EP0009044A1

EP0009044A1 - Process for obtaining aluminium by electrolysis in a melted bath and electrolytic cell.

Info

Publication number: EP0009044A1
Application number: EP79900193A
Authority: EP
Inventors: Siegfried Wilkening
Original assignee: Vereinigte Aluminium Werke AG
Current assignee: Vereinigte Aluminium Werke AG
Priority date: 1978-02-09
Filing date: 1979-08-13
Publication date: 1980-04-02
Also published as: US4919771A; ATA39079A; JPS55500203A; DE2805374A1; WO1979000606A1; EP0009044B1; AU4408779A; DD142061A5; EP0003598B1; CA1151099A; AU523266B2; AT375409B; DE2805374C2; NO790412L; ES477525A1; EP0003598A1; ES477521A1; GR64827B

Abstract

Procede d'obtention d'aluminium par electrolyse en bains fondus; ce procede utilise en tant qu'electrolyte un bain fondu d'halogenures alcalins et/ou alcalino-terreux et en tant qu'anode un melange contenant de l'oxyde d'aluminium et du carbone.Method for obtaining aluminum by electrolysis in molten baths; this process uses as an electrolyte a molten bath of alkali and / or alkaline earth halides and as an anode a mixture containing aluminum oxide and carbon.

Description

Process for the production of aluminum by melt flow electrolysis

There are essentially two methods known for the melt flow electrolytic extraction of aluminum.

The first method is based on the electrolysis of aluminum oxide, which is dissolved in molten cryolite at temperatures of 950-970 ° C. Apart from cryolite, no other salt has been found to date, the dissolving power of which is sufficient for aluminum oxide in order to obtain aluminum below 1000 C by electrolysis. In the technically operated electrolysis cells, the aluminum oxide content fluctuates between approx. 2 and 8 wt%. If the aluminum oxide content in the cryolite melt is too low, e.g. below 1-2%, the so-called anode effect occurs at the anode, - which manifests itself in a multiple increase in cell voltage. The anode and cathode are made of carbon. The one from the

Alumina decomposition Oxygen released converts with the carbon of the anode to carbon dioxide and carbon monoxide. In the case of prebaked carbon anodes, about 0.43 to 0.50 kg of carbon are consumed per kg of aluminum produced.

The second method concerns the melt flow electrolysis of aluminum chloride. Since the aluminum chloride sublimes at 183 C and is a poor ion conductor, it is usually dissolved in alkali chloride melts. In order to separate the aluminum liquid, electrolysis temperatures of approx. 700 C are used. Graphite is mainly used as the anode and cathode material. Gaseous chlorine is removed at the graphite anode divorced. Several process proposals have been made for performing aluminum chloride electrolysis.

Aluminum chloride electrolysis has a number of difficulties. First of all, the detection and derivation of the gaseous chlorine developed at the anode at around 700 C means a material technology problem. The vapor pressure of the aluminum chloride dissolved in the salt melt is relatively high, so that when the chlorine gas is drawn off, noticeable amounts of aluminum chloride are also extracted from the

Cell is removed. With increasing aluminum chloride concentration in the melt, the electrical conductivity drops. The supply of aluminum chloride, which is obtained in gaseous form, into the molten salt is also difficult to accomplish. Experience has shown that the aluminum chloride and molten salt must be free from oxidic impurities, because the decomposition of the oxides consumes carbon in the graphite anodes and thus reduces the resistance . A particular disadvantage, however, is that it has not yet been easily possible to use aluminum ores, e.g. Build it to produce pure aluminum chloride directly by reducing chlorination. It has therefore been proposed to produce pure aluminum oxide next to the known Bayer process and then to convert it with chlorine and carbon or phosgene to aluminum chloride and carbon dioxide

The process mentioned leads to pure aluminum, but includes an additional process step and is accordingly more complex.

The object of the present invention is to obtain aluminum by melt flow electrolysis using an electrolyte consisting predominantly of chlorides. Here Not only should the deficiencies described for aluminum chloride electrolysis and aluminum oxide electrolysis be avoided, but also the production of aluminum chloride as the starting material should be avoided.

