EP3030695B1 - Aluminerie comprenant un circuit électrique de compensation - Google Patents

Aluminerie comprenant un circuit électrique de compensation Download PDF

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Publication number
EP3030695B1
EP3030695B1 EP14834860.0A EP14834860A EP3030695B1 EP 3030695 B1 EP3030695 B1 EP 3030695B1 EP 14834860 A EP14834860 A EP 14834860A EP 3030695 B1 EP3030695 B1 EP 3030695B1
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EP
European Patent Office
Prior art keywords
electrolysis
current
conductors
electrolytic cell
compensating
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EP14834860.0A
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German (de)
English (en)
French (fr)
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EP3030695A1 (fr
EP3030695A4 (fr
Inventor
Steeve RENAUDIER
Benoit BARDET
Olivier Martin
Christian Duval
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Rio Tinto Alcan International Ltd
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Rio Tinto Alcan International Ltd
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Priority to SI201431028T priority Critical patent/SI3030695T1/sl
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Publication of EP3030695A4 publication Critical patent/EP3030695A4/fr
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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
    • C25C3/16—Electric current supply devices, e.g. bus bars
    • 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
    • C25C3/20—Automatic control or regulation of cells
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C3/00—Electrolytic production, recovery or refining of metals by electrolysis of melts
    • C25C3/06—Electrolytic production, recovery or refining of metals by electrolysis of melts of aluminium
    • C25C3/24—Refining
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
    • C25C7/005—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells of cells for the electrolysis of melts

Definitions

  • the present invention relates to an aluminum smelter, a method of using this smelter and a method for stirring alumina in the electrolysis tanks of this smelter.
  • an electrolytic cell comprising a steel box inside which is arranged a coating of refractory materials, a cathode of carbon material, crossed by cathode conductors for collecting the electrolysis current at the cathode to lead to cathode outlets through the bottom or sides of the box, routing conductors extending substantially horizontally to the next vessel from the cathode outlets, an electrolytic bath in which is dissolved alumina at least one anode assembly comprising at least one anode immersed in said electrolytic bath, an anode frame to which the anode assembly is suspended, and electrolysis current rise conductors extending from bottom to top connected to the conductors for routing the preceding electrolytic cell to convey the electrolysis current from the cathode outlets to the anodic frame e and the anode assembly and the anode of the next vat.
  • the anodes are more particularly of anode type
  • Aluminum production plants, or aluminum smelters traditionally comprise several hundred electrolytic cells, aligned transversely in parallel queues and connected in series.
  • MHD magnetohydrodynamic instabilities
  • the horizontal component of the magnetic field generated by the whole the path of the electric current, both in the conductors located inside the tank and those located outside, interacts with the electrical current flowing through the liquids, which generates a stationary deformation of the metal sheet.
  • the unevenness of the metal sheet caused must remain low enough so that the anodes are consumed uniformly with little waste.
  • it is necessary that the horizontal components of the magnetic field are the most antisymmetric possible in liquids (electrolytic bath and metal sheet).
  • antisymmetric means that when we move perpendicular to the central axis of the tank, parallel to the relevant component of the field, and when we go located at equal distance on either side of this central axis, the value of the component considered is opposite.
  • the antisymmetry of the horizontal components of the magnetic field is the configuration providing the most symmetrical interface interface and as flat as possible in the tank.
  • the main advantage of self-compensation is the use of the electrolysis current itself to compensate for MHD instabilities.
  • Another solution for reducing MHD instabilities known in particular from the patent document FR2425482 is to use a secondary electrical circuit, or external loop, along the rows of electrolysis tanks, on the sides.
  • This secondary electrical circuit is traversed by a current whose intensity equals a predetermined percentage of the intensity of the electrolysis current.
  • the outer loop generates a magnetic field that compensates for the effects of the magnetic field created by the electrolysis current of the next row of electrolysis cells.
  • the external loop compensation solution has the advantage of having a secondary circuit independent of the main circuit traversed by the electrolysis current.
  • the arrangement of the secondary circuit located on the sides of the tank lines near the short sides of the boxes, at the height of the bath-metal interface, allows compensation of the vertical component without impacting the horizontal component of the magnetic field.
  • the external loop compensation solution significantly reduces the length, mass and electrical losses of the routing conductors, but requires an additional power station and additional independent secondary electrical circuit. It should also be noted that the external loop compensation solution involves a combination of magnetic fields, with the current of the series, creating a very strong total ambient field, so that it implies constraints on operations and equipment (for example shielding necessary vehicles), and so that the magnetic field of a queue impacts the stability of the tanks of the next file. To limit the influence of a queue on the neighboring queue, it is necessary to move them away from each other, which constitutes a significant spatial constraint and therefore involves housing each row of electrolysis cells in a separate shed.
