EP1807552A2 - Extraction electrolytique d'aluminium avec circulation d'electrolyte amelioree - Google Patents

Extraction electrolytique d'aluminium avec circulation d'electrolyte amelioree

Info

Publication number
EP1807552A2
EP1807552A2 EP05800288A EP05800288A EP1807552A2 EP 1807552 A2 EP1807552 A2 EP 1807552A2 EP 05800288 A EP05800288 A EP 05800288A EP 05800288 A EP05800288 A EP 05800288A EP 1807552 A2 EP1807552 A2 EP 1807552A2
Authority
EP
European Patent Office
Prior art keywords
anode
stems
electrolyte
foraminate
alumina
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Withdrawn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
EP05800288A
Other languages
German (de)
English (en)
Inventor
Vittorio De Nora
Thinh T. Nguyen
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.)
Moltech Invent SA
Original Assignee
Moltech Invent SA
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 Moltech Invent SA filed Critical Moltech Invent SA
Publication of EP1807552A2 publication Critical patent/EP1807552A2/fr
Withdrawn legal-status Critical Current

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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
    • C25C3/08—Cell construction, e.g. bottoms, walls, cathodes
    • C25C3/12—Anodes

Definitions

  • This invention relates to electrowinning aluminium in a cell having foraminate metal-based anodes which permit an improved electrolyte circulation.
  • the invention also relates to such a cell and to the anode.
  • the technology for the production of aluminium by the electrolysis of alumina, dissolved in molten cryolite, at temperatures around 950 0 C is more than one hundred years old and still uses carbon anodes and cathodes.
  • US Patent 4,614,569 (Duruz/Derivaz/Debely/ Adorian) describes metal anodes for aluminium electrowinning coated with a protective coating of cerium oxyfluoride, formed in-situ in the cell or pre-applied, this coating being maintained during electrolysis by the addition of small amounts of a cerium compound to the molten cryolite electrolyte so as to protect the surface of the anode from the electrolyte attack.
  • US Patent 4,681,671 discloses vertical anode plates or blades operated in low temperature aluminium electrowinning cells.
  • US Patent 5,310,476 discloses oxygen-evolving anodes consisting of roof-like assembled pairs of anode plates.
  • US Patent 5,362,366 describes non- consumable anode shapes including roof-like assembled pairs of anode plates.
  • US Patent 5,368,702 discloses vertical tubular or frustoconical oxygen-evolving anodes for multimonopolar aluminium cells.
  • US Patent 5,683,559 describes an aluminium electrowinning cell with oxygen- evolving bent anode plates which are aligned in a roof- like configuration facing correspondingly shaped cathodes.
  • US Patent 5,725,744 discloses vertical oxygen- evolving anode plates, preferably porous or reticulated, in a multimonopolar ' cell arrangement for aluminium electrowinning cells operating at reduced temperature.
  • WO00/40781 and WO00/40782 both de Nora both disclose aluminium production anodes with a series of parallel spaced-apart elongated anode members which are electrochemically active for the oxidation of oxygen.
  • Various anodes are disclosed, in particular WO00/40782 discloses an anode with a rectangular anode-member arrangement which is held by two spaced-apart large feet, each foot being integral with a large anode stem and located towards one end of the anode-member arrangement.
  • a main object of the present invention is to enhance the circulation of electrolyte in an aluminium electrowinning cell having foraminate metal-based anodes and the dissolution of alumina by using a new cell configuration.
  • the invention is concerned with the flow of the electrolyte resulting inter-alia from the shape and configuration of the anode.
  • foraminate anode bodies instead of having foraminate anode bodies that are suspended usually from their centre by- large prior art anode stems, foraminate anode bodies are suspended by a greater number of anode stems, preferably of smaller size, which are distributed around a central part of the anode and which do not significantly interfere with the electrolyte upflow.
  • the electrolyte can flow up through substantially the entire foraminate anode body and this upflow is not weakened by being diverted into a multitude of different directions from below a large main anode stem.
  • a strong electrolyte circulation is produced and electrolyte circulates from and to substantially the entire active anode surface which is substantially uniformly operative for the oxidation of oxygen.