It has been found that by electrolysis in a melt of alkali chlorides with an anode which is composed of aluminum oxide and carbon, aluminum is obtained cathodically with a relatively good current efficiency without chlorine or aluminum chloride being released at the anode. Temperatures of 700 to 850 C are preferably used for this electrolysis process. The main component of the molten salt is sodium chloride with the addition of potassium chloride, lithium chloride or alkaline earth chlorides. , Addition of 10-40% cryolite or other alkali, alkaline earth or light metal fluorides is advisable to the aluminum due to lower surface tension with respect to the hydrochloric easier to cause ^"melt to coalesce. Further, it is useful to electrolysis with a small A1C1, - Bringing the content of 3-5% in the molten salt in motion, because otherwise primary alkali chloride decomposes initially.

Electro graphite and titanium diboride have proven themselves as the material for the cathode arranged on the bottom and on the sides of the electrolysis cell. It depends on the construction of the electrolysis cell whether the side walls of the cell are partially lined with a ceramic, electrically non-conductive product such as magnesite or corundum stones, for example when using bipolar electrodes. A preferred range for the anodic current density is 0.2-2

2 amps per cm.

The surprising moment of the present invention is that the reducing chlorination of the aluminum oxide in the anode and the electrolytic decomposition of the aluminum formed Chloride run off simultaneously in stoichiometric ratios. Despite fairly low-oxide content in the Elektro¬ lytschmelze the initially mentioned phenomenon of -Anodeneffekts was not observed even at an assumed beyond the normal ^• levied anodic current density.

Compared to the two known electrolysis processes, the AlCl ^ electrolysis and the A1 _? 0 electrolysis in cryolite, the following advantages can be shown for the process according to the invention: The handling and transport of chlorine and aluminum chloride are eliminated. The expenditure for the apparatus and facilities is therefore considerably less. Chlorine is a very corrosive gas, especially if it has to be collected in the AlCl _, - electrolysis cell at approx. 700 ° C. Aluminum chloride is hygroscopic, is hydrolytically split into hydroxide and hydrochloric acid by air humidity and, as a sublimate, takes up a lot of space. Dealing with aluminum chloride and chlorine requires closed, corrosion-resistant equipment. This results in larger investment,

Operating and repair costs.

Furthermore, the concentration of the aluminum chloride occurring as an intermediate product in the molten salt is at a very low level, so that neither its vapor pressure nor its unfavorable influence on the conductivity of the molten salts can be felt.

Similar to Al _p 0_ electrolysis in the cryolite melt, an anode gas of carbon dioxide and carbon monoxide is formed at the anode. But while the well-known A1 _? 0 electrolysis in cryolite at bath temperatures around 950oC, are sufficient for electrolysis with the Al _? 0 "-C anode in predominantly chloride melt Working temperatures of maximum 850 C, on average of 750 C. The lower electrolytic temperatures reduce the heat losses and reduce

-BUKE

C.VP the specific energy consumption. The electrolysis cell according to the invention is supplied on the raw material side only with the compact aluminum oxide-carbon anode as the electrode, and it can be supplied discontinuously in block form or continuously in strand form. In contrast to this, in the electrolysis with the Al _p O, -containing cryolite melt, the A1_0 concentration in the electrolysis bath must be maintained in that aluminum oxide is introduced into the melt bath by breaking the surface crusts at predetermined intervals. The operation of the electrolytic cell according to the invention is limited to changing the anodes and sucking out the deposited aluminum. The procedure allows the electrolysis cell to be encapsulated with a simple housing that is difficult to open.

The aluminum oxide and carbon anode to be used as part of the invention posed some problems, the solution of which was an important task.

