AU2006228730B2

AU2006228730B2 - Method and apparatus for the production of aluminium

Info

Publication number: AU2006228730B2
Application number: AU2006228730A
Authority: AU
Inventors: Dietrich Willem Van Der Plas; Yanping Xiao
Original assignee: Aleris Aluminum Koblenz GmbH
Current assignee: Novelis Koblenz GmbH
Priority date: 2005-03-31
Filing date: 2006-03-27
Publication date: 2010-07-29
Anticipated expiration: 2026-03-27
Also published as: EP1863953A1; DE602006014108D1; ATE466974T1; CA2603095A1; WO2006103085A1; AU2006228730A1; CA2603095C; NO20075476L; EP1863953B1

Abstract

The invention relates to a method for the continuous production of aluminium from alumina comprising a first step of converting alumina (AI2O3) into aluminiumsulphide (AI2S3) and a second step of separation of aluminium from aluminiumsulphide in a separating reactor, 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 further the invention relates to an apparatus for operating the method.

Description

WO 2006/103085 PCT/EP2006/002949 Method and apparatus for the production of aluminium FIELD OF THE INVENTION The invention relates to a method for the continuous production of aluminium from alumina comprising a first step of converting alumina (A1 2 0 3 ) into aluminiumsulphide (Al 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. BACKGROUND OF THE INVENTION International publication WO-00/37691, incorporated herein by reference, discloses a method wherein in a first step, also called sulphidation step, solid alumina is converted into solid aluminiumsulphide (Al 2

S

3 ) by reacting with gaseous carbon sulphide. In a second step, also called separation step, the solid aluminiumsulphide is fed into a separating reactor such as an electrolysis cell wherein metallic aluminium is separated from the aluminiumsulfide. This has various drawbacks. One such drawback is that it requires two separate processes: the sulphidation step and further the separation step. As a consequence the aluminiumsulphide has to be transported from the reactor in which it is formed to the reactor in which the separation step is carried out. Aluminiumsulphide has a very high affinity to oxygen. Therefore, any oxygen with which the aluminiumsulphide comes into contact, e.g. as oxygen in air or in water, converts the aluminiumsulphide back into alumina. The known process therefore puts high demands on the handling of aluminiumsulphide. 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. Furthermore, 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. CONFIRMATION COPY 2 However, 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 5 aluminiumsulphide increase. A further drawback is that compounds from the separation step, in particular alumina, have to be discarded. The discussion of documents, acts, materials, devices, articles and the like is included in this specification solely for the purpose of providing a context for the present invention. It is not suggested or represented that any or all of these matters formed part 10 of the prior art base or were common general knowledge in the field relevant to the present invention as it existed before the priority date of each claim of this application. DESCRIPTION OF THE INVENTION. It is a preferred object of the present invention to provide a method for the 15 manufacture of aluminium, in particular primary aluminium, which has a higher efficiency of use of the alumina. It is another preferred object of the present invention to provide a method for the manufacture of aluminium, in particular primary aluminium, with which a higher conversion of alumina can be achieved. 20 It is yet another preferred object of the present invention to provide a method for the manufacture of aluminium, in particular primary aluminium, which requires fewer steps, preferably a method with which, the sulphidation and separation steps are at least partly integrated. It is a further preferred object of the present invention to provide a method for the 25 manufacture of primary aluminium, which avoids or at least reduces the problem associated with the handling of aluminiumsulphide. One or more of these objects are achieved with the method according to the invention for the continuous production of aluminium from alumina, the method comprising a first step of converting alumina (A1 2 0 3 ) into aluminiumsulphide (A1 2

S

3 ) and 30 a second step of separation of aluminium from aluminiumsulphide in a separating reactor, 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 35 the separating apparatus is a electrolysis cell, and whereby the melt with the dissolved 3 alumina and the aluminiumsulphide is continuously recirculated between the first and the second process step. For the purpose of this description the term "salt" also comprises a mixtures of salts, and the term "sulphur containing gas" comprises sulphides. 5 Throughout the description and claims of this specification, the word "comprise" and variations of the word, such as "comprising" and "comprises", is not intended to exclude other additives, components, integers or steps. The method according to an embodiment of the invention has one or more of the following advantages. The aluminiumsulphide formed is dissolved in the molten salt and 10 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 15 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 ?0 Hall-Heroult process for the reduction of alumina into metallic aluminium, which requires regular replacement of the consumable anodes. In the current invention, due to the reduced cell voltage, the carbon electrodes remain inert and can be used for a prolonged time. Another advantage of the process according to an embodiment of the invention 25 over the known prior art process is related to the thermal imbalance. The known sulphidation process is endothermic and requires heat input. In the separation process, on the other hand, heat is generated by ohmic losses. Integration of the two steps in accordance with the present invention enables a direct input of the heat generated by the separation process into the sulphidation reaction. Reference to the current Hall 30 Heroult process serves to illustrate this point, namely in modern Hall-Heroult cells, typically about 30% of the energy is dissipated as heat losses in the molten salt. As the bath temperature should remain constant, this heat must be dissipated to the surroundings. Apart from the loss of energy, the Hall-Heroult cell must be designed to dissipate heat, which obstructs more favourable compact cell designs. In the current 35 invention, substantially all the heat that is generated by ohmic losses is absorbed in the 4 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. 5 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 10 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. Another relevant characteristic is that the sulphidation reaction proceeds by direct 15 contact between the sulphidising gas and the melt. Thus 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, !0 similar to what is known from the regular Hall-Heroult process for the reduction of alumina. In this melt, A1 2 0 3 and A1 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 A1 2 0 3 and A1 2

S

3 . For simplicity, the words "alumina" and "aluminiumsulphide" that are used throughout this description refer to and include these 25 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 30 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.