  • the present invention relates to a method of operating an aluminium electrowinning cell.
  • the cell has one or more metal-based anodes that comprise metal-based foraminate anode bodies which are suspended by metal- based anode stems in a molten electrolyte and which are spaced above a cathode.
  • the method comprises electrolysing alumina dissolved in the molten electrolyte by passing current via the anode stems and the or each anode body through the electrolyte to the facing cathode whereby aluminium is cathodically produced and gas is anodically evolved.
  • the evolved gas promotes an electrolyte circulation through the or each foraminate anode body to facilitate dissolution of alumina fed thereabove.
  • the or each anode has a foraminate anode body suspended by at least three anode stems that are spaced apart from one another and distributed around a foraminate stemless central part of the anode body. These stems extend from the anode body to above the molten electrolyte. Electrolyte flows up through and above this foraminate central part to enhance dissolution of alumina.
  • the anode of the present invention has at least three anode stems that are located around a central part of the foraminate anode body and are so dimensioned and positioned as to minimise interferences with the electrolyte upflow through and above the central part and generally through and above substantially the entire anode body.
  • Such a circulation also permits the supply of alumina-rich electrolyte to substantially the entire active anode surface so that electrolysis takes place over substantially the entire active anode surface, i.e. without having significant areas of the active anode surface that remain inoperative for lack of electrolyte circulation to and from these active areas.
  • the alumina is preferably supplied to the electrolyte between the stems of at least one anode vertically above the central part of the anode body directly into the electrolyte main flow to maximise dissolution of the alumina due to the electrolyte's stirring effect.
  • the cathode can be aluminium-wettable.
  • the product molten aluminium can be drained on the cathode.
  • Various aluminium-wettable cathodes and drained cathodes have been disclosed in the prior art which can be used for this invention.
  • Another aspect of the invention relates to an aluminium electrowinning cell having one or more metal- based anodes that comprise metal-based foraminate anode bodies which are suspended by metal-based anode stems in an alumina-containing molten electrolyte and which are spaced above a cathode.
  • This cell is arranged so as to permit an electrolyte circulation promoted by anodically evolved gas through the or each foraminate anode body to facilitate dissolution of alumina in the electrolyte fed thereabove.
  • the or each anode has a foraminate anode body- suspended by at least three anode stems that are spaced apart from one another and distributed around a foraminate stemless central part of the anode body. These stems extend from the anode body to above the molten electrolyte so as to permit an upflow of electrolyte through and above the foraminate central part to enhance dissolution of alumina.
  • the anode has a metal-based active surface, in particular an oxide surface that can for example contain at least one iron, cobalt, nickel and copper.
  • the active surface is made predominantly of cobalt oxide CoO which provides the advantages described below.
  • the anode stems of one anode can be connected together by cross-members.
  • the cell has a cover above the electrolyte.
  • the cover can be an insulating cover, in particular for cell operation with a substantially crustless and/or ledgeless molten electrolyte. Covers and materials are disclosed in US 6,402,928, WO02/070784 and WO03/102274 (all assigned to MOLTECH Invent S.A.) .
  • the anode stems of one anode can be connected together by cross-members above or below the insulating cover.
  • the cross-members can be joined to a main current conductor (or main stem) that is connected to an anode bus bar.
  • the bus bar is usually part of the cell superstructure located above the cell cover.
  • Such a main conductor should be located outside the electrolyte circulation to avoid interference therewith, for example this conductor can be located above the electrolyte.
  • the alumina-containing electrolyte is a fluoride-based electrolyte, in particular an electrolyte containing predominantly aluminium fluoride and sodium fluoride.