Theoretically, the anode would have to consist of 85% aluminum oxide and 15% carbon if carbon dioxide is formed as the reaction gas in the electrochemical reduction. The Ab¬ decision of coal monoxide would an anode with 7 U% "Al _p O and 26% C require. However, the formation of pure carbon onoxide is not possible due to the Boudouard equilibrium at temperatures around 750 C, but only a C0 _p -C0 gas mixture with approx. 80% CO. Theoretically, the alumina-carbon ratio can be between the limits 5.66: 1 and 3.4: 1. The current yield deviating from 100% and a slight air burn of the anodes increase the carbon consumption. Under practical electrolysis conditions, a gas containing predominantly CO _p develops at the anode. The weight ratio of Al _p O to C can vary in the anode in a width of 5 to 1 to 3 to 1 without this causing serious disturbances in the Make the electrolysis process noticeable. The self-adjusting CO _p / GO ratio of the anode gas has a regulating effect. In the tests carried out, a usable composition of the anode consisting of 80% by weight of A1 _? 0_ u 20 wt .-% C ,. ie a weight ratio of 4: 1 is aimed for.

The volume fraction of carbon in the Al _p 0 -.- C anode is higher, however, because the true density of the carbon is about 2.00 g / cm 3 and that of the aluminum oxide is about 3.8 g / cm3. From this, a volume fraction of carbon of 32.2% is calculated for the stated weight ratio of 4: 1.

An anode made of aluminum oxide and carbon can be produced, for example, by mixing finely divided aluminum oxide and / or aluminum hydroxide with electrode pitch, shaping it into a body and burning it at about 1000 ° C. in the absence of air at the same rate. The g burned aluminum oxide-carbon anode has a specific electrical resistance of approximately 1000 Ω. mm / m. E carbon anode, as is used for Al _p 0_ electrolysis in molten cryolite, has only a resistance of approx. 60- ^ 2. mm / m. The A1 _? 0 -C anode is therefore not suitable for a long current path in the anode. To the voltage drop in the A1 _? To keep the 0 -C anode as low as possible, it is expedient for the process according to the invention to combine the Al _p O ^ -C anode with an auxiliary conductor made of electrographite. The electrical resistance of the graphite electrodes is approx. 10 1 mm / m and is thus six times smaller than that of a burned carbon anode. The graphite material "

2 can be loaded with current densities up to 10 A / cm.

If you want at least anodic current densities from 0.6 to 1.0

2 A / cm, as is common in Al _p O electrolysis with carbon anode and cryolite melt, it is sufficient that for electrographite a conductive cross section of about one fifth of the cross section of A1 _? 0 -C anode is seen vor¬. The composite anode from the A1 _? The 0 -C body and the graphite material can then be loaded similarly to a pre-burned carbon anode without having to fear overheating or unfavorable energy consumption. The highly conductive graphite material is mainly connected in parallel to the Al _p 0 _, - C body. This can happen, for example, in such a way that the graphite is in the form of a rod or plate in the core of the Al _p 0 -, - C body or encompasses the Al _p 0_-C body outside.

It has now surprisingly turned out that the auxiliary conductor made of electrographite next to the A1 _? 0 -C mass is not consumed in the electrolysis cell. Electrographite can therefore be reused as a carrier material for the Al _p O ^ -C mass.

Firing in deep chamber ring furnaces, a process step with unsatisfactory space-time yield, is part of the production of an electrically conductive, solid molded body made of aluminum oxide and pitch. In a further embodiment of the invention, this production cycle can be blocked if a self-baking Söderberg mass is produced from the aluminum oxide and suitable tars or pitches. It is expedient to either embed the conductive auxiliary material made of graphite elements in the Al _p 0_ pitch composition or to surround it. If the consumption of the anode in the electrolysis cell continues, the Al _p O -Pech mass reaches increasingly hotter temperature zones, is gradually coked and electrically and mechanically connected to the graphite parts. The metallic current conductors leading to the anode are connected to the graphite elements for reasons of low contact or contact resistance. The metal contact pieces and their brackets are designed so that they can be continuously and automatically moved.

