EP1534879B1 - Verfahren und vorrichtung zur verminderung von sulfur verunreinungen und verbesserung der stromleistung in aluminium-elektrolysezellen mit inerten anoden - Google Patents

Verfahren und vorrichtung zur verminderung von sulfur verunreinungen und verbesserung der stromleistung in aluminium-elektrolysezellen mit inerten anoden Download PDF

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Publication number
EP1534879B1
EP1534879B1 EP02807650.3A EP02807650A EP1534879B1 EP 1534879 B1 EP1534879 B1 EP 1534879B1 EP 02807650 A EP02807650 A EP 02807650A EP 1534879 B1 EP1534879 B1 EP 1534879B1
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Prior art keywords
cell
sulfur
bath
aluminum
inert anode
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French (fr)
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EP1534879A1 (de
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Alfred F. Lacamera
Siba P. Ray
Xinghua Liu
Robert L. Kozarek
Jerry L. Roddy
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Alcoa Corp
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Alcoa Corp
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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

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  • the present invention relates to the operation of electrolytic aluminum production cells. More particularly, the invention relates to the reduction of sulfur impurities in inert anode aluminum production cells in order to increase current efficiencies of the cells.
  • Aluminum is conventionally produced in electrolytic reduction cells or smelting pots which include an electrolytic bath comprising molten aluminum fluoride, sodium fluoride and alumina, a cathode, and consumable carbon anodes.
  • the energy and cost efficiency of aluminum smelting can be significantly reduced with the use of inert, non-consumable and dimensionally stable anodes.
  • Replacement of traditional consumable carbon anodes with inert anodes allows a highly productive cell design to be utilized, and may provide environmental benefits because inert anodes produce essentially no CO 2 or CF 4 .
  • Some examples of inert anode compositions comprising nickel ferrite-based ceramic materials and/or metal alloys are provided in U.S. Patent Nos. 5,794,112 , 5,865,980 , 6,126,799 , 6,217,739 , 6,332,969 , 6,372,119 , 6,416,649 , 6,423,195 and 6,423,204 .
  • sulfur, iron, nickel, vanadium, titanium and phosphorous may build up in the electrolytic bath.
  • sulfur species can build to higher concentrations in the bath because it is no longer removed as COS or other sulfur-containing species as in consumable carbon anode cells.
  • the presence of sulfur or other multi-valence elemental impurities in the bath causes unwanted redox reactions which consume electrical current without producing aluminum.
  • Such impurities can significantly reduce the current efficiency of the cells.
  • Sulfur species have a high solubility in the bath and act as oxidizing agents to react Al to form Al 2 O 3 . This can cause unwanted back reaction of the aluminum which also reduces the current efficiency of the cell.
  • sulfur, iron, nickel and other impurities in the bath can lower the interfacial energy between the bath and the molten pad of aluminum formed in the cell, thereby reducing coalescence or promoting emulsification of the surface of the aluminum pad.
  • the present invention has been developed in view of the foregoing, and to address other deficiencies of the prior art.
  • the present invention recognizes the build up of sulfur impurities in inert anode aluminum production cells, and reduces such impurities in order to increase current efficiencies of such cells.
  • Sulfur impurities may be reduced and removed in regions of the bath in order to achieve high current efficiencies.
  • Gaseous emissions may be scrubbed prior to dry scrubbing with alumina in order to minimize the recirculation of impurities into the bath while maintaining acceptably low sulfur concentrations.
  • Sulfur content of materials introduced into the bath may be controlled.
  • An embodiment of the present invention provides impurity reduction zones in the bath of inert anode aluminum production cells which reduce or eliminate unwanted impurities.
  • the impurity reduction zone is provided by a purifying electrode having an electrochemical potential that is controlled within a selected potential range which reduces or oxidizes sulfur impurities, thereby facilitating removal of the impurities from the bath.
  • reduced sulfur species have much lower bath solubility than oxidized sulfate impurity species, and the reduced sulfur species can escape relatively easily from the bath while avoiding a redox cycle caused by the oxidized sulfate species.