  • a further aspect of the invention relates to an aluminium electrowinning metal-based anode for use in a cell as described above.
  • the anode comprises a metal- based foraminate anode body and metal-based anode stems which are connected to the anode body.
  • the or each anode has a foraminate anode body connected by at least three of said anode stems that are spaced apart from one another and distributed around a foraminate stemless central part of the anode body. These stems extend during use from the anode body to above the molten electrolyte so as to permit an upflow of electrolyte through and above this foraminate central part to enhance dissolution of alumina.
  • anode stems can be connected to an anode body, in particular four to six stems.
  • the anode body has a grid-like or plate- like foraminate structure that is parallel to the facing cathode.
  • Examples of such anode bodies are disclosed in WO00/40781, WO00/40782 and WO03/006716 (all assigned to MOLTECH Invent S.A.) .
  • the anode body has an upper face to which the stems are connected around a central point of the upper face.
  • Each anode stem can be located at a distance from the central point which is in the range of 1/4 to 3/4 of the length of a segment of a line extending from the central point to a side of the face and intercepting the anode stem, in particular 1/3 to 2/3 of said length.
  • the anodes stems are preferably positioned on the anode bodies taking into account the current distribution in the anode bodies during use so as to optimise this distribution.
  • the anode body has polygonal, in particular a square or rectangular upper face.
  • the anode body is suspended by four anode stems. These stems can be generally located on crossing diagonals of the body's upper face, each stem being located generally on the upper face about half way between a corner of the body's face and the crossing point of the diagonals.
  • the rectangular or square upper face can be notionalIy divided into four equal rectangular or square quadrants in the middle of which an anode stem is connected to the anode body.
  • These four stems may be generally located substantially on crossing perpendicular median lines of the body's upper face, each stem being connected about half way between a side of the body' s face and the crossing point of the median lines.
  • an anode body has a generally circular upper face.
  • the upper face can be generally elliptic.
  • the upper face may be connected to four stems evenly distributed around the body's central part. Each stem can be located substantially in the middle of a radius of the circular upper face.
  • the anode stems have ends away from the anode body that are connected together by cross-members .
  • the anode can have pairs of opposite stems that are connected by intercepting cross-members.
  • the anode has four stems that are connected by two cross-members that form an "X" or three cross- members that form an "H” .
  • the cross-members can be joined to a main current conductor for connection to a busbar.
  • the anode stems connected to the anode body have a sufficient transverse cross-sectional area for passing a current that leads to a current density in the range of 0.5 to 1.5 A/cm 2 near the surface of the anode body with a voltage drop along the anode stems below 80 mV/cm, in particular in the range of 20 to 50 mV/cm.
  • the total voltage drop along the stems can be of the order of 0.2 to 0.5 V.
  • the anode body can have an active surface that has a total projected surface area AA and the anode stems connected to the anode body have a cumulated transverse cross-sectional area AS (equal to the sum of the transverse cross-sectional area of the individual anode stems) , the area AS corresponding to a fraction of the area AA which is in the range of 0.1% to 2% of the area AA, in particular 1 to 1.5%.
  • each anode stem may be in the range of 2 to 8 cm, in particular 2.5 to 6 cm, such as 3 to 4 cm. This is significantly smaller than the usual diameter of anode stems, which is typically 10-15 cm.
  • the anode body has an active face that usually has a total projected surface area in the range of 0.2 to 2 m 2 , in particular 0.5 to 1.5 m 2 .
  • the total projected surface area mentioned above refers to the overall active surface without deduction of the holes present at the surface due to the fact that the anode body is foraminate.
  • the active anode surface can be made of any prior art non-carbon materials, in particular metal-based materials such as materials containing at least one of iron, nickel and cobalt and oxides thereof.
