MXPA06009412A - Process and plant for electrodepositing copper - Google Patents

Abstract

The present invention relates to a process for electrochemically winning or refining copper by electrodepositing copper from an electrolyte solution containing the metal in ionogenic form, in which the electrolyte is passed through an electrolysis plant compris-ing at least one electrolytic cell, which in an electrolyte tank for receiving the electrolyte has at least two electrodes serving as anode and cathode, which are alternately ar-ranged at a distance from each other, and to a corresponding plant. To increase the economic efficiency of such processes and plants, it is proposed in accordance with the invention to immerse the at least one cathode during operation of the electrolysis into the electrolyte over a length of at least 1.2 meters.

Description

PROCESS AND PLANT FOR THE ELECTROLYTIC DEPOSIT OF COPPER Field of the Invention The present invention relates to a process for the electrochemical refining or extraction of copper by the electrolytic deposition of copper from an electrolyte solution containing the metal in an ionogenic form, in which the electrolyte is passed through an electrolysis plant comprising at least one electrolytic cell, in which an electrolyte tank for receiving the electrolyte has at least two electrodes that serve as an anode and cathode, which are alternately placed at a certain distance from one another; as well as a corresponding plant.

BACKGROUND OF THE INVENTION A multitude of processes are known to produce copper, particularly pyrometallurgical and hydrometallurgical processes. In the pyrometallurgical processes an enriched copper pyrite is melted in a suspension furnace or a bath type melting furnace by adding oxygen to obtain a copper matrix, in the converters it is then converted to raw copper in two blow stages , and is further purified in a final step of electrolytic refining. This electrolysis is also known as refining electrolysis. In hydrometallurgical processes, on the other hand, particularly oxidized low-copper ores, with a copper content of about 0.5 to 1% by weight are used as starting materials. The low-copper start ore, which due to its mineral composition can not always be processed economically by means of other processes such as flotation, is leached for example with dilute sulfuric acid, and in an extraction plant the resulting rich solution in copper it is treated with an organic extractant which selectively extracts the copper ions from the solution. Subsequently, the extractant containing copper is subjected to desorption with an impure electrolyte with a copper content of about 30 to 40 g / l, which originates from the successive electrolysis plant, the copper from the extraction phase that passes inside the electrolyte, which with additional purification to remove extractant residues and solids generally, is recirculated to the electrolysis plant with a copper content of 40 to 50 g l. Said electrolysis is also referred to as extraction electrolysis. During the electrolysis operation, the copper ions are reduced in the cathodes and deposited as elemental copper. The conventional electrolysis plants for the electrolytic copper extraction, as described for example in JA Wells and WR Snelgrove, The Design and Engineering of Copper Electrowinning Tankhouses, Proceedings of the International Symposium on Electrometallurgical Plant Practice, Pergamon Press, 1990, pages 57 a 72 [The Design and Engineering of Tank Houses for Copper Electrolytic Extraction, Memoirs of the International Symposium on the Practice of Metallurgical Plants] comprises up to 188 electrolytic cells, each of which has between 20 and 60 cathodes, mainly made of stainless steel, as well as a corresponding number of anodes. At predetermined distances, depending on the size of the plant, the copper-coated cathodes are removed from the electrolytic cell manually or by means of cranes and transferred to a desorption plant, in which the copper coatings are debarked (desorbed) from the cathodes, before the cathode start sheets are returned to the electrolyte cells after their corresponding subsequent treatment. The desorbed copper is finally processed in foundry furnaces. For an efficient after-treatment of the copper-charged cathodes, in particular for debarking the copper deposited in the desorption machine, a rather uniform deposition of the copper on the cathodes is desirable, based on the surface area of the cathodes. This is only ensured with a more efficient distribution line along the length of the cathodes. As described, for example, in A. Schmidt, Angewandte Elektrochemie [Applied Electrochemistry], Verlang Chemie 1976, pages 49 to 51, the uniformity of the most efficient distribution with a given electrolyte conductivity is, however, increased with a decreasing width and with a particular length of the electrode surface immersed in the electrolyte. Additionally, the most efficient distribution depends on the conductivity of the electrode material and the current density applied during electrolysis. Because of these relationships, both refining electrolysis and extraction electrolysis generally use electrodes with a surface area immersed to the maximum within the electrolyte of about 1x1 meters. The smelting furnaces for copper post processing are also adjusted to this size. Due to the high investment and high operating costs of the electrolysis plants and the cathode processing plants that comprise cranes and desorption machines, which were combined in the so-called tank house, attempts have already been made for enough time to increase the economic efficiency of both refining electrolysis and extraction electrolysis. This depends to a large extent on the efficiency of the electrolysis as well as on the number of cathode movements and thus on the amount of copper deposited per cathode. To increase the efficiency of electrolysis, it is highly desirable to increase the current density during electrolysis, with the purpose of achieving a higher deposition of copper in the cathodes per unit of time. However, the current density on the side of the cathode is limited by the quality of the deposited copper, since due to the increased overvoltage in the cathodes more impurities are deposited with an increasing current density. On the anode side, the lead alloy used as the electrode material for the extraction electrolysis becomes more unstable, and the copper anode used for the refining electrolysis becomes passive with increasing current density. As a result of these two effects, the current electrolysis operates with a maximum current density of about 370 jA7m2 of electrode surface. In extraction electrolysis, a higher current density can be achieved only by the use of expensive anode materials with a smaller amount of electrodeposited copper. In this way, a further reduction of production costs with a consistent quality of electrodeposited copper can only be achieved by reducing the specific investment and operating costs of the cathode processing plants comprising the crane and the processing machines. desorption, that is, by decreasing the necessary number of cathode movements based on the amount of electrodeposited copper per cathode.