  • the impurity reduction zone comprises a volume of the bath in which oxygen is reduced or eliminated, e.g., oxygen generated during operation of an inert anode cell is prevented from entering a region of the bath.
  • the impurity reduction zone is created through all or portion of the bath by adding a reductant such as Al, carbonates (e.g., Na, Ca, Li, Al and Mg carbonates), CO and/or CO 2 .
  • a reductant such as Al, carbonates (e.g., Na, Ca, Li, Al and Mg carbonates), CO and/or CO 2 .
  • electric current flow is interrupted through some or all of the electrodes of a cell, or electrodes are not positioned in certain areas of the cell, in order to allow sulfur-containing gas to escape from the bath.
  • Another embodiment of the present invention removes sulfur impurities from gaseous cell emissions by techniques such as scrubbing with activated carbon to remove SO 2 before it is absorbed by the alumina that is returned to the inert anode cell.
  • a further embodiment of the present invention reduces sulfur impurities to acceptable levels by controlling the sulfur content of materials added to the bath, such as the sulfur content of alumina and aluminum fluoride fed to the bath. Mass balance calculations may be used in order to select acceptable sulfur content of alumina and other materials added to the bath.
  • An aspect of the present invention is to provide a method of operating an inert anode electrolytic aluminum production cell.
  • the method comprises providing a cell comprising an electrolytic bath, a cathode and at least one inert anode positioned at or above a level of the cathode, passing current between the inert anode and the cathode through the electrolytic bath, and maintaining a sulfur impurity concentration in the electrolytic bath of less than about 500 ppm. In a preferred embodiment, the sulfur impurity concentration is maintained below about 100 ppm.
  • Another aspect of the present invention is to provide a method of reducing sulfur impurities in an electrolytic aluminum production cell.
  • the method comprises providing an impurity reduction zone within an electrolytic bath of the cell.
  • the cell comprises inert anodes.
  • a further aspect of the present invention is to provide a method of producing aluminum.
  • the method includes the steps of providing a cell comprising an electrolytic bath, a cathode and at least one inert anode located at or above a level of the cathode, passing current between the at least one inert anode and the cathode through the electrolytic bath, maintaining a sulfur impurity concentration in the electrolytic bath of less than about 500 ppm, and recovering aluminum from the cell.
  • Another aspect of the present invention is to provide an inert anode electrolytic aluminum production cell comprising means for reducing sulfur impurities contained in an electrolytic bath of the cell during operation of the cell.
  • a further aspect of the present invention is to provide an inert anode electrolytic aluminum production cell comprising a cathode, at least one inert anode located at or above a level of the cathode, an electrolytic bath communicating with the cathode and the at least one anode, and a sulfur impurity reduction zone within the electrolytic bath.
  • Another aspect of the present invention is to provide an inert anode electrolytic aluminum production cell comprising a cathode, at least one inert anode, an electrolytic bath communicating with the cathode and the at least one anode, and a purifying electrode at least partially submerged in the electrolytic bath for providing a sulfur impurity reduction zone within the electrolytic bath.
  • a further aspect of the present invention is to provide an inert anode electrolytic aluminum production cell comprising a cathode, at least one inert anode, an electrolytic bath communicating with the cathode and anode, and a purifying electrode at least partially submerged in the electrolytic bath for providing an impurity reduction zone within the electrolytic bath.
  • the present invention reduces sulfur impurities during aluminum smelting processes which have been found to adversely affect current efficiency of the electrolytic cells. Additional types of impurities to be reduced or eliminated include iron, copper, nickel, silicon, zinc, cobalt, vanadium, titanium and phosphorous impurities.
  • the "current efficiency" of a cell can be determined by the amount of aluminum produced by a cell during a given time compared with the theoretical amount of aluminum that could be produced by the cell based upon Faraday's Law.
  • Sulfur is a particularly harmful impurity which has been found to significantly adversely effect current efficiency of inert anode cells.