4a A feature of an embodiment 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 5 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.

WO 2006/103085 PCT/EP2006/002949 5 An advantage is that the operating conditions in both the conversion reactor and in the separating reactor do not, or only to a small extent, vary in time. In the conversion reactor and in the separating reactor optimum conditions can be selected. Also there is no need to aim at a full conversion of alumina into aluminiumsulphide or a 5 full separation of alumina from the aluminiumsulphide. The method according to the invention is therefore carried out as a continuous process. Conversely, 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 10 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. As the anode is not consumed in the electrolysis of aluminiumsulphide, a multi 15 polar cell can be used 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. In a further embodiment according to the invention the electrolysis cell has a 20 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 25 vessel operating as a single reactor. In this embodiment 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. 30 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.

WO 2006/103085 PCT/EP2006/002949 6 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. In an embodiment the sulphur containing gas is substantially carbondisulphide 5 (CS 2 ). Another embodiment of the method of the invention is characterized in that the molten salt substantially comprises chloride salts, and preferably a mixture of NaCl and KCl. In particular NaCI and KCl are relatively inexpensive, its mixture, more in particular the eutectic composition, has a suitable melting point, a low vapour pressure 10 in the proposed operational window of the process, and they are harmless under regular operating conditions. Preferably the composition of the molten salt comprises in the range of between 30 and 70 wt.% NaCl and in the range of between 70 and 30 wt.% KCl. A further embodiment of the method of the invention is characterized in that the 15 melt of salt comprises a fluorine containing compound. The suitable fluorine containing compound may include one or more compounds having a molecular formula NaaAIFa+ 3 and/or KaAIFa+ 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 20 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. In a preferred embodiment fused sodium aluminiumfluoride, commonly called 25 cryolite, or a mixture of cryolite and other fluorides is used. Tests have shown that addition of fluorine containing compounds, such as cryolite, to the molten salt has a very beneficial effect on the current density in an electrolyses cell at a given cell potential. An increase of a factor three or more as compared to a molten salt without cryolite, is achievable. 30 Although not intended to be bound to any particular mechanism, it is assumed that for, an efficient conversion of alumina into aluminiumsulphide, carbon and sulphur are required as reactants. Carbondisulphide contains both these elements and its manufacture and processing is based on proven technology. Furthermore, carbondisulphide is a gas at the operational conditions, thus facilitating the contact WO 2006/103085 PCT/EP2006/002949 7 between the reactants. Carbondisulphide is also a compound that is substantially free of oxygen, as required for a good conversion as explained above. Preferably the melt of salt is substantially free of alkaline earth metals or compounds thereof. 5 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. Preferably the conversion reactor is a bubble column wherein the sulphide containing gas is fed into the lower portion thereof thereby forming bubbles which rise 10 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 15 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 20 complexity of the total plant for the production of primary aluminium. In a preferred embodiment 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 25 characterized in that the conversion of alumina into aluminiumsulphide is carried out at a temperature in a range of between 7000C and 11000C, preferably in a range of between 8000C and 1 000*C, more preferably in a range of between 8000C and 900*C. Tests have shown that the conversion of alumina into aluminiumsulphide proceeds faster at higher temperature. However, it has also been found that for an 30 efficient conversion y-alumina is being preferred. At temperature above about 1100*C, V-alumina transforms to a-alumina at a high rate. Therefore the temperature at which the conversion is carried out is preferably chosen below about 11000C, more preferably below about 10000C and even more preferably below about 900*C.