Objective and Compendium of the Invention It is the objective of the present invention to increase the copper charge per cathode on the basis of the number of cathode movements with a consistent quality of the electrodeposited copper. According to the invention, this objective is solved by a process and a plant with the features of claims 1 and 23, respectively. Preferred embodiments of the invention are apparent from the appended claims. Surprisingly, it can be found according to the present invention that - contrary to the prejudice existing among experts that electrodes with an electrolyte immersion surface of more than 1 x 1 meter, and in particular electrodes with a depth of immersion of more than 1 meter, they are not suitable for copper extraction due to the uneven and more efficient distribution that is necessarily obtained in the electrodes - a depth of electrolyte immersion of the electrodes of more than 1.2 m leads to a sufficiently uniform deposit copper on the cathodes in processes for the electrolytic deposition of copper from an electrolyte solution containing the metal in an ionogenic manner also with the cathode materials commonly employed in refining and extraction electrolysis and with the current densities commonly adjusted. Here also, an efficient processing of the charged cathodes, in particular a desorption of the deposited copper, is possible with the known processing techniques. In the process of the invention, more copper is produced by the movement of the cathode than in known processes with a consistent quality of the electrodeposited copper due to the greater depth of the electrolyte immersion, so that the costs per ton of copper extracted can be decreased dramatically. During the electrolysis operation, the immersion depth of the electrodes within the electrolyte is preferably an integer multiple of the immersion depth commonly used of about 1 m and particularly preferably to about 2 m with a cathode width of about 1 m each. The advantage is that the melting furnaces, which due to the active surface of the cathode, that is, the surface of the cathode immersed in the electrolyte, were normally designed for a size of lxl meters in the known processes, can be used without changes , in which the desorbed copper sheets to be obtained with the processes according to the invention are reduced to the corresponding size of lxl meters subsequent to the desorption operation and before being supplied to the melting furnace. With an active electrode length of 2 meters, this can easily be achieved in such a way that for example the copper sheets are bent in the middle part and are bent in the flexural surface. It is similarly possible to obtain two cathode sheets each separated by one meter during the desorption operation, for example, by a circumferential region horizontally isolated and provided around the level of half the height of the cathode, so that another fold or reduction in size is superfluously made. Finally, a mechanical separation is also possible. According to a development of the invention, it is proposed that at least one electrolytic cell has more than 60 cathodes, particularly preferably more than 100 cathodes, and more preferably and particularly 114 cathodes. As a result, the efficiency of the process of the invention is further increased, since the size of the electrolytic cells caused by this measurement provides a less expensive transport while at the same time reducing the number of cells per production capacity. This brings us to smaller tank houses, shorter distribution trajectories and less dispersed currents. In principle, cathodes can be made of all materials known to people trained for this purpose, the stainless steel cathodes are preferred. It turned out to be advantageous to carry out the electrolysis with a current density as used in the known processes, preferably with a current density of more than 200 A / m 2, and particularly preferably with a current density of between 250 and 370. A / m2. In this way, the deposit of larger amounts of impurities on the cathodes is avoided and the copper is produced with the required quality. Due to the greater electrode length and surface area, higher specific current intensities, ie, higher current intensities per electrode, are obtained in the process of the invention when compared to prior art processes. While in the processes mentioned at the end with cathodes and anodes of an electrode active surface of lxl meter each, the specific current intensity is 740 A per electrode with a current density of 370 A / m2, the current intensity specific is duplicated according to the invention at 1480 A per electrode when electrodes with an active surface of 1x2 meters are used. In the processes of the invention, the electrodes can in principle be placed in the electrolytic cells, be fixed and supplied with current in any manner known to those skilled in the art. However, electrodes with a horizontal suspension bar known per se, which has a first end and a second end and which is preferably made of the same material as the cathode surface, in particular steel, turned out to be advantageous. For the power supply, one end of the cathode suspension bar rests on a first contact bar connected to a power source, while one end of each of the anode suspension bar each is on contact with a second contact bar connected to the power source. Preferably, the two contact rods are arranged in a contact bar each, which are provided on the edge of the