In a Söderberg mass made of aluminum oxide and pitch, it is also possible to use aluminum as an auxiliary conductor instead of electrographite. The aluminum melts at approx. 100 C below the electrolysis temperature at approx. 650 C from, but between 550 and 650 C is a current transfer from

Aluminum for Al _p 0_-C mass possible.

The gases released in and on the anode are completely captured by encapsulating the electrolytic cell, suctioned off and fed to an exhaust gas cleaning system. The unavoidable chlorine and salt losses of the melt flow electrolyte are compensated for by adding a salt mixture of aluminum chloride and the corresponding salt components of the cell electrolyte used, which has been melted elsewhere, as required.

After the basic features of the method according to the invention have been presented, three electrolysis units operating according to this principle will be described.

Figure 1 shows a section through an electrolytic cell with only one composite anode to be replaced. The conductor rails 2 made of steel are embedded in the cathode 1 made of electrographite or another carbon material. There is a layer of liquid aluminum 3 on the bottom of the cathode basin 1 and the electrolyte melt 4 above it. The carbon cathode 1 is surrounded by the heat-insulating masonry 5. The steel pan 6 forms the outer frame of the electrolysis vessel. The discontinuous composite anode 7/8 consists on the one hand of an Al _p 0_ carbon mass 7 and on the other hand of the graphite part 8. The in the molten salt 4th

SURE 3KP immersed anode is held by the metal rod 9. The metal rod 9, which also serves as a conductor, is screwed into the graphite part 8 and clamped to a conductor rail above the electrolytic cell. In order to avoid corrosion of the metal rod within the cell space, it is surrounded by a protective sleeve 10. The electrolysis cell is covered with the sheet metal hood 11. The electrolysis gases are drawn off through the openings 12, to which a pipeline is connected.

Figure 2 illustrates in longitudinal section a multi-chamber

Electrolytic cell. The electrolysis unit contains a series of plate-shaped graphite cathodes 21 which are connected in parallel and are suspended in the rectangular electrolysis room by means of the screwed-in power supply bolts 22. Arranged between the cathodes are the anodes 23, 24, which, as in FIG. 1, consist of the aluminum oxide-carbon mass 23 and the support plates 24 made of graphite. The anodes are also carried by laterally screwed-in power supply bolts 25 and are immersed in the electrolyte 26 with their AlpO_-C mass. At the bottom of the electrolytic cell, the aluminum layer 27 spreads across all chambers. A lining made of carbon plates 28 is in contact with the aluminum 27 and the electrolyte 26. After this lining material 28 there is a ceramic thermal insulation 29 and then the steel container 30. The electrolytic cell is closed by the cover plate 31. It is not shown that the cover has flaps through which the anodes 23, 24 can be replaced. The exhaust gas is sucked out through the outlet holes 32.

FIG. 3 is a horizontal section at position AB through the electrolysis cell sketched in FIG. 2. In addition to this sectional drawing, it should be noted that the power supply bolts of the cathode and anode elements 22 and 25 are in contact half-shells 3, which are connected outside the container 30 to the corresponding positive and negative current bars. For the rest, the code numbers used in FIG. 3 apply to FIG. 3.

The electrolytic cell according to FIGS. 2 and 3 can, of course, also contain any number of cathode and anode elements as desired, as in the example shown. When operating such an electrolysis cell, care will be taken to ensure that the A1 _? 0_-C mass 23 is not the same for the individual anodes. When the Al _p 0_-C mass 23 is completely removed due to electrolysis on one of the anodic mother plates 24, a change is made to a new anode element. During the anode change, the other anode elements connected in parallel take over the current flow. The aluminum produced is transferred in a known manner from the electrolysis cells

Proboscis sucked into vacuum crucible.