  • metal-based materials such as materials containing at least one of iron, nickel and cobalt and oxides thereof.
  • the anode's active surface can be made of the materials disclosed in any of the following publications: WO99/36591 and WO99/36592, WO99/36593 and W099/36594,
  • FIG. 1 is a perspective view of an anode body of an anode according to the invention
  • Figure 1 shows an anode body 10 of an anode according to the invention.
  • the anode body 10 has a generally rectangular upper face and comprises a series of parallel spaced apart anode members 11 that have a generally pentagonal cross-section with a tapered upper part for guiding an electrolyte circulation.
  • suitable anode members 11 are disclosed in WO03/006717
  • the anode members 11 are connected by two end-members 12 and two intermediate cross-members 13 as shown in Fig. 1.
  • the anode body 10 has in the cross-members 13 four sockets 15 each with an opening 16 for receiving anode stems (not shown) .
  • An anode stem can be screwed, force- fitted or welded into opening 16.
  • an anode stem can be made integral with the cross-member 13.
  • Each socket 15 is located in the middle of a notional quadrant delimited by dashed lines A and B which divide the upper face of the anode body into four equal quadrants.
  • each socket 15 is located on a diagonal of the body's upper face, half way between a corner of the upper face and the intersection of the diagonals (which coincides with the intersection of dashed lines A and B) .
  • Sockets 15 are joined to cross- members 13 which permits a better current distribution from anode stems and sockets 15 to anode members 11.
  • the anode body 10 has a total length of 65 cm along the direction of the anode members 11 and a total width of 61 cm across the direction of the anode members.
  • Each anode member 11 has a width of 20 mm and a height of 25 mm.
  • the anode members are spaced apart by inter-member gaps of 20 mm.
  • the total projected active bottom surface of the anode body (without deduction of the inter-member gaps) is about 65 cm x 61 cm, i.e. approximately 0.4 m 2 .
  • Each socket 15 has an outer diameter 60 mm and the opening 16 has a diameter of 40 mm. This opening can receive an anode stem whose lower end has a corresponding diameter, i.e. 40 mm.
  • the remaining part of the anode stems can have the same diameter or a different diameter, in particular a larger diameter. However, the diameter of this remaining part should not be too large, in any case no larger than the outer diameter of socket 15, in order to avoid noticeable interference of the anode stems with upflowing electrolyte during operation in a cell.
  • sockets 15 and the corresponding anode stems are significantly smaller than prior art central anode stems which have a typical diameter of the order of 120 mm.
  • the cross members 13 have a width of
  • Figs 2 to 5 show schematically plan views of anodes 5 having variations of the anode body shown in Fig. 1.
  • the anode bodies 10 of Figs 2 & 3 have a circular shape. These anode bodies 10 can be made up of concentric circular anode members connected by radial cross-members
  • the anode body 11 shown in Fig. 2 is suspended by four anode stems 20, each stem 20 being usually joined to or integral with a radial cross-member.
  • Anode stems 20 are located on a radial cross-member and spread around the centre of the anode body 11.
  • the anode body 11 shown in Fig. 3 is suspended by three anode stems 20, each stem 20 being located close to the middle of a radial cross-member.
  • Fig. 2 indicates in dotted lines intercepting members 23 for connecting anode stems 20 above the anode as explained in Figs 6 and 7.
  • the anode bodies 11 of Figs. 4 and 5 have a square shape.
  • Four anode stems 20 are located on median lines A and B to the anode body 11 of Fig. 4.
  • Six anode stems 20 are located on median line A and diagonals C and D in
  • Figure 6 shows in cross-sectional view a drained- cathode aluminium electrowinning cell with two different anodes 5.
  • the cell has a carbon cathode 30 with an inclined aluminium-wettable drained cathode surface 31 and an aluminium collection reservoir 35.
  • the surface of the carbon cathode can be made wettable by applying thereto a layer of aluminium-wettable material, in particular a titanium diboride coating as for example disclosed in WO02/096831 (in the name of MOLTECH Invent S.A.) .
  • collector bars 37 that are usually made of steel.
  • the drained cathode surface 31 is covered with a thin layer of product aluminium 60.
