or a single integrated reactor.
  • the sulphur containing gas is substantially carbondisulphide (CS 2 ).
  • the molten salt substantially comprises chloride salts, and preferably a mixture of NaCI and KCI.
  • NaCI and KCI are relatively inexpensive, its mixture, more in particular the eutectic composition, has a suitable melting point, a low vapour pressure in the proposed operational window of the process, and they are harmless under regular operating conditions.
  • composition of the molten salt comprises in the range of between 30 and 70 wt.% NaCI and in the range of between 70 and 30 wt.% KCI.
  • a further embodiment of the method of the invention is characterized in that the melt of salt comprises a fluorine containing compound.
  • the suitable fluorine containing compound may include one or more compounds having a molecular formula Na 3 AIF 3+3 and/or K 3 AIF 3+3 ("a" being an integer equal to a greater than 1), such as NaAIF 4 , Na 2 AIF 5 and Na 3 AIF 6 , and KAIF 4 , K 2 AIF 5 and K 3 AIF 6 .
  • the fluorine compound may further include one or more of: a simple mixture of NaF or AIF 3 , a simple mixture of KF or KF 3 , an eutectic mixture of NaF and AIF 3 , an eutectic mixture of KF and KF 3 , and a certain complex such as sodiumfluoraluminate or pottasiumfluoraliminate. Any one of these fluxes may be selected, though two or more of them may be added in combination.
  • cryolite fused sodium aluminiumfluoride, commonly called cryolite, or a mixture of cryolite and other fluorides is used.
  • the melt of salt is substantially free of alkaline earth metals or compounds thereof. It has been shown that alkaline earth metals have a good affinity to sulphur and form sulphides before aluminiumsulphides can form. Therefore earth alkaline metals have a detrimental effect on the efficiency of the sulphide containing gas.
  • the conversion reactor is a bubble column wherein the sulphide containing gas is fed into the lower portion thereof thereby forming bubbles which rise in the bubble column.
  • Bubble columns per se are known in the process industry. They have the advantage of being based on a proven technology and they can be manufactured in an embodiment suitable for the method of the invention.
  • An advantageous embodiment of the method according to the invention is characterized in that the bubbles rising in the bubble column are used to transport at least part of the aluminiumsulphide containing melt to the separating apparatus.
  • Bubbles rising up in the bubble column lift molten salt with aluminiumsulphide dissolved therein. This lifting action can be used to transport aluminiumsulphide from the bubble column to the separating reactor, thereby saving energy and reducing complexity of the total plant for the production of primary aluminium.
  • the bubbles rising in the bubble column are used to provide at least part of the driving force to recirculate the melt between the sulphidation and separation stages.
  • Yet another embodiment of the method according to the invention is characterized in that the conversion of alumina into aluminiumsulphide is carried out at a temperature in a range of between 700 0 C and 1100 0 C, preferably in a range of between 800 0 C and 1000°C, more preferably in a range of between 800 0 C and 900 0 C.
  • the temperature at which the conversion is carried out is preferably chosen below about 1100 0 C, more preferably below about 1000°C and even more preferably below about 900 0 C.
  • the temperature at which the conversion is done is preferably chosen above about 700 0 C, more preferably above 800 0 C.
  • the sulphidation process is carried out at a pressure above atmospheric pressure, preferably at a pressure above 2 bar, and more preferably at a pressure of 3 bar or more.
  • the invention is also embodied in an apparatus for carrying out the method according to the invention and comprising a bubble column suitable for converting alumina into aluminiumsulphide by a gaseous sulphur containing compound, feeding means for feeding the gaseous sulphur containing compound into the bottom portion of the bubble column, an electrolysis cell, a first connecting duct between the top portion of the bubble column and the electrolysis cell and a second connecting duct between the lower portion of the bubble column and the electrolysis cell.
  • a bubble column is a well-known reactor vessel embodying proven technology and suitable for reactions between a melt and a gaseous reactant.
  • use can be made of the lifting effect of the rising bubbles to convey aluminiumsulphide to the electrolysis cell.
  • ducts are provided for transport of molten salt from the bubble column to the electrolysis cell and in reverse direction. It is noted that the ducts can be part of the two reactors, bubble column and the electrolysis cell, whereby these two reactors are then integrated into a single reactor.
  • Fig. 1 shows a basic diagram of an apparatus for the production of aluminium for alumina according to the invention