The method according to the invention also makes it possible to operate electrolytic batteries with bipolar electrodes. FIGS. 4 and 5 show an exemplary embodiment for a five-cell electrolysis battery. 4 shows a horizontal section at the height EF of FIG. 5 and FIG. 5 shows a vertical section through the CD of FIG. 4. They denote in detail

41 = graphite cathode, 42 = cathodic current bolts made of metal ,. 3 = Al _p 0_-C mass of the bipolar electrode, 44 = anode made of graphite, 45 = anodic current bolts made of metal, 46 = bipolar electrodes, 47 = graphite plate of the bipolar electrode, 48 = melt flow electrolyte, 49 = corrosion-resistant, electrically insulating lining material, 50 = ceramic thermal insulation, 51 = steel tank, 52 = liquid aluminum 53 = cover of the electrolytic cell, 54 = outlet holes for exhaust gas.

or - '. Pi The cathode 41, the anode 44 and the bipolar electrodes 46 are, as shown in ^'Figures 4 and 5 it can be seen loosely in the electrolysis chamber into the appropriate locations ge provides. The little-wearing cathode 41 can remain in the electrolytic cell for a long time. The bipolar electrodes must be replaced when the layer thickness of the Al ^ O -C mass is almost used up. A complete consumption of the Al ₂ O -, - C mass 43 on the graphite plates, as is possible with the cell construction according to FIGS. 2 and 3, cannot be allowed for the bipolar electrodes due to chlorine separation and decomposition of the alkali chlorides. If the Al_0_-C mass 43 on the anode 44 has almost been removed and a change has to be made, this measure leads to a current interruption in the electrolysis cell. A current interruption can be avoided, however, by dividing the anode into at least two halves, which are changed at different times. For the individual bipolar electrodes, too, a division and a time-shifted exchange of the two halves is recommended. In this way, the Al _p O ^ -C mass on the bipolar electrodes can be used up practically completely.

The electrolysis cells described in FIGS. 1 to 5 are to be regarded as examples and basic models which allow a variety of construction variants without changing the principle.

The materials usually used for the cathode are carbon, electrographite, titanium boride, zirconium boride or mixtures thereof.

In a further embodiment of the invention, it is possible to use an anode in which the mass of aluminum oxide and carbon is not mechanically firmly connected to the anode part made of graphite. It is sufficient if the Al_0_-C mass is included the electrically good conductive material graphite is in electrical contact. A practical implementation of this principle is shown in FIG. 6.

FIG. 6 shows a vertical section of an electrolysis cell which differs from the previously described electrolysis cells in FIGS. 1-5 in the structure of the anode and in the supply of the Al 0 -C mass. In the middle of the electrolysis cell, the cathode 61 made of graphite with the metallic current conductor 62 is arranged. The anode consists of three green elements. The first part of the anode is one

«

Graphite plate 64 with the threaded bolt 65, via which the electrolysis current is supplied. In front of the graphite plate 64 is the Al ₂ 0_-C mass in lump form. The Al 0 -C mass is charged as briquettes, pellets, tablets or as other granules and held by a plate 66. In this example it is made of graphite and has horizontal slots. However, other materials, in particular sintered corundum, zirconium oxide and sintered magnesia, are also suitable for the production of the plate 66. The plate 66 embodies a kind of diaphragm and has the task to ensure that on the one hand no particles of the Al O -.- C mass get from the anode space into the electrolyte and on the other hand a sufficiently free passage for the electrolyte melt 67, which the electr trolysis space between cathode and anode is present, therefore the plate 66 must either contain an open pore system or appropriate holes or channels. The aluminum is deposited in liquid form on the cathode 61. It drips from it and collects at the bottom of the electrolytic cell to bath 68.

The anode consisting of the components 63, 64 and 66 and the remaining electrolysis room are enclosed in a corrosion-resistant, electrically non-conductive masonry 69. The heat protection of the electrolysis cell is ensured by the fire-proof insulation 70. The lumpy Al _p O ^ -C mass can be charged in batches or fully continuously, adapted to the consumption of the electrolytic cell, using a funnel. The three-part anode according to claim 22 can of course be installed in place of the composite anodes 23, 24 in FIGS. 2 and 3 and 43, 44 in FIGS. 4 and 5 of the multi-cell electrolysis units.