  • junction portion of the electrolysis circuit and the secondary circuit joining the ends of two adjacent rows of electrolytic cells tends to destabilize the end of the tank.
  • this portion of the secondary circuit according to a predetermined path, as known from the patent. FR2868436 , in order to correct the magnetic field so that the impact on the end tanks becomes acceptable.
  • this path lengthens the length of the secondary circuit, therefore the material cost.
  • the usual solution is to move the junction portion of the secondary circuit and the electrolysis circuit of the tanks located at the end of the line, but this increases the space requirement in addition to increasing the length of the electrical conductors so the material and energy cost.
  • the present invention aims to overcome all or part of these disadvantages by providing an aluminum smelter with a magnetic configuration for improved performance and a small footprint.
  • the subject of the present invention is an aluminum smelter, comprising at least one row of electrolysis cells arranged transversely with respect to the length of the line, one of the electrolytic cells comprising a box, and anode assemblies comprising a support and at least one anode, and a cathode crossed by cathode conductors for collecting the electrolysis current I 1 at the cathode to lead it to cathode outlets outside the box, characterized in that the tank of electrolysis comprises electrical conductors for mounting and connecting to the anode assemblies extending upwardly along two opposite longitudinal edges of the electrolytic cell to conduct the electrolysis current I 1 to the anode assemblies, and connected to the cathode outlets and intended to conduct the electrolysis current from the cathode outlets to the electrical conductors of the mount e and connecting the next electrolytic cell, and in that the aluminum comprises at least one electrical compensation circuit extending under the electrolytic cells, said compensation circuit being traversed by a current I 2 of compensation circulating under the electrolysis tanks in the
  • the aluminum plant according to the invention has a small footprint and offers the advantage of having very magnetically stable tanks, so that the overall yield is improved.
  • the compensation circuit is traversed by a compensation current I 2 flowing under the electrolytic cells in the opposite direction to the overall flow direction of the electrolysis current I 1 flowing through the tanks. electrolysis located above.
  • the intensity of the compensation current I 2 is of the order of 50% to 150% of the intensity of the electrolysis current I 1 .
  • the electrical conductors of rise and connection are arranged in the inter-tank spaces, at the two longitudinal sides of the electrolytic cell, on either side of the tank to compensate each other and obtain a substantially antisymmetric distribution of the horizontal components of the magnetic field of the tank providing a small difference in elevation of the aluminum sheet without impacting the vertical component of the magnetic field, so that the electrical conductors of the tank, among the conductors routing, mounting and connection , causing an unfavorable vertical and horizontal magnetic field to be compensated are in practice only the tank-bottom conductors circulating horizontally below the box, that is to say more specifically the routing conductors.
  • the compensation of this unfavorable magnetic field is then obtained by means of the compensation electric circuit, which can advantageously be traversed by a current I 2 of intensity compensation of the order of 50% to 150% of the intensity of the current.
  • the magnetic field is weak or virtually canceled near the tanks and rows of tanks and the aluminum plant according to the invention, so that the constraints related to strong magnetic fields on the operations and equipment used in the aluminum smelter are deleted. Also, the magnetic field of a queue no longer affects the stability of the tanks of the neighboring queue so that neighboring tank lines can be brought together and two rows of neighboring tanks can in particular be placed in the same building of reduced width, so that significant savings in structural costs can be realized even when a compensation circuit is used.
  • the compensation circuit passes under the electrolytic cells, and not on the sides of the electrolysis cell line or rows.
  • a space is clear on both sides of the row or rows of electrolysis tanks. This allows to consider a lateral clearance of each electrolysis tank, and more particularly the box, which is less expensive than lifting.
  • the absence of heavy and expensive lifting solutions offers significant structural savings.
  • the compensation electric circuit is a secondary electrical compensation circuit distinct from the electrical circuit traversed by the current I 1 electrolysis. Separate means that the two circuits are not electrically connected.
  • the compensation circuit is damaged and cut or can not no longer operate normally, this affects the efficiency, because the compensation circuit can no longer compensate the magnetic field generated by the circulation of the electrolysis current, but the smelter can continue to operate in degraded mode with a lower yield without suffering from detrimental stop, since the current flowing in the compensation circuit is intended for magnetic field compensation only and not for the production of aluminum.
  • the use of a separate secondary compensation circuit also offers the possibility of changing over time the compensation magnetic field created by this compensation circuit. It is necessary for this purpose to vary the intensity of the current flowing in the secondary electrical compensation circuit. This is of paramount importance in terms of scalability and adaptability. Firstly because it allows, in case of increase of the intensity of the electrolysis current during the life of the smelter, to adapt the magnetic compensation to this evolution, by variation of the intensity of the current compensation according to needs. On the other hand because it makes it possible to adapt the amperage of the compensation current to the characteristics and the quality of the available alumina. This makes it possible to control the speed of MHD flows to promote or limit the mixing of liquids and the dissolution of alumina in the bath. depending on the characteristics of the available alumina, which ultimately contributes to the best possible yield given the supply of alumina.