  • Fig.2 shows the decrease of the reaction rate as conversion proceeds for various temperatures according to the prior art
  • Fig. 3 shows the effect of the reaction time (in minutes) on the conversion rate in %) according to the present invention
  • Fig. 4 shows the effect of the temperature (in 0 C) in the conversion reactor on the conversion rate (in %);
  • Fig. 5 shows the effect of the partial pressure (in bar) of carbonsulphide on the conversion rate (in %).
  • reference number 1 refers to a conversion reactor, preferably in the form of a bubble column.
  • Alumina is fed into the conversion reactor through alumina supply line 2.
  • the conversion reactor 1 contains a bath 3 of molten salt.
  • a sulphur and carbon containing gas, such as CS 2 is fed to the bottom portion of the conversion reactor 1.
  • alumina is dissolved in the molten salt and converted into aluminiumsulphide.
  • aluminiumsulphide is decomposed into molten aluminium and gaseous sulphur.
  • a bath of molten aluminium 7 is formed, which can be tapped off through tapping line 8.
  • As the liquid is transported to the first transfer duct 5 by the gas lift in the bubble column, a similar amount of liquid is entrained from the second transfer duct 9.
  • the gas lift in the bubble column provides a driving force for the recirculation of the melt between the sulphidation and the separation reactor.
  • no external agents like pumps may be required.
  • Components present in the separating reactor 6 are fed back into the conversion reactor 1 through the second transfer duct 9.
  • the components fed back into the conversion reactor may still contain alumina and not yet decomposed aluminiumsulpihde.
  • Conversion reactor 1 Conversion reactor 1 , first transfer duct 5, separating reactor 6 and second transfer duct 9 from a closed loop system in which molten salt, alumina and aluminiumsulphide circulate.
  • First transfer duct 5 and second transfer duct 9 may be constructed such that they form part of one or both of the reactors leading to a single reactor in which both steps, conversion and separating, take place.
  • Gaseous sulphur from the separation step is fed back through sulphur return line 10 to the carbondisulphide plant 11.
  • sulphur return line 10 to the carbondisulphide plant 11.
  • reaction products or unreacted reactants from the conversion process such as COS, CS 2 and S 2 are fed back through feed back line 12.
  • Make-up sulphur is fed to the carbondisulphide plant 11 through sulphur supply line 13; a carbon containing reactant, such as natural gas is fed to the carbondisulphide plant 11 through carbon supply line 14.
  • the components therein rise in temperature, such that the flow of components through the second transfer duct 9 have a higher temperature than the components conveyed through first transfer duct 5.
  • a temperature rise from 790°C to 800°C can be mentioned. This extra sensible heat can be used for the endothermic conversion of alumina into aluminium sulphide.
  • the components flowing through the first transfer duct 5 are high in aluminiumsulphide, the components flowing through the second transfer duct 9 are low in aluminiumsulphide.
  • Fig. 2 shows the effect of reaction time of the conversion rate for the sulphidation process according to the prior art disclosed in WO-00/37691. It is observed that the reaction rate slows down as conversion proceeds. Thus, the known process becomes less efficient for a high conversion ratio, while at the same time, a full conversion is desired for the subsequent separation process.
  • Fig. 3 shows the effect of the reaction time on the conversion ratio in a method according to the invention.
  • gamma alumina was added to a salt mixture containing a eutectic composition of NaCI and KCI, and to which 10 wt.% of cryolite was added.
  • the experiment was carried out at atmospheric pressure, the CS 2 partial pressure being about 0.70 bar.
  • increase of reaction time has a positive effect on the conversion ratio.
  • the conversion rate (amount of alumina converted per unit of time) remains substantially constant.
  • Fig. 4 shows the measured effect of the temperature on the conversion ratio after 100 minutes. Apart from the temperature, all experimental conditions were identical to those described with figure 2. These measurements show that the temperature in the conversion reactor preferably lies in the range between about 800 0 C and about 1000 0 C.
  • Fig. 5 shows the effect of the partial pressure of carbondisulphide in the conversion reactor on the conversion rates after 100 minutes. Apart from the CS 2 partial pressure, all experimental conditions were identical to those described with Fig.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Manufacturing & Machinery (AREA)
  • Mechanical Engineering (AREA)
  • Electrolytic Production Of Metals (AREA)
  • Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
  • Chemical Treatment Of Metals (AREA)