  • sulfur in ionized forms such as sulfates, e.g., Na 2 SO 4 and Na 2 SO 3
  • S +6 species is particularly disadvantageous in inert anode cells because it can be easily reduced and subsequently reoxidized.
  • the sulfur impurities form redox couples between the anodes and cathodes of the cells which consume electricity without producing aluminum.
  • sulfur impurities adversely affect the bath/aluminum interfacial energy such that uncoalesced aluminum is dispersed in the bath where it can be more easily oxidized. Current efficiency is significantly reduced as a result of sulfur impurities. It is therefore desirable to eliminate some or all sulfur species from the bath. It is typically desirable to maintain sulfur impurity levels below about 500 ppm in the bath, preferably below about 250 ppm. In a particularly preferred embodiment, sulfur impurity levels are maintained below about 100 ppm.
  • Iron impurities are disadvantageous because iron can also form redox couples which adversely affect current efficiency of the cell. Furthermore, it is desirable to minimize the amount of iron impurities contained in the aluminum produced by the cell. Iron impurity levels in the produced aluminum are preferably maintained below about 0.5 weight percent, typically below about 0.25 or 0.2 weight percent. In a particularly preferred embodiment, the iron impurity level is below about 0.18 or 0.15 weight percent. Copper impurity levels in the produced aluminum are preferably maintained below about 0.2 or 0.1 weight percent, more preferably below about 0.04 or 0.03 weight percent. Nickel impurity levels in the produced aluminum are preferably maintained below about 0.2 or 0.1 weight percent, more preferably below about 0.03 weight percent. The produced aluminum also preferably meets the following weight percentage standards for other types of impurities: 0.2 maximum Si; 0.03 maximum Zn; and 0.03 maximum Co.
  • sulfur and iron impurities have been found to significantly reduce the current efficiency of inert anode aluminum production cells. For example, sulfur levels above about 500 ppm in some inert anode cells have been found to reduce the current efficiency of the cells below about 80 percent.
  • the combination of sulfur and iron impurities has been found to be particularly disadvantageous in inert anode cells. The build-up of combined sulfur and iron impurity levels can actually cause aluminum produced during operation of the cell to be removed.
  • Fig. 1 is a graph illustrating the build up of sulfur impurity levels during operation of an aluminum production cell after the consumable carbon anodes of the cell have been replaced with inert anodes. After several days of operation with the inert anodes, the sulfur impurity level increases above 500 ppm.
  • impurity reduction zones are provided in aluminum production cells.
  • Figs. 2-5 illustrate embodiments in which reduction zones are created through the use of at least one purifying electrode positioned in the bath.
  • Fig. 2 is a partially schematic side sectional view of an aluminum smelting cell 10 in accordance with an embodiment of the present invention.
  • the cell 10 includes a refractory wall 11 and a cathode 12.
  • the cell 10 is partially filled with a molten electrolytic bath 13 which is contained by the refractory wall 11.
  • a molten pad of aluminum 14 forms at the bottom of the cell 10.
  • An anode assembly 15 includes anodes 16a and 16b which are partially submerged in the bath 13. The anodes 16a and 16b are positioned above the level of the cathode 12 in the embodiment shown in Fig. 2 .
  • anode/cathode configurations known in the art may be used in accordance with the present invention in which at least a portion of the anode(s) are positioned at the same level as the cathode(s). With these configurations, sulfur impurities tend to build up in the bath 13 without contacting the aluminum pad 14 that is formed at the bottom of the cell 10.
  • the anodes 16a and 16b preferably comprise inert anodes, for example, as disclosed in U.S. Patent Nos. 6,162,334 , 6,217,739 , 6,332,969 , 6,372,119 , 6,416,649 , 6,423,195 and 6,423,204 comprising ceramic and/or metallic compositions.
  • a purifying electrode 17 is partially submerged in the bath 13.
  • the purifying electrode 17 may be made of any suitable material such as carbon, graphite, TiB 2 , W, Mo, carbon steel or stainless steel.