electrolyte tank. The respective second ends of the suspension rods of the electrodes can rest on a support surface of an insulating material, which for example is arranged in a similar manner in the contact rods. According to a particular embodiment of the present invention, the electrodes have the first end of their suspension bar each resting on one of the two contact rods by means of a two-line contact. This is advantageous in particular because due to the higher specific current densities in the process of the invention higher currents must be transmitted from the contact rods to the electrodes, which can be carried out more effectively with two-line contacts due to the largest contact surface. For this purpose, a contact bar with at least one substantially trapezoidal groove is used particularly preferably, on which the first end of the suspension bar is applied with a contact surface having at least a substantially rectangular cross section. The contact of two lines can also, of course, be made in any other way known to a person trained for this purpose. To ensure a rather leak-free current transmission between the contact rods and the cathodes, which are for example made of stainless steel, also at high specific current intensities, the process of the invention preferably employs cathodes whose, for example, , suspension bar sheathed with steel has a copper core. Due to the high electrical conductivity of the copper, the current thus transmitted from the contact rod to the suspension bar is transmitted to the active surface of the electrode only with minimal losses, while the steel cover surface of the suspension bar provides the suspension bar in particular with high mechanical strength and high corrosion resistance. Based on its cross section, the copper core preferably has the same geometry as the suspension bar. In this case a suspension bar made of steel, which for example is substantially square in cross section, similarly includes a substantially square copper core. According to a development of the invention it is proposed that it has the respectively second end of the suspension bar of the cathodes resting on a leveling bar preferably placed on one of the two contact rods, regardless of whether the contact of the other ends of the suspension bar with the contact rods is effected by means of a contact of a line or two contact lines or any other contact in any way. The advantage of this method is that the cathodes in this way have two electrical contacts, that is, on the one hand, with a contact bar and, on the other hand, with a leveling bar, by means of which the distribution The current between the electrodes is more uniform. This is particularly convenient with high specific current currents, in order to minimize transfer resistance and electrical losses. For the same reasons, it is preferred in the process of the invention that the second end of the suspension rod of the anodes also be held on an anode leveling bar separate from the cathode leveling bar. According to a particular embodiment of the present invention, the contact rods and / or possibly the leveling rod or, particularly and preferably, the intermediate contact rods, over which the contact rods and possibly the leveling rods are placed, they are cooled during the electrolysis, in order to avoid a loss of energy, which results from a high specific current intensity and the high related current load, and a heating of the corresponding bus bars. For this purpose, cooling by means of water of the conductor bars was found to be particularly convenient, which is carried out, for example, by the passage of cooling water through a chill water channel in the conductor bars. Good results are achieved in particular with water channels having a diameter of about 15 to 20 mm. Extruded conductor bars with embedded cooling channels are preferably used for this purpose, although good results are also achieved with conductive bars with milled grooves, which are subsequently covered and welded, or with welded copper pipes. To provide water to the corresponding bus bars, PVC pipes or vinyl material nozzles turned out to be particularly useful. In order to achieve an efficient heat exchange between the conductive bars and the cooling water, it is proposed according to the invention to pass the cooling water through the cooling water channels with a sufficient speed to maintain a turbulent water flow, in where a speed of about 1.5 ms must, however, not be exceeded. According to the invention, the supply of cooling water can also be effected by means of two cooling circuits divided into a primary circuit, which at least partially extends through the intermediate conductor bars to be cooled, and a secondary circuit, which preferably preferably extends completely outside the conductive bars that are to be cooled. The connection of the two circuits can be effected in any manner known to those skilled in the art. Particularly, tube and shell heat exchangers as well as plate type heat exchangers proved to be useful. Particular and preferably, the primary circuit extends exclusively through the conductive bars that are to be cooled and is operated a high purity cooling water, for example purified water by means of a reverse osmosis plant, while the secondary circuit is fed raw water and is re-cooled, for example, by means of an atmospheric cooling tower. To ensure that the primary circuit is always filled cooling water, it preferably includes a water expansion tank.