  • the secondary electrical compensation circuit may be more particularly powered by a clean power station, different from the station supplying the electrolysis cells with electrolysis current.
  • the aluminum plant comprises two rows of tanks arranged parallel to one another, fed by the same station, and electrically connected in series so that the electrolysis current flowing in the first two rows of tanks then circulates in the second of the two rows of tanks in a direction generally opposite to that in which it circulated in the first of the two rows, and in that the compensation circuit forms a loop under these two rows of parallel tanks.
  • the secondary electrical compensation circuit forms a loop under the tanks, it becomes advantageous to use an electrical conductor made of a superconducting material in order to achieve it, and it is above all possible to carry out several turns in series, as described in the application for patent WO2013007893 in the name of the plaintiff.
  • the electrolytic cell comprises for each of its two longitudinal edges a plurality of electrical conductors rise and connect distributed at predetermined intervals over substantially the entire length of the corresponding longitudinal edge.
  • the rise and connection conductors may be arranged at regular intervals in the longitudinal direction of the electrolytic cell.
  • a tank operating with an intensity of 400 to 1000k amps can for example preferably comprise from 4 to 40 distributed rise and connection conductors. regularly over the entire length of each of its two longitudinal edges.
  • the upstream and upstream electrical conductors and the upstream and downstream electrical conductors may be arranged equidistant from a longitudinal median plane of the electrolytic cell, that is to say a plane substantially perpendicular to a transverse direction of the vessel and separating it into two substantially equal portions.
  • electrical conductor upstream and upstream connection and electrical conductor upstream and downstream connection is meant electrical conductors rise and connect arranged respectively next to the longitudinal edge upstream or downstream of the electrolytic cell, the upstream longitudinal edge corresponding to the one that is closest to the beginning of the electrolysis cell line and the downstream longitudinal edge corresponding to the longitudinal edge of the electrolysis cell farthest from the beginning of the electrolysis cell line, taking into account the meaning overall flow of electrolysis current at the scale of the electrolysis cell line.
  • the electrical conductors for mounting and connection are arranged substantially symmetrically with respect to a longitudinal median plane of the electrolytic cell.
  • the rising and connecting electrical conductors extending along one of the two longitudinal edges of the electrolytic cell are arranged substantially symmetrically with respect to the electrical conductors for mounting and connection.
  • extending along the opposite longitudinal edge of the electrolytic cell with respect to a longitudinal median plane of the electrolytic cell, that is to say a plane substantially perpendicular to a transverse direction of the vessel and separating it from ci in two substantially equal parts.
  • electrolysis is of the order 30-70% upstream and 30-70% downstream, and preferably 40-60% upstream and 40-60% downstream, respectively.
  • the current distribution between the electrical conductors of rise and connection arranged upstream of the electrolytic cell and the electrical conductors of rise and connection arranged downstream of the electrolytic cell is 45-55% upstream and 45-55% downstream respectively.
  • the routing conductors extend under the electrolytic cell substantially straight, and only in a direction transverse to the electrolysis cell.
  • the compensation electric circuit may comprise electrical conductors extending substantially parallel to a transverse axis of the electrolysis cells.
  • the compensation electric circuit comprises electrical conductors forming a plurality of secondary electrical secondary compensation sub-circuits independent of each other.
  • Each of these secondary electrical compensation sub-circuits is traversed by an intensity compensation current that can be variable independently of the intensity of the electrolysis current.
  • independent secondary electrical sub-circuit compensation is meant subcircuit not electrically connected to the other secondary electrical sub-circuits compensation, and can be powered by a separate power station from that of other secondary electrical sub-circuits compensation.
  • the compensation electric circuit may comprise electrical conductors forming several turns in parallel and / or in series under the electrolysis cells.
  • the compensation electric circuit comprises electrical conductors extending parallel under the electrolysis cells.
  • the electrical conductors of the compensation electric circuit may be arranged substantially symmetrically with respect to a transverse median plane of the electrolysis cells, that is to say a plane substantially perpendicular to a longitudinal direction of the electrolysis cells and separating the tank in two substantially equal parts.
  • the electrical conductors forming the compensation electric circuit or, where appropriate, the secondary electrical compensation sub-circuits extend under the electrolysis cells together forming a layer of two to twelve, preferably three to ten , parallel electrical conductors.
  • said electrical conductors are substantially equidistant and distributed substantially symmetrically with respect to a transverse center axis of the electrolysis cells.
  • each module may comprise, for example, an electrical conductor of the compensation electric circuit and a number of routing conductors and associated risers and connection conductors for each electrolysis cell.
  • the conductor circuit, and therefore each tank, can be composed of a number of modules, determining the length of the tanks and the intensity of the current flowing through the tanks.