Abstract

La présente invention concerne un procédé de production en continu d'aluminium à partir d'alumine. La première opération est la conversion d'alumine (Al2O3) en sulfure d'aluminium (Al2S3). La deuxième opération est la séparation, dans un réacteur, entre aluminium et sulfure d'aluminium. En l'occurrence, pour la première opération, on utilise un convertisseur donnant une solution d'alumine dans un sel fondu, donnant un produit fondu, un gaz soufré traversant le produit fondu où il fonctionne réactif convertissant au moins une partie de l'alumine en sulfure d'alumine. Une partie au moins du produit fondu sert pour la deuxième opération. L'invention concerne également un appareil pour la mise en oeuvre du procédé.
PCT/EP2006/002949 2005-03-31 2006-03-27 Procede et appareil de production d'aluminium Ceased WO2006103085A1 (fr)

Priority Applications (6)

Application Number Priority Date Filing Date Title
AU2006228730A AU2006228730B2 (en) 2005-03-31 2006-03-27 Method and apparatus for the production of aluminium
DE602006014108T DE602006014108D1 (de) 2005-03-31 2006-03-27 Verfahren und vorrichtung zur produktion von aluminium
EP06723909A EP1863953B1 (fr) 2005-03-31 2006-03-27 Procede et appareil de production d'aluminium
AT06723909T ATE466974T1 (de) 2005-03-31 2006-03-27 Verfahren und vorrichtung zur produktion von aluminium
CA2603095A CA2603095C (fr) 2005-03-31 2006-03-27 Procede et appareil de production d'aluminium
NO20075476A NO20075476L (no) 2005-03-31 2007-10-30 Fremgangsmate og apparat for fremstilling av aluminium

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP05075752 2005-03-31
EP05075752.5 2005-03-31

Publications (1)

Publication Number Publication Date
WO2006103085A1 true WO2006103085A1 (fr) 2006-10-05

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Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2006/002949 Ceased WO2006103085A1 (fr) 2005-03-31 2006-03-27 Procede et appareil de production d'aluminium

Country Status (7)

Country Link
EP (1) EP1863953B1 (fr)
AT (1) ATE466974T1 (fr)
AU (1) AU2006228730B2 (fr)
CA (1) CA2603095C (fr)
DE (1) DE602006014108D1 (fr)
NO (1) NO20075476L (fr)
WO (1) WO2006103085A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109321763B (zh) * 2018-11-06 2021-05-28 广东巨晨装备科技有限公司 一种铝熔炼设备

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB189523707A (en) * 1895-12-10 1896-06-13 Henry Spencer Blackmore Process for Producing, Decomposing, Converting, or Transforming Compounds, and Reducing Metallic Compounds so Generated to Metallic State.
US4265716A (en) * 1979-06-14 1981-05-05 The United States Of America As Represented By The United States Department Of Energy Method of winning aluminum metal from aluminous ore
WO2000037691A1 (fr) * 1998-12-18 2000-06-29 Corus Technology Bv Procede et appareil pour la production d'aluminium
WO2004088000A2 (fr) * 2003-03-31 2004-10-14 Corus Aluminium Walzprodukte Gmbh Procede d'electrolyse de sulfure d'aluminium

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB189523707A (en) * 1895-12-10 1896-06-13 Henry Spencer Blackmore Process for Producing, Decomposing, Converting, or Transforming Compounds, and Reducing Metallic Compounds so Generated to Metallic State.
US4265716A (en) * 1979-06-14 1981-05-05 The United States Of America As Represented By The United States Department Of Energy Method of winning aluminum metal from aluminous ore
WO2000037691A1 (fr) * 1998-12-18 2000-06-29 Corus Technology Bv Procede et appareil pour la production d'aluminium
WO2004088000A2 (fr) * 2003-03-31 2004-10-14 Corus Aluminium Walzprodukte Gmbh Procede d'electrolyse de sulfure d'aluminium

Also Published As

Publication number Publication date
CA2603095A1 (fr) 2006-10-05
NO20075476L (no) 2007-10-30
AU2006228730A1 (en) 2006-10-05
CA2603095C (fr) 2013-05-21
DE602006014108D1 (de) 2010-06-17
ATE466974T1 (de) 2010-05-15
AU2006228730B2 (en) 2010-07-29
EP1863953B1 (fr) 2010-05-05
EP1863953A1 (fr) 2007-12-12

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