According to a development of the invention, it is proposed to provide a fluid distributor in the at least one electrolytic cell, through which during the operation of the extraction electrolysis a liquid, a gas, a gas mixture or a gas mixture and liquid is introduced, particularly and preferably from below, into the electrolytic cell. Due to the convection flow generated by said introduction of fluid a better intermixing of the electrolyte is achieved, which is why the copper is deposited on the cathodes in a more uniform manner. In addition, the convection flow makes a reduction in the thickness of the boundary layers at the electrodes, which results in a better and faster mass transfer of the copper ions to the electrode surface. An introduction of fluid from below into the electrolytic cell is particularly preferred, because in the upper region of the cell a certain convection flow is obtained automatically due to the gas bubbles released at the anode during the extraction electrolysis, and therefore, in particular in the lower region of the electrolytic cell an additional convection flow is important. Preferably, the electrolyte solution or a mixture of electrolyte solution and gas bubbles are introduced into the electrolytic cell through the fluid distributor. Because the electrolyte is continuously regenerated with copper sulphate from the leaching plant, it must in any case be supplied to the electrolytic cell during the electrolysis operation, the fluid supply system does not require an increase in the investment or in the operating costs in the first case and only a negligible increase in this in the second case. To increase convection, other liquids, gases or gas mixtures can also be supplied to the electrolytic cell instead of electrolyte solution or a mixture of electrolyte solution and gas bubbles, or other systems such as mechanical mixing devices or the application of ultrasound can be used. According to a particular embodiment of the present invention, the fluid distributor, as it is of a simple construction and efficient in terms of operating costs, consists of two tubes arranged substantially parallel to the longitudinal sides of the electrolytic cells, which in their surfaces each have one or more fluid outlet holes. The tubes are arranged at a small distance from the side wall. The distance is defined by the tube clamping mechanism in the wall of the cell and is provided for depositing sediments in the bottom of the cell. Typically, the distance is 10 to 50 mm. The distance of the two tubes from the bottom of the cell should be chosen so that the sediments of the electrolyte can be collected under the fluid distributor at the bottom of the cell. Typically the distance from the bottom of the cell is 100-200 mm. As a conduit for the supply of fluid to the fluid distributor, for example, a tube placed in the middle of the terminal face of the electrolytic cell can be used, which with respect to the electrolytic cell extends vertically from the top towards the bottom and at its lower end it branches into two tubes extending horizontally and in parallel to the terminal face of the electrolytic cell, one of whose tubes is connected to one end of the tubes of the fluid distributor, which extends substantially in parallel to the longitudinal sides of the electrolytic cells. To achieve an effective convection flow, the fluid distributor must have a high enough number of fluid outlet holes. In accordance with the present invention it was found that for this purpose the relative number of fluid outlet holes with respect to the total number of electrode pairs per electrolytic cell is decisive. Preferably, the fluid distributor has 1-5, particularly preferably about 1-2 fluid outlet holes per pair of electrodes and cell side provided in the electrolytic cell. The shape of the fluid outlet orifices is less decisive in terms of the convection flow. However, it proved to be advantageous to provide substantially circular fluid outlet holes. However, what influences the quality of convection flow achieved much more is the cross-sectional area of the fluid outlet holes. In the case of circular fluid outlet holes, the diameter thereof is preferably 1 to 10 mm, particularly preferably 5 to 7 mm, and in particular about 6 mm. According to a development of the invention, it is proposed to provide at least two electrolyte outlets per electrolytic cell, in order to achieve a problem-free overflow and promote a uniform distribution of the electrolyte in the electrolytic cell. According to a particular embodiment of the present invention, the cathodes used have a V-shaped cross-section in their lower longitudinal edge. In this way, a densification of current lines that necessarily occurs on straight edges, which leads to an -no desirable- increase in the copper deposit at the edges, can be reduced and optimally even be completely avoided. During the desorption, the notch also performs a separation of the front and rear sides deposited on the cathode in two cathode sheets. The grant will be subsequently explained in detail with reference to the modalities and drawings. All the features, per se or in any combination, constitute the subject of the invention, independently of their inclusion in the claims or their references.