  • the purifying electrode 17 is connected to the power supply of the cell 10.
  • An oxygen barrier 18 is provided in the bath 13 between the anode 16b and the purifying electrode 17.
  • the oxygen barrier 18 may be made of any suitable material such as TiB 2 , BN or ferrites.
  • current supplied to the purifying electrode 17 creates a positive potential of sulfur, such that sulfur species are oxidized, e.g., to gaseous phases such as COS and SO 2 .
  • the cell 10 is typically a commercial scale cell operated above 50,000 Amps for the commercial production of aluminum.
  • Fig. 3 is a partially schematic side sectional view of an aluminum smelting cell 20 in accordance with another embodiment of the present invention.
  • the cell 20 is similar to the cell 10 shown in Fig. 2 , with the exception that the purifying electrode 17 is connected to a separate power supply 19.
  • Fig. 4 is a partially schematic side sectional view of an aluminum smelting cell 30 in accordance with a further embodiment of the present invention.
  • the cell 30 is similar to the cell 10 shown in Fig. 2 , except the cell 30 includes a purifying electrode 37 which operates in a cathodic mode through its contact with the molten aluminum pad 14 which, in turn, is electrically connected to the cathode 12.
  • the purifying electrode 37 operates at a negative potential of sulfur, such that sulfur species are reduced, e.g., to elemental S or gaseous S 2 .
  • Fig. 5 is a partially schematic side sectional view of an aluminum smelting cell 40 in accordance with another embodiment of the present invention.
  • the cell 40 is similar to the cell 30 shown in Fig. 4 , except it includes a purifying electrode 47 that is externally connected to the cathode 12.
  • Fig. 6 is a partially schematic side sectional view of an aluminum smelting cell 50 in accordance with a further embodiment of the present invention.
  • the cell 50 is similar to the cell 10 shown in Fig. 2 , except the cell 50 does not include a purifying electrode and is provided with an oxygen barrier tube 52 partially submerged in the bath 13.
  • the oxygen barrier tube 52 may be made of any suitable material such as alumina, TiB 2 , BN or ferrites.
  • the interior 53 of the oxygen barrier tube 52 contains a portion of the bath 13 which is isolated from gaseous species generated at the interface between the anodes 16a and 16b and the bath 13.
  • anodes 16a and 16b comprise inert anodes
  • oxygen generated at the anode/bath interface is prevented from entering the interior 53 of the barrier tube 52.
  • This substantially oxygen-free zone allows sulfur-containing species such as SO 2 to vent from the bath 13 through the barrier tube 52 rather than creating unwanted oxygen-containing reaction products in the bath 13.
  • Fig. 7 is a graph of sulfur concentration versus operation time of bench scale aluminum production cells operated with a single inert anode.
  • the dashed lines represent tests performed with no purifying electrodes, while the solid lines represent tests performed with TiB 2 purifying electrodes.
  • the dashed lines in Fig. 7 show sulfur levels in the test cell operated without a purifying electrode, after doping with 200 ppm sulfur (lower dashed line) then doping with 300 ppm sulfur (upper dashed line). Doping was done using Na 2 SO 3 . The same results were achieved using Na 2 SO as the dopant.
  • the sulfur concentration remained substantially constant or slightly increased in these cells operated without a purifying electrode
  • the sulfur concentration decreased from an initial level of about 560 ppm to about 110 ppm within 2 hours.
  • the square points in Fig. 7 are from a test cell similar to that shown in Fig. 4 with a TiB 2 purifying electrode immersed into the metal pad.
  • the sulfur concentration decreased from about 250 ppm to about 110 ppm within 2 hours.
  • the triangular points in Fig. 7 are from a test cell similar to that shown in Fig. 5 in which a TiB 2 purifying electrode was externally connected to the cathode.
  • the sulfur impurity level decreased from about 160 ppm to about 120 ppm in 2 hours.
  • Fig. 8 is a graph of current efficiency versus sulfur concentration in the bath, demonstrating significant decreases in current efficiencies as the sulfur impurity levels increase. At sulfur concentrations above 500 ppm, the current efficiency of the cell decreases below 70 percent.