  • the cell has sidewalls 40 which are made of or covered with a material resistant to molten electrolyte, such as silicon carbide or fused alumina or aluminium- wetted porous aluminium as disclosed in WO02/070783 (de Nora) .
  • Sidewall 40 is lined with an insulating material 41 in steel shell 42.
  • Sidewalls 40 are joined to cathode 30 by a body 43 of solidified ramming paste.
  • the cell is covered with an insulating cover 45 which can be of the type disclosed in US 6,402,928, WO02/070784 and WO03/102274 (all assigned to MOLTECH Invent S .A. ) .
  • the cell contains an electrolyte 50 and has a sufficient insulation 36,41,45 to maintain electrolyte 50 in a molten state substantially without crust or ledge.
  • a suitable molten electrolyte can be at a temperature below 950 0 C, in particular in the range from 910° to 94O 0 C, and consist of: - 6.5 to 11 weight% dissolved alumina, in particular 7 to 10 weight%; - 35 to 44 weight% aluminium fluoride, in particular 36 to 42 weight% aluminium fluoride, such as 36 to 38 weight; - 38 to 46 weight% sodium fluoride, in particular 39 to 43 weight%;
  • weight% potassium fluoride in particular 3 to 10 weight% potassium fluoride, such as 5 to 7 weight%; - 0 to 5 weight% calcium fluoride, in particular 2 to 4 weight% calcium fluoride; and
  • the presence in the electrolyte of potassium fluoride in the above amount has two effects. On the one hand, it leads to a reduction of the operating temperature by up to several tens of degrees without increase of the electrolyte's aluminium fluoride content or even a reduction thereof compared to standard electrolytes operating at about 950 0 C with an aluminium fluoride content of about 45 weight%. On the other hand, it maintains a high solubility of alumina, i.e. up to above about 8 or 9 weight%, in the electrolyte even though the temperature of the electrolyte is reduced compared to conventional temperature.
  • basic fluorine-poor aluminium oxyfluoride ions do not significantly dissolve the anode's surface, in particular when made of predominantly of cobalt or nickel oxide, and do not noticeably passivate or corrode the anode's metals, in particular metallic cobalt or nickel.
  • the weight ratio of dissolved alumina/aluminium fluoride in the electrolyte should be above 1/7, and often above 1/6 or even above 1/5, to obtain a favourable ratio of the fluorine-poor aluminium oxyfluoride ions and the fluorine-rich aluminium oxyfluoride ions .
  • the electrolyte may for example consist of: 7 to 10 weight% dissolved alumina; 36 to 42 weight% aluminium fluoride, in particular 36 to 38 weight%; 39 to 43 weight% sodium fluoride; 3 to 10 weight% potassium fluoride, such as 5 to 7 weight%; 2 to 4 weight% calcium fluoride; and 0 to 3 weight% in total of one or more further constituents.
  • AlF 3 aluminium fluoride
  • the electrolyte can contain as further constituent (s) at least one fluoride selected from magnesium fluoride, lithium fluoride, cesium fluoride, rubidium fluoride, strontium fluoride, barium fluoride and cerium fluoride.
  • at least one fluoride selected from magnesium fluoride, lithium fluoride, cesium fluoride, rubidium fluoride, strontium fluoride, barium fluoride and cerium fluoride.
  • the electrolyte contains alumina at a concentration near saturation on the active anode surface.
  • the cell is preferably fitted with means to monitor and adjust the electrolyte's alumina content.
  • drained-cathode cell trough 30,36,37,40,41,42,43 shown in Fig. 6 and suitable variations are disclosed in greater detail in the prior art, in particular in US patents 6,682,643, 6,692,620 and 6,783,656, and in WO02/070783, WO02/070785, WO02/097168 and WO02/097169 (all assigned to MOLTECH Invent S.A.) .
  • the cell has anodes 5 with a foraminate anode body 10 that is suspended by four anode stems 20 distributed around a foraminate stemless central part of the anode body and that is held above the cathode 30 parallel to the drained cathode surface 31.
  • the anode bodies 10 are in particular of the type shown in Fig. 1.
  • Anode stems 20 of each anode 5 are connected by cross-members 23 to a main current conductor 25.
  • anodes 5 have an active surface with an enhanced stability against corrosion by the highly aggressive circulating electrolyte and/or against oxidation by anodically evolved oxygen, the enhanced stability being provided by a layer that contains predominantly cobalt oxide CoO.
  • Such a composition is particularly suitable for anodes 5 of the invention which during use are exposed to a strong central electrolyte circulation.