Brief Description of the Drawings Figure 1 shows the basic structure of an electrolysis plant for copper extraction or refining. Figure 2 shows a section along line A-A in Figure 1; Figure 3 shows schematically a section through an electrolytic cell with a cathode supported by a suspension bar; Figure 4 shows schematically a section through an electrolytic cell with an anode supported by a suspension bar; Figure 5 schematically shows contacts of two lines between the suspension bar and a contact bar; Figure 6 schematically shows contacts of a line between the suspension bar and a contact bar with a leveling bar; and Figure 7 shows schematically the structure of a pilot plant to carry out the process of the invention.

Description of Preferred Modes In the electrolysis plant for the extraction or refining of copper, which is illustrated schematically in Figures 1 and 2, the electrolytic cells 1 (dimensions L x W x H, for example, approximately 12.5 x 2 x 2.7 meters) each with the plurality of, for example, 115 anodes 2 and 114 cathodes 3, each of which is placed alternately and are held at the edges of the electrolytic cells 1 by means of suspension rods 4, are provided in numerous rows of cells.

By means of a crane 5, the suspension bar 4 with the electrodes suspended thereon can be transported between the maintenance area 6 for the anodes 2, the cells 1 as well as the desorption machine 7, in which the copper deposited in the cathodes 3 is desorbed in a manner known per se. Figure 3 schematically shows a cathode 3 resting on the edges of the electrolytic cell by means of the suspension bar 4. Correspondingly, Figure 4 shows an anode 2 which is maintained in a similar way by a suspension bar 4. The anode 2 additionally has holes 8 for spacers, which ensure that the uniform distance required between anodes and cathodes is, for example, 50 mm between each. By means of a contact 9 of two lines, one end of the suspension bars 4 rests on a contact rod 10 placed on the edge of the electrolyte cell (Fig. 5), which is connected to a non-energy source. illustrated by means of a conductive bar. The other end of the suspension bar 4 rests on a leveling bar 11. In general, this is effected by means of a one-line contact. (Fig. 6). With the process according to the invention, which is characterized by a high specific current intensity - based on the electrodes - more copper is produced than in the known processes due to the greater depth of electrolyte immersion of the cathodes by movement of cathode with a consistent copper quality. A cathode with an active immersion surface increased to 2x1 m needs only to be removed from the electrolyte tank for processing after a 200 kg load of copper, while a conventional prior art cathode of lxl m must already be processed after the deposit of 100 kg of copper. In this way, the effort involved in the movements of the cathode is halved by a factor of 2, so that, based on the same amount of copper produced, correspondingly fewer or smaller crane systems are required, for example one instead of two cranes to handle the electrodes, a smaller number of desorption machines and in this way a smaller production area and less personnel. The floor area required for the assembly of the electrolytic cells in the house tanks is drastically reduced as well. In the process according to the invention, on the other hand, different contact rods and possibly leveling bars are required due to the higher specific current intensity, and for the subsequent processing of the charged cathodes, crane systems with a higher load carrying capacity due to the higher weight of these cathodes are required. The height of the tank house between the upper cell edge and the crane route must be adjusted for the processing of the extended cathodes, and the same is true for the mounting of the electrolytic cells with an increased overall height. Due to the larger cathode surface, desorption machines of different sizes are required as well as bending or fragmentation machines to bend the larger copper sheets before supplying them to a foundry furnace designed for conventional plants. Since both investment and operating costs for the measures mentioned above are lower than the corresponding savings achieved due to the lower number of cathode movements, a significant reduction in production costs is achieved in its entirety. On the basis of an annual production of 120,000 tons, a comparison of the processes of the invention, which is carried out with an active electrode surface of 2 x 1 m, against prior art processes carried out with a surface of the active electrode of 1 x 1 m, but with twice the number of electrodes with the same current density, produces the following characteristics: When the process of the invention is used, the investment costs for corresponding plants for electrochemical copper extraction in this way can be decreased by up to 20%, and production costs can be decreased by up to 10%.