  • Fig. 9 is a graph showing current efficiency versus sulfur impurity levels in a bath and total impurity levels in the produced aluminum.
  • a test was performed to determine the influence of sulfur on current efficiency at a relatively large scale.
  • An electrochemical cell including one inert anode and was operated at 950 Amperes. Initially the electrolyte was low in sulfur and the contaminates in the aluminum produced by the cell were at low levels. Since the alumina is decomposed to oxygen and aluminum, oxygen evolution from the cell was used to determine the current efficiency of the cell. Aluminum contaminants such as iron, nickel and copper were added to the cell to determine their effect on current efficiency.
  • Fig. 9 is a summary of the results of this test.
  • the impurity reduction zone is created through all or a portion of the bath by adding or controlling the distribution of reductants such as Al, Na 2 CO 3 , CaCO 3 , Li 2 CO 3 , MgCO 3 , CO and CO 2 ,
  • reductants such as Al, Na 2 CO 3 , CaCO 3 , Li 2 CO 3 , MgCO 3 , CO and CO 2
  • Al When Al is used to reduce impurities, it may be added in the form of recirculated aluminum produced by the cell, or the aluminum may be added as pellets, rods or slabs.
  • the aluminum reductant may be continuously or intermittently added to the bath.
  • Gaseous reductants such as CO and CO 2 may be added to the bath by means such as standard sparging techniques.
  • electric current flow may be interrupted through some or all of the electrodes of a cell in order to allow impurities to escape from the cell in gaseous forms.
  • electrode current may be interrupted to some or all of the inert anodes of a cell in order to allow sulfur-containing gas such as sulfur dioxide to escape from the bath.
  • selected regions of the cell may not include anodes in order to provide a region or regions within the cell where oxygen generation is reduced or eliminated.
  • a purifying electrode such as shown in Figs. 2-5 may be positioned within the tube.
  • purifying reductants such as aluminum may be introduced into the bath through such an oxygen barrier tube, with or without the additional use of a purifying electrode.
  • sulfur contained in gaseous emissions from inert anode cells is removed by scrubbing techniques.
  • the hot gases emitted from the cell may be recovered and used to heat the incoming alumina feed by passing the hot gases over the alumina.
  • sulfur and other impurities contained in the gaseous emissions contact the alumina, they are absorbed and carried back to the cell by the incoming alumina.
  • Scrubbing removes sulfur in the off-gas flow, e.g., by electrostatic or chemical (wet or dry scrubbing) means.
  • Electrostatic techniques use electrically charged plates or electrostatic precipitators, which attract the charged sulfur species. The surface is periodically cleaned to remove deposited sulfur species.
  • Wet scrubbing means injecting water or a chemical solution into the exhaust gases. Dry scrubbing uses materials having high surface areas, such as active carbon or lime, which react with the gases.
  • Sulfur removal may be achieved by passing the gaseous emissions through a bed of reactive material such as activated carbon or the like. Adsorption of SO 2 onto activated carbon occurs in two steps. In the first step SO 2 is catalytically oxidized on the carbon to SO 3 . Then the SO 3 hydrolyzes in the presence of water vapor to form sulfuric acid, which condenses in the pores of the carbon: SO 2 + 1 ⁇ 2 O 2 ⁇ carbon SO 3 SO 3 + H 2 O ⁇ H 2 SO 4 condensed .
  • Fig. 11 is a schematic diagram of a sulfur scrubbing system 60 including a cell 62 equipped with a hood 64. Pot gases 66 comprising oxygen, sulfur-containing species such as SO 2 and fluorides flow from the cell 62 to an activated carbon bed 68 where the SO 2 and other sulfur-containing species are removed. Carbon and sulfuric acid 70 from the activated carbon bed 68 are treated in a regeneration chamber 72, and regenerated carbon 74 is reintroduced into the activated carbon bed 68.