  • CoO-containing layer can be a layer made of sintered particles, especially sintered CoO particles.
  • the CoO-containing layer may be an integral oxide layer on a Co-containing metallic layer or anode core. Tests have shown that integral oxide layers have a higher density than sintered layers and are thus preferred to inhibit oxygen diffusion.
  • CoO When CoO is to be formed by oxidising metallic cobalt, care should be taken to carry out a treatment that will indeed result in the formation of CoO. It was found that using Co 2 O 3 or Co 3 O 4 in a known aluminium electrowinning electrolyte does not lead to an appropriate conversion of these forms of cobalt oxide into CoO. Therefore, it is important to provide an anode with the CoO layer before the anode is used in an aluminium electrowinning electrolyte.
  • CoO on the metallic cobalt is preferably controlled so as to produce a coherent and substantially crack-free oxide layer.
  • any treatment of metallic cobalt at a temperature above 895 0 C or 900 0 C in an oxygen-containing atmosphere will result in optimal coherent and substantially crack-free CoO layer that offers better electrochemical properties than a Co 2 0 3 /Co 3 0 4 .
  • the temperature for treating the metallic cobalt to form CoO by air oxidation of metallic cobalt is increased at an insufficient rate, e.g. less than 200°C/hour, a thick oxide layer rich in Co 3 O 4 and in glassy Co 2 O 3 is formed at the surface of the metallic cobalt.
  • a layer does not permit optimal formation of the CoO layer by conversion at a temperature above 895 0 C of Co 2 O 3 and Co 3 O 4 into CoO.
  • a layer of CoO resulting from such conversion is not preferred but still useful despite an increased porosity and may be cracked. Therefore, the required temperature for air oxidation, i.e.
  • At least 92O 0 C or preferably above 940 0 C should be attained sufficiently quickly, e.g. at a rate of increase of the temperature of at least 300 0 C or 600 0 C per hour to obtain an optimal CoO layer.
  • the metallic cobalt may also be placed into an oven that is pre-heated at the desired temperature above 900 0 C.
  • the cooling down should be carried out sufficiently fast, for example by placing the anode in air at room temperature, to avoid significant formation of Co 3 O 4 that could occur during the cooling, for instance in an oven that is switched off.
  • An anode with a CoO layer obtained by slow heating of the metallic cobalt in an oxidising environment will not have optimal properties but still provides better results during cell operation than an anode having a
  • Co 2 O 3 -Co 3 O 4 layer and therefore also constitutes an improved aluminium electrowinning anode according to the invention.
  • the section of main current conductor 25 shown in Fig. 6 corresponds to the section of prior art stems whereas the section of anode stems 20 is a fraction of the section of conductor 25, usually about the size of the section of the conductor 25 divided by the number of anode stems 20 connecting each anode body 10.
  • anode stems 20 extend through cell cover 45 and are connected by cross- members 23 above cover 45.
  • anode stems 20 are connected to cross-members 23 below cover 45.
  • the connection can be achieved by screwing, welding or force-fitting.
  • the anode stems are integral with cross-members.
  • dissolved alumina is electrolysed between anode bodies 10 and cathode 30 to produce aluminium 60 cathodically and oxygen anodically.
  • the oxygen released at the anode body 10 promotes an electrolyte upflow in the direction of arrow 51 through anode body 10. This upflow is strongest through and above the central part of anode body 10.
  • electrolyte can circulate through substantially the entire anode body 10 and is electrolysed over the entire active surface of anode body 10.
  • the main current conductor 25 being located above electrolyte 50, it does not interfere with this electrolyte circulation.
  • Alumina is fed to the electrolyte 50 vertically above the central part of each anode body 10 between anode members 20 of each anode 5 where the stirring effect of the electrolyte is highest .
  • the alumina dissolves as it enters the electrolyte and is circulated with the electrolyte 50 to the gap spacing the anode body 10 and cathode 30 mainly around anode body 10 and is electrolysed substantially uniformly under anode body 10.
  • Figure 7 shows a variation of the cell shown in Fig. 6.
  • the cell operates with a shallow aluminium pool 60 on a horizontal cathode 30.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Electrolytic Production Of Metals (AREA)