WO 2006/103085 PCT/EP2006/002949 8 On the other hand, to have a sufficiently high conversion rate, the temperature at which the conversion is done is preferably chosen above about 7000C, more preferably above 8000C. Preferably the sulphidation process is carried out at a pressure above 5 atmospheric pressure, preferably at a pressure above 2 bar, and more preferably at a pressure of 3 bar or more. Tests have shown that the conversion rate of alumina into aluminiumsulfide increases with the partial pressure of the sulphide containing gas. Therefore it is preferred to execute the method at above atmosphere pressure in 10 the conversion reactor. 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 15 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. Advantageously, 20 use can be made of the lifting effect of the rising bubbles to convey aluminiumsulphide to the electrolysis cell. For transport of molten salt from the bubble column to the electrolysis cell and in reverse direction, ducts are provided. 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. 25 BRIEF DESCRIPTION OF THE DRAWINGS The invention will now be illustrated with reference to a non-limiting embodiment according to the drawings in which: Fig. 1 shows a basic diagram of an apparatus for the production of aluminium for 30 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; WO 2006/103085 PCT/EP2006/002949 9 Fig. 4 shows the effect of the temperature (in '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 %). 5 DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS In Fig. 1 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. Through 10 supply line 4 a sulphur and carbon containing gas, such as CS2, is fed to the bottom portion of the conversion reactor 1. In the conversion reactor, alumina is dissolved in the molten salt and converted into aluminiumsulphide. A two phase flow of bubbles, containing gaseous reagents and reaction products, dispersed in a liquid containing the molten salt, aluminiumsulphide and 15 unconverted alumina, rises in the conversion reactor 1 and lifts the liquid to the first transfer duct 5 through which the components are conveyed to the separating reactor 6, here in the form of a multi-pole electrolysis cell. In the multi-pole electrolysis cell, 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 20 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. Thus the gas lift in the bubble column provides a driving force for the recirculation of the melt between the sulphidation and the separation reactor. Thus no external agents like pumps may be required. 25 Components present in the separating reactor 6 are fed back into the conversion reactor I 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, first transfer duct 5, separating reactor 6 and second 30 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 35 10 to the carbondisulphide plant 11. To this carbondisulphide plant 11 also reaction WO 2006/103085 PCT/EP2006/002949 10 products or unreacted reactants from the conversion process, such as COS, CS2 and S2 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 5 carbondisulphide plant 11 through carbon supply line 14. Through the energy, dissipated in the electrolysis cell, 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. As a typical value, a temperature rise from 7900C to 8000C can be mentioned. 10 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. 15 EXAMPLES 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 20 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. In this experiment gamma alumina was added to a salt mixture containing a 25 eutectic composition of NaCl and KCl, and to which 10 wt.% of cryolite was added. The salt mixture was preheated to 8500C under argon atmosphere, and at t=0 a mixture of argon and CS2 was supplied through a tube injected into the salt mixture from the top. The experiment was carried out at atmospheric pressure, the CS 2 partial pressure being about 0.70 bar. As can be seen, increase of reaction time has a 30 positive effect on the conversion ratio. However, the conversion rate (amount of alumina converted per unit of time) remains substantially constant. This facilitates the tuning of the process towards its most efficient operational window, and reduces possible transient effects that may occur, for instance, during start up or as a consequence of changes in the alumina content of the melt.

WO 2006/103085 PCT/EP2006/002949 11 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 5 800 0 C and about 1000"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 2. This graph shows that considerable advantages can be achieved by operating the 10 conversion reactor at a pressure above atmospheric pressure. Having now fully described the invention, it will be apparent to one of ordinary skill in the art that many changes and modifications can be made without departing from the spirit or scope of the invention as herein described. 15

Claims

1. Method for the continuous production of aluminium from alumina, the method comprising a first step of converting alumina (A1 2 0 3 ) into aluminiumsulphide 5 (A1 2 S 3 ) and a second step of separation of aluminium from aluminiumsulphide in a separating reactor, 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 10 used in the second step, and wherein the separating apparatus is a electrolysis cell, and whereby the melt with the dissolved alumina and the aluminiumsulphide is continuously recirculated between the first and the second process step.

2. Method according to claim 1, wherein the separating apparatus is a multi-pole 15 electrolysis cell.

3. Method according to any one of the preceding claims, wherein the first step and the second step are performed in a reactor vessel operating as a single reactor. 20

4. Method according to any one of the preceding claims, wherein the sulphur containing gas is substantially carbondisulphide.

5. Method according to any one of the preceding claims, wherein the molten salt substantially comprises chloride salts, preferably a mixture of NaCl and KCl. 25

6. Method according to any of the preceding claims, wherein the melt of salt comprises a fluorine containing compound, and preferably cryolite.

7. Method according to any one of the preceding claims, wherein the melt of salt is 30 substantially free of alkaline earth metals or compounds thereof.

8. Method according to any one of the preceding claims, wherein 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. 35 WO 2006/103085 PCT/EP2006/002949 13

9. Method according to claim 8, wherein the bubbles rising in the bubble column are used to transport at least part of the aluminiumsulphide containing melt to the separating apparatus. 5

10. Method according to claim 9, wherein 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.

11. Method according to any one of the preceding claims, wherein the conversion of 10 alumina into aluminiumsulphide is carried out at a temperature in a range of between 7000C and 11000C, preferably in a range of between 800 0 C and 1000 C, more preferably in a range of between 8000C and 9000C.

12. Method according to any one of the preceding claims, wherein the sulphidation 15 process is carried out at a pressure above atmospheric pressure, and preferably at a pressure of 3 bar or more.

13. Apparatus for the use with a method according to any one of the preceding claims comprising: 20 a bubble column suitable for converting alumina into aluminiumsulphide by a gaseous sulphur containing compound, a feeder for feeding the gaseous sulphur containing compound into the bottom portion of the bubble column, an electrolysis cell, 25 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. 30 14

14. Method for the continuous production of aluminium from alumina substantially as hereinbefore described with reference to the accompanying Figures and/or Examples. 5

15. Apparatus according to claim 13 substantially as hereinbefore described with reference to accompanying Figures and/or Examples.