  • the activated carbon can be regenerated by treatment with water in the regeneration chamber 72 to form an effluent 73 such as dilute acid or chemicals such as gypsum.
  • Oxygen and fluoride gases 76 exit the activated carbon bed 68 and pass through a dry alumina scrubber 78 to remove fluoride values so they can be returned to the cell 62, thereby recycling the fluoride values and minimizing fluoride emissions to the atmosphere. Gases from the scrubber 78 are vented 80 to atmosphere. Alumina 82 is fed to the dry scrubber 78. As described in more detail below, the alumina 82 may comprise various sulfur impurity contents. After the alumina 82 is contacted with the oxygen and fluoride gases 76 in the dry scrubber 78, the alumina and absorbed fluorides 84 are recycled 86 to the cell 62.
  • alternative scrubbing or stripping systems that may be used in accordance with the present invention include other types of reactive beds such as lime beds, aqueous leaching systems, electrostatic precipitators, and the like.
  • the sulfur content of various materials introduced into the bath is controlled.
  • Figs. 12-17 illustrate, through mass balance calculations, the influence on the steady state concentration of sulfur in the cell of the following parameters: the use of cleaner raw materials; scrubbing SO 2 from the pot gas to reduce recycle back to the cell; and providing an impurity reduction zone in the cell.
  • Fig. 12 shows that with a sulfur content in the alumina fed to the cell of 60 ppm, and considering 40 percent efficient dry scrubbing, the steady state sulfur in the bath would be under 100 ppm.
  • the use of an activate carbon bed also can achieve 102 ppm sulfur in the bath.
  • Fig. 12-17 illustrate, through mass balance calculations, the influence on the steady state concentration of sulfur in the cell of the following parameters: the use of cleaner raw materials; scrubbing SO 2 from the pot gas to reduce recycle back to the cell; and providing an impurity reduction zone in the cell.
  • Fig. 12 shows that with a sulfur content in the alumina fed to the cell of 60 ppm,
  • the sulfur increases to 170 ppm.
  • Increasing the sulfur in the alumina to 250 increases the sulfur in the bath to 374 ppm, as shown in Fig. 15 .
  • the use of an impurity reducing zone in the cell would increase the SO 2 removal four-fold, allowing the use of 250 ppm sulfur alumina while achieving a sulfur level in the bath of less than 100 ppm, as shown in Fig. 16 .
  • the combination of an impurity reducing zone in the cell with activated carbon scrubbing can permit the use of alumina containing as much as 450 ppm while still achieving a sulfur level in the bath of 100 ppm, as shown in Fig. 17 .
  • the sulfur content of alumina may be selected within various ranges while maintaining acceptable sulfur impurity levels in the bath.
  • low-sulfur alumina having a sulfur content within a range of from about 40 to about 100 ppm may be used with no additional sulfur-reducing steps, or with minimal additional sulfur-reducing techniques.
  • Medium-sulfur alumina having a sulfur content within a range of from about 100 to about 250 ppm may be used with selected sulfur-reducing techniques of the present invention necessary to achieve the desired sulfur concentration in the bath.
  • High-sulfur alumina having a sulfur content of from about 250 to about 600 ppm or higher may be used in combination with the present sulfur-reducing techniques in order to maintain the desired sulfur concentration in the bath.