  • the choice of the number of modules per tank during the design or an extension of the length of the tanks by the addition of such modules does not disturb the magnetic equilibrium of the tanks, unlike the lengthening of tanks of the self-compensated or compensated type by of the magnetic compensation circuits arranged on the sides of known prior art tanks for which the conductor circuits must be completely redrawn.
  • the ratio of the amount of material forming the conductor circuit brought to the production surface of the tanks does not deteriorate when extending the tanks, it increases proportionally to the number of modules and the intensity through the tanks.
  • the tanks can be elongated simply according to the needs and the intensity of the current passing through them is not limited. It then becomes possible to increase the intensity of the current passing through the tanks above 1000 k amperes, or even 2000 k amperes.
  • the rising and connecting electrical conductors extending along one of the two longitudinal edges of the electrolytic cell are arranged in staggered relation to electrical conductors for mounting and connecting arranged on the adjacent longitudinal edge of a previous or next separate electrolytic cell.
  • the electrical conductors upstream and upstream connection of an electrolysis vessel N are arranged in staggered relation to the electrical conductors of upstream and downstream connection of the electrolytic cell N-1, that is to say say of the electrolysis tank preceding it.
  • the electric compensation circuit is traversed by an intensity compensation current of the order of 70% to 130% of the intensity of the current I 1 d electrolysis, and preferably of the order of 80% to 120% of the intensity of the current I 1 electrolysis.
  • the intensity of the compensation current flowing through this compensation circuit can be of the order of 70% at 130% of the intensity of the electrolysis current.
  • the intensity of the compensation current flowing through the electrical conductor may be of the order of one third from 70% to 130% of the intensity of the current electrolysis.
  • the compensation electric circuit is formed by three secondary electrical compensation sub-circuits each making twenty turns in series and each made with electrical conductors of superconducting material, then the intensity of the compensation current, each traveling through these three secondary electrical compensation sub-circuits can be of the order of one sixtieth of 70% to 130% of the intensity of the electrolysis current.
  • each cathodic output leaves the box only in a vertical plane perpendicular to the longitudinal direction of the electrolytic cell.
  • the cathode outlets pass through the bottom of the chamber of the electrolytic cell. Having outlets at the bottom instead of at the sides of the electrolytic cell decreases the length of the feed conductors, as well as the horizontal currents in the liquids, resulting in better MHD stability.
  • the electrical conductors for routing may extend in a straight line, substantially parallel to a transverse direction of the electrolytic cell to the electrical conductors for mounting and connecting the next electrolytic cell.
  • a electrolysis tank of the state of the art comprises a superstructure longitudinally crossing the electrolytic cell, above the box and anodes.
  • the superstructure includes a beam resting on feet at each of its longitudinal ends. It supports an anode frame, also extending longitudinally over the box and anodes, which supports the anode assemblies and to which the anode assemblies are connected.
  • the support of the anode assembly comprises a cross member extending transversely to the electrolytic cell being supported and electrically connected at each of the two longitudinal edges of the and other of the electrolysis cell.
  • the anode assembly is no longer supported and electrically connected by means of a superstructure longitudinally crossing the electrolytic cell, above the box and anodes so that the electrolysis cells can be elongated to take full advantage of the possibilities offered by the principle of compensation or magnetic balancing of the method of use of the aluminum smelter according to the invention.
  • the rising and connecting conductors extend on either side of the box without extending to the right of the or anodes.
  • the right of the anode or means in a volume formed by vertical translation of the surface obtained by projection of the anode or in a horizontal plane XY.
  • Such an embodiment makes it possible to advantageously replace the anode by pulling it vertically upwards, since the anode towed upward does not encounter any elements having served at its connection. From this simplification of the placement and the anode removal there also arise savings in the management and operation of the aluminum plant according to the invention.
  • the length of the rising and connecting conductors is reduced with respect to the use of conventional type rise and connection conductors which typically extend above the vessel into the longitudinal central portion of the vessel. This helps to reduce manufacturing costs.
  • the rising and connecting conductors are more particularly connected to the anode assemblies at the edges of the box.
  • edges of the box By the right of the edges of the box is meant in a volume formed by vertical translation of the surface obtained by projecting the edges of the box in a plane horizontal XY.
  • the rising and connecting electrical conductors extend at a height h between 0 and 1.5 meters above a substantially horizontal plane including the surface of the liquids contained in the electrolytic cell.
  • the method according to the invention makes it possible to modify the magnetic compensation, by increasing or decreasing the intensity of the compensation current I 2 , to induce controlled MHD instabilities, these instabilities contributing to stir the alumina for a better yield.
  • Such a method is particularly interesting with the configuration of the electrical conductors described above which makes the tanks magnetically very stable.
  • the characteristics of the alumina analyzed can notably be the ability of the alumina to dissolve in the bath, the fluidity of the alumina, its solubility, its fluorine content, its humidity, etc.