A process scheme for the production of the lumpy material from Al _^ O., and carbon is shown in Figure 7. The individual process steps are examples. traditional and replaceable by similar procedural units. For example, the chamber shaft furnace can be replaced by a tunnel furnace. If the flow diagram in FIG. 7 is compared with the preparation courses of the raw and auxiliary materials of the two known electrolysis processes mentioned at the outset, the process according to the invention has significant apparatus and energy-saving advantages.

Claims

Patent claims

1. A process for the production of aluminum by melt flow - electrolysis, characterized in that a melt consisting of alkali metal and / or alkaline earth metal halides is used as the electrolyte and a mixture containing aluminum oxide and carbon is used as the anode.

A method according to claim 1, characterized in that the electrolyte contains more than 50% alkali chlorides.

3- The method according to any one of the preceding claims, characterized in that the electrolyte melt consists of more than 50% of sodium and / or potassium chloride.

4. The method according to any one of the preceding claims, characterized in that the electrolyte melt contains ent of 10-40% cryolite, alkali and / or alkaline earth fluoride ent.

5. The method according to any one of the preceding claims, characterized in that the electrolytic reduction is carried out at temperatures of 680-850 C.

6. The method according to any one of the preceding claims, characterized in that the electrolyte melt lithium chlorine and / or alkaline earth chlorides are added in amounts of 2-20%.

7. The method according to any one of the preceding claims, characterized in that the aluminum chloride content of the molten salt is 3-5% before the start of the electrolysis.

oy Method according to one of the preceding claims, characterized in that the raw material containing aluminum is supplied through the anode during the electrolysis.

Method according to one of the preceding claims, characterized in that the raw material containing aluminum is fed continuously or continuously through the anode as granules or in pieces during the electrolysis.

10. The device for carrying out the method according to any one of the preceding claims, characterized in that the electrolytic cell contains at least one anode which consists of a mixture containing aluminum oxide and carbon and the cathode consists of a compared to the electrolyte and liquid aluminum resistant material with good conductivity.

11. Device according to one of the preceding claims, characterized in that _. the anode contains electrographite.

12. Device according to one of the preceding claims, characterized in that the aluminum oxide of the anode has a degree of purity of at least 98% for the production of pure aluminum.

13- Device according to one of the preceding claims, characterized in that the anode contains a carbon-containing binder.

i H. Device according to one of the preceding claims, .da¬ characterized in that the anode consists of a self-baking mixture containing aluminum oxide, tar and / or pitch.

15. Device according to the preceding claim, marked by a self-baking mixture surrounded by graphite elements.

16. Device according to one of the preceding claims, characterized in that the electrolysis cell has side walls made of ceramic, electrically non-conductive material.

17. Device according to one of the preceding claims, characterized in that the side walls consist of magnesite and / or the corundum stones.

18. Device according to one of the preceding claims, characterized in that several parallel sections with cathodes and anode elements are present in an electrolytic cell.

19. Device according to one of the preceding claims, characterized in that several electrolytic cells below

Use of bipolar electrodes in a common container are connected in series to form a battery

20. Anode according to one of the preceding claims, contain aluminum oxide and carbon in a weight ratio of 5 b

3 to 1.

21. A method for preparing an anode according to one of v take precedence claims, characterized in that finely partially saturated alumina and / or aluminum mixed denpech with electric, formed into a body and close with slower on ^'under Luf heating rate fired to about 1000 ° C .

22. Device according to one of the preceding claims, characterized in that the anode is formed from a container in which the mixture containing aluminum oxide and carbon is introduced and the container wall towards the cathode has a perforated shield (66 ) having.

23- Device according to one of the preceding claims, characterized in that the shield (66) consists of graphite, sintered corundum, zirconium oxide and / or sintered raagnesia.

24. Device according to one of the preceding claims, characterized in that the container, in which the lumpy mixture of aluminum oxide and carbon is contained, is used in a multi-chamber electrolysis cell or as a bipolar electrode in a multi-cell electrolysis unit.