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Claims (6)

  1. Verfahren zum Betreiben einer elektrolytischen Inertanodenaluminiumproduktionszelle (10, 20, 30, 40, 50), wobei das Verfahren Folgendes umfasst:
    Bereitstellen einer Zelle (10, 20, 30, 40, 50), die ein elektrolytisches Bad (13), eine Kathode (12) und mindestens eine Inertanode (16a, 16b), die sich an oder über einer Höhe der Kathode (12) befindet, umfasst;
    Leiten von Strom zwischen der mindestens einen Inertanode (16a, 16b) und der Kathode (12) durch das elektrolytische Bad (13) und
    Aufrechterhalten einer Schwefelverunreinigungskonzentration in dem elektrolytischen Bad (13) von weniger als 500 ppm; wobei die Schwefelverunreinigungskonzentration durch Bereitstellen einer Verunreinigungsverringerungszone in dem elektrolytischen Bad (13) aufrechterhalten wird, wobei die Verunreinigungsverringerungszone durch eine bzw. eines der folgenden bereitgestellt wird:
    (a) eine Reinigungselektrode (17, 37, 47), die zumindest zum Teil in das elektrolytische Bad (13) eingetaucht ist,
    (b) ein Sauerstoffbarriereelement (18, 52), das zumindest zum Teil in das elektrolytische Bad (13) eingetaucht ist,
    (c) Zugeben eines Reinigungsreduktans zu dem elektrolytischen Bad (13),
    (d) Entfernen mindestens einer Inertanode aus einer Region der Zelle oder
    (e) Unterbrechen eines elektrischen Stroms durch mindestens eine Elektrode der Zelle.
  2. Verfahren nach Anspruch 1, wobei die Schwefelverunreinigungskonzentration unter 100 ppm gehalten wird.
  3. Verfahren nach Anspruch 1 oder 2, wobei die Zelle mit einer Stromausbeute von mindestens 80 Prozent arbeitet.
  4. Verfahren nach Anspruch 1 oder 2, wobei die Zelle mit einer Stromausbeute von mindestens 90 Prozent arbeitet.
  5. Verfahren nach Anspruch 1, wobei von der Zelle produziertes Aluminium maximale Verunreinigungsgrade von 0,5 Gewichtsprozent Eisen, 0,2 Gewichtsprozent Kupfer und 0,2 Gewichtsprozent Nickel aufweist.
  6. Elektrolytische Inertanodenaluminiumproduktionszelle (10, 20, 30, 40, 50), die Folgendes umfasst:
    eine Kathode (12);
    mindestens eine Inertanode (16a, 16b), die sich an oder über einer Höhe der Kathode (12) befindet;
    ein elektrolytisches Bad (13), das mit der Kathode (12) und der mindestens einen Anode (16a, 16b) in Verbindung steht; und
    eine Schwefelverunreinigungsverringerungszone in dem elektrolytischen Bad (13), die durch Folgendes bereitgestellt wird:
    (a) eine Reinigungselektrode (17, 37, 47), die zumindest zum Teil in das elektrolytische Bad (13) eingetaucht ist, oder
    (b) ein Sauerstoffbarriereelement (18, 52), das zumindest zum Teil in das elektrolytische Bad (13) eingetaucht ist.
EP02807650.3A 2002-08-05 2002-08-05 Verfahren und vorrichtung zur verminderung von sulfur verunreinungen und verbesserung der stromleistung in aluminium-elektrolysezellen mit inerten anoden Expired - Lifetime EP1534879B1 (de)

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CN102121121A (zh) * 2010-01-07 2011-07-13 贵阳铝镁设计研究院 一种铝用阳极生产过程中对铁含量的工艺控制方法
WO2014004392A1 (en) * 2012-06-25 2014-01-03 Silicor Materials Inc. Method to purify aluminum and use of purified aluminum to purify silicon
TWI488807B (zh) 2012-06-25 2015-06-21 Silicor Materials Inc 添加鹼金屬鎂鹵化物至溶劑金屬
TWI615363B (zh) * 2016-04-08 2018-02-21 科閎電子股份有限公司 降低電解液中至少一污染性陽離子濃度的方法

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DK181867B1 (en) * 2020-11-24 2025-02-26 Elysis Lp Removing impurities from an electrolyte

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CA2495162C (en) 2010-07-27
NO344248B1 (no) 2019-10-21
WO2004013380A1 (en) 2004-02-12
AU2002332463B2 (en) 2008-06-26
NO20051171L (no) 2005-05-03
CN100430523C (zh) 2008-11-05
CN1659313A (zh) 2005-08-24
EP1534879A1 (de) 2005-06-01
BR0215834B1 (pt) 2013-02-19
BR0215834A (pt) 2005-06-07

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