  • the determination of a value of intensity of the compensation current required according to the characteristics of the analyzed alumina can be carried out in particular by use of an abacus, for example made by a person skilled in the art by experimentation and recording of the optimal correspondences intensity.
  • compensation current I 2 / characteristics of the alumina This is to quantify the desired MHD instabilities.
  • the alumina available for continuous operation of the smelter is of different quality, more or less pasty, and therefore having different abilities to dissolve in the electrolysis bath.
  • the movements of liquids in the electrolysis tanks are an asset, because they allow to stir this alumina to promote its dissolution.
  • the magnetic field at the origin of the movements of the liquids is directly compensated via the electrolysis current itself, with a distribution of the magnetic field imposed and frozen by the course of the routing conductors.
  • the figure 1 shows an aluminum smelter 100 of the state of the art.
  • the aluminum smelter 100 comprises electrolytic cells arranged transversely with respect to the length of the line that they form.
  • the tanks are here aligned in two rows 101, 102 parallel and traversed by an electrolysis current I 100 .
  • Two secondary electric circuits 104, 106 extend on the sides of the queues 101, 102 to compensate for the magnetic field generated by the circulation of the electrolysis current I 100 from one tank to another and in the neighboring line.
  • the secondary electric circuits 104, 106 are respectively traversed by currents I 104 , I 106 flowing in the same direction as the electrolysis current I 100 .
  • Power supply stations 108 supply the series of electrolysis cells and the secondary electrical circuits 104, 106.
  • the distance D 100 between the electrolysis cells closest to the power stations 108 and the stations 108 power supply is of the order of 45m
  • the distance D 300 on which the circuits 104, 106 electrical secondary beyond the end of the queue extends is of the order of 45m
  • the distance D 200 between the two rows 101, 102 is of the order of 85m to limit magnetic disturbances from one line to the other.
  • the figure 2 shows two tanks 200 of traditional electrolysis consecutive of the same line of tanks.
  • the electrolysis tank 200 comprises a box 201 internally lined with refractory materials 202, a cathode 204 and anodes 206 immersed in an electrolytic bath 208 at the bottom of which is formed a sheet 210 of aluminum.
  • the cathode 204 is electrically connected to cathode conductors 205 which pass through the sides of the box 201 at cathode outlets 212.
  • the cathode outputs 212 are connected to routing conductors 214 which convey the electrolysis current to the conductors 213.
  • these rising and connecting conductors 213 extend on one side only, the upstream side, of the electrolytic tank 200 and extend above the anodes 206, up to the part longitudinal center of the tank.
  • the figure 3 schematically illustrates the path traveled by the electrolysis current I 100 in each of the tanks 200 and between two adjacent tanks such as those shown in FIG. figure 2 .
  • the rise of the electrolysis current I 100 to the anode assembly of a tank is asymmetrical since this rise is carried out only upstream of the tanks in the overall flow direction of the electrolysis current I 100 in the queue (to the left of the tanks on the Figures 2 and 3 ).
  • the figure 4 shows a sectional view of a traditional tank 200, in which there is the arrangement on the sides of the tank 200 of the electrical conductors forming the secondary electrical circuits 104, 106 to compensate for the magnetic field generated by the current flow I 100 electrolysis of a tank 200 to another and in the neighboring queue.
  • the figure 5 shows an aluminum smelter 1 according to one embodiment of the invention.
  • the aluminum smelter 1 comprises a plurality of substantially rectangular electrolysis tanks 50 intended for the production of aluminum by electrolysis, which can be aligned along one or more queues, in this case two queues, substantially parallel, connected in series. and supplied with current I 1 electrolysis.
  • electrolysis tanks 50 are arranged transversely with respect to the line they form. It will be noted that per electrolysis tank 50 arranged transversely is meant electrolysis tank 50, the largest dimension of which, the length, is substantially perpendicular to the overall direction in which the electrolysis current I 1 flows, that is to say to say to the flow direction of the electrolysis current I 1 at the level of the rows of electrolysis tanks 50.
  • the aluminum smelter 1 also comprises an electric compensation circuit 6, traversed by a compensation current I 2 .
  • a compensation current I 2 Unlike circuits 104, 106 illustrated on the figure 1 it is important to note that the electric compensation circuit 6 extends under the electrolysis tanks 50. It will also be noted that the compensation current I 2 flows in the opposite direction of the electrolysis current I 1 .
  • the electric compensation circuit 6 of the figure 5 more particularly form a loop under the rows of electrolysis tanks 50.
  • a set of supply stations 8 independently feeds the electrolysis tanks 50 and the electric compensation circuit 6.
  • the electric compensation circuit 6 is a secondary electric circuit of compensation distinct from the main electric circuit 7 traversed by the current I 1 of electrolysis.
  • the intensity of the compensation current I 2 is variable, independently of the electrolysis current I 1 .