Example In the test station to conduct verification tests on a pilot scale as shown in Figure 7, two electrolytic cells Ib are provided, connected in parallel with respect to the electrolyte source and a common electrolyte preparation as well as a circulation system. Both electrolytic cells are electrically connected in series (not shown). The electrolytic cell is equipped with two lead anodes (A, with a width of 0.5 m and a height of 2 m, submerged surface) and a centrally placed K cathode. The electrolytic cell Ib has 3 anodes (A, with a width of 0.5 m and a height of 1 m, submerged surface) and two K cathodes of equal size. The number and size of electrodes used leads to the fact that in the case of a series connection, equal current densities are achieved in both electrolytic cells. Both electrolytic cells are charged with the same amount of fresh electrolyte (20a and 20b). The incoming electrolyte flow is adjusted so that during a stationary operation of both electrolytic cells a copper reduction of about 1.5 g / l is obtained. The spent solution 21a and 21b, respectively, is supplied to the electrolyte circuit. It comprises a leaching tank 22 with agitation, in which the depleted amount of copper is compensated by the addition of copper oxide 23. The overflow of the leaching tank 22 (enriched electrolyte 25) is introduced into the tank 24 of the bomb. The pump vessel tank 24 is electrically heated by means of the heater 26 and stirred by means of a partial recirculation of the enriched electrolyte 25 S The pump 27 is used for the circulation of the electrolyte. In pilot tests, a synthetically produced sulfuric acid copper sulfate solution was used as an electrolyte. To improve the morphology of the cathode, a small amount of guar solution (not shown) was added to the reservoir tank 24. The current density used was 300 A / m2. Several tests were carried out, which took from 5 to 7 days. In all tests, cathodes of very good quality were produced in both cells. The copper quality achieved was independent of the cathode size. In all tests, a current efficiency was achieved > 90% (Table 1, all concentrations at the entrance of the cell, for example, cell la): List of Reference Numbers 1 Electrolytic cell 2 Anode 3 Cathode 4 Suspension bar 5 Crane 6 Maintenance area 7 Desorption machine 8 Holes 9 Two-line contact 10 Contact rail 11 Leveling bar 20a, b Fresh electrolyte 21a, b Decreased solution 22 Leaching tank 23 Copper oxide 24 Pump container tank ,25 'Enriched electrolyte 26 heater 27 pump A anode K cathode

Claims (33)