Abstract

L'invention concerne un procédé permettant de faire fonctionner une cellule d'extraction électrolytique d'aluminium possédant au moins une anode a base de métal (5) . La ou les anodes (5) comprennent des corps d'anode (10) perforés à base de métal suspendus par des tiges d'anode (20) à base de métal dans un électrolyte fondu (50) et espacés au-dessus d'une cathode (30). Ce procédé consiste à électrolyser de l'alumine dissoute dans l'électrolyte fondu (50) en faisant passer du courant par l'intermédiaire des tiges d'anode (20) et des corps d'anode (10) à travers l'électrolyte (50) vers la cathode opposée (30), l'aluminium (60) étant produit par voie cathodique et du gaz étant émis par voie anodique. Le gaz promeut une circulation électrolytique (51) à travers les corps d'anode perforés (10), ce qui facilite la dissolution de l'alumine. Chaque anode (5) possède un corps d'anode perforé (10) suspendu au moyen d'au moins trois tiges d'anode (20) espacées les unes des autres et distribuées autour d'une partie centrale dépourvue de tige perforée du corps d'anode (10). Ces tiges s'étendent du corps d'anode (10) au-dessus de l'électrolyte fondu (50), l'électrolyte (50) coulant à travers et au-dessus de la partie centrale perforée du corps d'anode (10) pour améliorer la dissolution de l'alumine amenée.
EP05800288A 2004-11-05 2005-10-24 Extraction electrolytique d'aluminium avec circulation d'electrolyte amelioree Withdrawn EP1807552A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IB2004003642 2004-11-05
PCT/IB2005/053466 WO2006048790A2 (fr) 2004-11-05 2005-10-24 Extraction electrolytique d'aluminium avec circulation d'electrolyte amelioree

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EP1807552A2 true EP1807552A2 (fr) 2007-07-18

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EP (1) EP1807552A2 (fr)
AU (1) AU2005300270A1 (fr)
CA (1) CA2584064A1 (fr)
RU (1) RU2007120813A (fr)
WO (1) WO2006048790A2 (fr)

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CN103630101B (zh) * 2013-11-07 2016-07-06 中国铝业股份有限公司 一种在线测量电解槽阳极厚度的方法

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WO2000040782A1 (fr) * 1999-01-08 2000-07-13 Moltech Invent S.A. Cellules d'extraction electrolytique de l'aluminium pourvues d'anodes a emission d'oxygene
NO20024048D0 (no) * 2002-08-23 2002-08-23 Norsk Hydro As Fremgangsmåte for drift av en elektrolysecelle samt midler for samme

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AU2005300270A1 (en) 2006-05-11
WO2006048790A3 (fr) 2007-02-08
RU2007120813A (ru) 2008-12-10
WO2006048790A2 (fr) 2006-05-11
CA2584064A1 (fr) 2006-05-11

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