  • the intensity of the compensation current I 2 can be modified without the intensity of the electrolysis current I 1 necessarily being so.
  • the figure 8 shows three consecutive electrolysis tanks 50 of the aluminum plant 1.
  • the electrolysis tanks 50 can conventionally comprise a box 60, provided with cradles of reinforcements 61, which may be metallic, for example steel, and an inner coating 62 refractory materials.
  • the electrolytic cells 50 comprise a plurality of anode assemblies consisting of a support 53 (here a transverse horizontal bar) and at least one anode 52, in particular of carbon material and more particularly of precooked type, conductors 54 of mounted and connected which, unlike the electrolysis tank 200, extend on either side of each of the electrolysis tanks 50 to conduct the current I 1 electrolysis to the anodes 52, and a cathode 56, optionally formed of several cathode blocks of carbon material, crossed by cathode conductors 55 for collecting the electrolysis current I 1 to lead to cathode outlets 58 leaving the bottom of the box 60 and connected to conductors 57 routing in turn leading the electrolysis current to the conductors 54 for mounting and connection of the next electrolysis tank 50.
  • the anode assemblies are intended to be removed and replaced periodically when the anodes are worn.
  • the cathode conductors, the cathode outputs and the routing conductors 57 may correspond to metal bars, for example aluminum, copper and / or steel.
  • the figure 6 schematically represents the path of the electrolysis current I 1 in two successive electrolysis tanks 50 of the aluminum plant 1 according to the invention.
  • the rise of the electrolysis current I 1 is here advantageously carried out on both longitudinal sides of the electrolytic cell 50.
  • the figure 9 represents schematically the path of the electrolysis current I 1 in two successive electrolysis tanks 50 of the aluminum plant 1 according to the invention and differs from the figure 6 in that the cathode outputs 58 come out of the box 60 more conventionally at the sides of the box 60.
  • the figure 7 shows a sectional view of an electrolysis tank 50 of the aluminum plant 1. Note also the presence of the compensation circuit 6, under the electrolysis tanks 50, and traversed by the current I 2 compensation circulating in the direction inverse of the global circulation direction of the electrolysis current I 1 from one tank 50 to the next.
  • the compensation circuit 6 forms, according to the example of the figure 7 a layer of three conductors substantially equidistant and arranged in the same substantially horizontal plane XY; in addition, the conductors of this layer may extend substantially symmetrically with respect to a transverse median plane XZ.
  • the circuit of electrical conductors of the tank, and of the smelter can advantageously be made in a modular manner.
  • the figure 7 shows in particular a tank formed of three identical modules M.
  • each module comprises the routing conductors 57 disposed between three adjacent cradles 61 of the box and a conductor of the compensation circuit 6 disposed substantially under the central cradle 61 of the module.
  • the conductor of the module compensation circuit 6 is traversed by a current of the order of 50% to 150% of the intensity of the electrolysis current corresponding to this module.
  • the stability of the tank does not depend on the number of modules forming the circuit of electrical conductors of the tank and the smelter.
  • the length and intensity of the tanks can be adjusted simply by adding modules to meet the desired conditions of realization of the smelter.
  • the rising and connecting conductors 54 extend upwards, for example substantially vertically, along each longitudinal edge of the electrolysis cells 50.
  • the longitudinal edges of the electrolysis tanks 50 correspond to the edges of larger dimension, substantially perpendicular to the transverse X direction.
  • the rising and connecting conductors 54 upstream and downstream may also be arranged equidistant from a median YZ plane of the electrolysis tank 50.
  • the rising and upstream connection conductors 54 may be substantially symmetrical to the downstream electrical conductors 54 relative to the median YZ plane of the electrolysis cells 50.
  • the conductors 54 upstream and connecting upstream of one of the electrolysis tanks 50 may be arranged in staggered relation to the conductors 54 of upstream and downstream connection of the electrolysis tank 50 preceding it in the line.
  • the figure 8 also shows that the conductors 54 of rise and connection extend on either side of the box 60 without extending to the right of the anodes 52, that is to say without extending into a vertically projected volume of the area of the anodes in a horizontal plane.
  • the electrical conductors 54 of rise and connection extend above the liquids 63 at a height h between 0 and 1.5 meters.
  • the support 53 of the anode assembly comprises a cross member extending transversely with respect to the electrolytic cell 50 being supported and electrically connected at each of the two longitudinal edges on either side of the vessel. 50 electrolysis.
  • the distribution of electrolysis current I 1 between the conductors 54 for upstream and upstream connection of the electrolysis tanks 50 and the conductors 54 for upstream and downstream connection of the electrolysis tanks 50 may be, for example, 30% to 70% upstream and 70% to 30% downstream respectively.
  • this current distribution is 40% to 60% upstream and 60% to 40% downstream, and preferably 45% to 55% upstream and 55% to 45% respectively.
  • 'downstream In other words, it is of the order of 50% plus or minus 20% upstream and the remainder downstream, and preferably of the order of 50% plus or minus 10%, and more preferably of the order of 50% plus or minus 5%.
  • the cathode outputs 58 and the routing conductors 57 may extend only in a vertical plane XZ perpendicular to the longitudinal direction Y of the electrolysis vessels 50.
  • the cathode outputs 58 may extend substantially vertically only.
  • the cathode outlets 58 may pass through the bottom of the box 60 of the electrolysis tanks 50, and the routing conductors 57 may extend under the electrolysis tanks 50, advantageously in a straight line, substantially parallel to a transverse direction.
  • the longitudinal opposites of the electrolysis tanks 50 make it possible to stabilize the liquids contained in the electrolysis tanks 50 and to limit the disturbances of the electrolysis tanks 50 at the end of the line because the magnetic fields generated by the electrolytic cells 50 electrolysis current passing under the tanks and the conductors of the compensation electric circuit are canceled.
  • the intensity of the compensation current flowing through the compensation circuit is advantageously of the order of 50% to 150% of the intensity of the electrolysis current I 1 , preferably of the order of 70% to 130% of the current.
  • intensity of the electrolysis current I 1 and more preferably of the order of 80% to 120% of the intensity of the electrolysis current I 1 , in order to ensure an appropriate cancellation of the magnetic fields and the stability of the tanks.
  • the distances between the queues, and the lengths of the electrolysis electric circuit and the electric compensation circuit 6, can be reduced.
  • the distance D 1 between the electrolysis tanks 50 closest to the supply stations 8 and / or the distance D 3 over which the electrical compensation circuit 6 extends beyond the ends of the line is less than or equal to at 30m, for example less than or equal to 20m, and preferably less than or equal to 10m;
  • the distance D 2 between the two rows is less than or equal to 40m, for example less than or equal to 30m, and preferably less than or equal to 25m.
  • the two rows of the aluminum smelter 1 according to the invention can be arranged in the same building 12, which allows very significant structural gains.
  • the electric compensation circuit 6 extends under the tanks 50 forming a sheet of two to twelve, preferably three to ten, substantially equidistant parallel electrical conductors distributed substantially symmetrically with respect to a transverse median axis X of the tanks 50.
  • the compensation current I 2 traversing, for example, evenly across the conductors of this layer of parallel conductors is thus better distributed over the entire length of the tank 50.
  • the magnetic fields generated by the routing conductors 57 traversed by the current I 1 of electrolysis, themselves distributed under the tank 50 over its entire length, are thus better compensated.
  • the electrical conductor or conductors forming the electrical compensation circuit 6 extend under the rows of tanks 50 substantially parallel to a transverse axis X of the electrolysis tanks 50.
  • the compensation circuit 6 may be formed by electrical conductors forming a plurality of independent secondary secondary electric compensation sub-circuits and each traversed by a compensation current flowing in the opposite direction of the current I 1 d 'electrolysis.
  • the secondary electrical compensation sub-circuits can form parallel loops under the electrolysis tanks 50, for example two in the case of the figure 5 . So, in case of piercing an electrolytic tank 50, if one of the subcircuits is reached, the other secondary electrical compensation sub-circuit (s) may continue to compensate for the magnetic field.
  • the electrical conductors of the compensation circuit 6, or if appropriate of one of the secondary electrical compensation sub-circuits may perform several turns in parallel and / or in series under the electrolysis cells, in particular when these Electrical conductors are made of superconducting material.
  • the electrical conductors forming the compensation circuit 6 may correspond to metal bars, for example aluminum, copper or steel, or, advantageously, to electrical conductors made of superconducting material, the latter making it possible to reduce the power consumption and because of their smaller mass than the equivalent metal conductors, to reduce structural costs to support them or to protect them from possible metal pouring by means of metal baffles.
  • these electrical conductors made of superconducting material can be arranged to perform several turns in series under the row or rows of tanks.
  • the sum of the intensities going through all the conductors of the compensation electric circuit passing under the tank is advantageously of the order of 50% to 150% of the intensity of the electrolysis current I 1 , preferably of the order of 70%. at 130% of the intensity of the electrolysis current I 1 , and more preferably of the order of 80% to 120% of the intensity of the electrolysis current I 1 .
  • the intensity of the compensation current flowing through this compensation electric circuit 6 may be of the order of 50%. at 150% of the intensity of the electrolysis current I 1 . If this secondary electric compensation circuit 6 forms N turns under the electrolysis tanks 50, then the sum of the N intensities crossing each of these turns is of the order of 50% to 150% of the intensity of the electrolysis current. Also, according to the example of figure 5 , The current I 2 corresponding to the sum of the intensities I 20 and I 21 passing through each of the two towers can be of the order of 50% to 150% of the intensity of the current I 1 of electrolysis.
  • the invention also relates to a method for stirring alumina in the electrolysis tanks 50 of the aluminum plant 1.
  • This method comprises a step of modulating the intensity of the compensation current flowing through the electric compensation circuit 6, or where appropriate compensation currents flowing through the subcircuits forming it.
  • This modulation may more particularly be a function of the characteristics of alumina, varying the intensity of the electrolysis current or structural modifications of the smelter.

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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)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
EP14834860.0A 2013-08-09 2014-07-30 Aluminerie comprenant un circuit électrique de compensation Active EP3030695B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
SI201431028T SI3030695T1 (sl) 2013-08-09 2014-07-30 Talilnica aluminija s kompenzacijskim električnim vezjem

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR1301910A FR3009564A1 (fr) 2013-08-09 2013-08-09 Aluminerie comprenant un circuit electrique de compensation
PCT/CA2014/050722 WO2015017924A1 (fr) 2013-08-09 2014-07-30 Aluminerie comprenant un circuit électrique de compensation

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EP3030695A1 EP3030695A1 (fr) 2016-06-15
EP3030695A4 EP3030695A4 (fr) 2017-03-29
EP3030695B1 true EP3030695B1 (fr) 2018-10-17

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US (1) US10344390B2 (tr)
EP (1) EP3030695B1 (tr)
CN (1) CN105452536B (tr)
AR (3) AR097248A1 (tr)
AU (1) AU2014305613B2 (tr)
BR (1) BR112016001961A2 (tr)
CA (1) CA2919050C (tr)
DK (1) DK179170B1 (tr)
EA (1) EA030271B1 (tr)
FR (1) FR3009564A1 (tr)
MY (1) MY178282A (tr)
SI (1) SI3030695T1 (tr)
TR (1) TR201821117T4 (tr)
WO (1) WO2015017924A1 (tr)

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Publication number Priority date Publication date Assignee Title
MY183698A (en) 2015-02-09 2021-03-08 Rio Tinto Alcan Int Ltd Aluminium smelter and method to compensate for a magnetic field created by the circulation of the electrolysis current of said aluminium smelter
WO2017020123A1 (en) * 2015-08-06 2017-02-09 9320-0145 Québec Inc. Electrical connector system for electrolysis cell of aluminum production plant and method of using same
US20170073829A1 (en) * 2015-09-14 2017-03-16 Siemens Aktiengesellschaft Method for reducing the formation of fluorocarbons in molten salt electrolysis
RU2678624C1 (ru) * 2017-12-29 2019-01-30 Общество с ограниченной ответственностью "Объединенная Компания РУСАЛ Инженерно-технологический центр" Ошиновка модульная для серий алюминиевых электролизеров

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NO139829C (no) * 1977-10-19 1979-05-16 Ardal Og Sunndal Verk Anordning for kompensering av skadelig magnetisk paavirkning mellom to eller flere rekker av tverrstilte elektrolyseovner for smelteelektrolytisk fremstilling av aluminium
FR2425482A1 (fr) 1978-05-11 1979-12-07 Pechiney Aluminium Procede de compensation du champ magnetique induit par la file voisine dans les series de cuves d'electrolyse a haute intensite
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FR2868436B1 (fr) 2004-04-02 2006-05-26 Aluminium Pechiney Soc Par Act Serie de cellules d'electrolyse pour la production d'aluminium comportant des moyens pour equilibrer les champs magnetiques en extremite de file
NO322258B1 (no) * 2004-09-23 2006-09-04 Norsk Hydro As En fremgangsmate for elektrisk kobling og magnetisk kompensasjon av reduksjonsceller for aluminium, og et system for dette
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Also Published As

Publication number Publication date
WO2015017924A1 (fr) 2015-02-12
FR3009564A1 (fr) 2015-02-13
CN105452536B (zh) 2017-09-19
DK201670126A1 (en) 2016-03-14
BR112016001961A2 (pt) 2017-08-01
EA030271B1 (ru) 2018-07-31
DK179170B1 (en) 2018-01-02
US10344390B2 (en) 2019-07-09
EA201690339A1 (ru) 2016-06-30
CA2919050A1 (fr) 2015-02-12
AR097247A1 (es) 2016-03-02
TR201821117T4 (tr) 2019-02-21
EP3030695A1 (fr) 2016-06-15
CA2919050C (fr) 2021-03-30
AR097246A1 (es) 2016-03-02
AU2014305613B2 (en) 2017-08-31
AR097248A1 (es) 2016-03-02
CN105452536A (zh) 2016-03-30
MY178282A (en) 2020-10-07
SI3030695T1 (sl) 2019-02-28
US20160201208A1 (en) 2016-07-14
EP3030695A4 (fr) 2017-03-29
AU2014305613A1 (en) 2016-02-11

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