1. Claims 1. A process for the electrolytic deposition of copper from an electrolyte solution containing the metal in ionogenic form, in which the electrolyte is passed through an electrolysis plant comprising at least one electrolytic cell which in An electrolyte tank to receive the electrolyte has at least two electrodes that serve as an anode and cathode, which are placed alternately at a certain distance from each other, which is characterized in that during the operation of the electrolysis the at least one cathode is submerged inside the electrolyte over a length of at least 1.2 meters.
2. 2. The process as claimed in claim 1, characterized in that during the operation of the electrolysis the at least one cathode is immersed in the electrolyte over a length of about 2 meters or another integer multiple of one meter.
3. 3. The process of claim 1 or 2, characterized in that during the operation of the electrolysis the at least one cathode is submerged within the electrolyte with a cross-sectional area of 2 x 1 meters.
4. 4. The process as claimed in any of the preceding claims, characterized in that at least one electrolytic cell has more than 60 cathodes, particularly and preferably more than 100 cathodes, and more particularly and preferably 114 cathodes.
5. 5. The process as claimed in any of the preceding claims, characterized in that the electrolysis is carried out with a current density of more than 200 A / m2, particularly and preferably between 250 and 370 A / m2.
6. The process as claimed in any of the preceding claims, characterized in that the electrodes have a horizontal suspension bar with a first end and a second end and at the edge of the electrolyte tank two contact rods are provided, each connected to a source of energy, the first end of the suspension bar rests on one of the two contact rods by means of a two-line contact and the first end of the suspension rod of the anodes rests on the other of the two contact bars by means of a two-line contact.
7. 7. The process as claimed in claim 6, characterized in that each of the contact rods has at least one substantially trapezoidal groove on which the respective first ends of the suspension rods rest with a contact surface that it has when minus a substantially rectangular cross section.
8. The process as claimed in claim 6 or 7, characterized in that the suspension bar has a shell surface made of steel and a core made of copper.
9. The process as claimed in any of claims 6 to 8, characterized in that the second end of the cathode suspension bar rests on a cathode leveling bar which is placed on one of the two bars contact.
10. The process as claimed in any of claims 6 to 9, characterized in that the second end of the suspension rod of the anodes rests on the leveling bar of the anode, which is placed in one of the two bars contact.
11. 11. The process as claimed in any of the preceding claims, characterized in that the contact rods and / or the leveling bars or the intermediate contact rods are cooled by means of water.
12. 12. The process as claimed in claim 11, characterized in that the bars to be cooled are cooled by the passage of cooling water through a cooling water channel provided in the contact rods.
13. The process as claimed in claims 11 or 12, characterized in that the cooling water is passed through a chill water channel in a turbulent flow.
14. The process as claimed in any of claims 11 to 13, characterized in that the contact rods to be cooled have two separate cooling circuits, one of which (primary circuit) is at least partly supplied. in the contact rods that are going to be cooled, and which are both connected by means of a heat exchanger.
15. 15. The process claimed in claim 14, characterized in that the primary circuit is fed with purified water and the second cooling circuit (secondary circuit) is fed with raw water.
16. 16. The process as claimed in any of the preceding claims, characterized in that a fluid distributor is provided in the at least one electrolytic cell, through which during the operation of the electrolysis solution of the electrolysis, they introduce gas bubbles or a mixture of an electrolyte solution and gas bubbles are introduced into the electrolytic cell.
17. The process as claimed in claim 16, characterized in that the fluid distributor is located at the lower end of the electrolytic cell and that the fluid is introduced into the electrolytic cell through the distributor below or approximately at the level of the lower end of the electrodes.
18. 18. The process as claimed in claims 16 or 17, characterized in that the fluid distributor consists of two tubes placed substantially parallel to the longitudinal sides of the electrolytic cell, which on its surface each have one or more fluid outlet holes and whose first ends are connected with a fluid-supplying conduit.
19. The process as claimed in any of claims 16 to 18, characterized in that the fluid distributor has about 1 to 5, particularly preferably about 1-2 fluid outlet holes per pair of electrodes and one cell laterally provided in the electrolytic cell, whose placement is substantially adjusted to the spaces between the electrodes.
20. The process as claimed in any of claims 16 to 19, characterized in that the fluid outlet holes of the fluid manifold are of a substantially circular shape and have a diameter of 1 to 10 mm, particularly and preferably from 5 to 7 mm, and more particularly and preferably approximately 6 mm.
21. 21. The process claimed in any of the preceding claims, characterized in that each electrolytic cell has two electrolyte outlets.
22. 22. The process as claimed in any of the preceding claims, characterized in that the cathodes have a V-shaped notch in cross section at their longitudinal bottom edge.
23. 23. An electrolysis plant for the electrolytic deposit of copper from an electrolyte solution containing the metal in an ionogenic form, in particular to carry out a process as claimed in any of claims 1 to 22, comprising at least of an electrolytic cell (1) which includes an electrolyte tank to receive the electrolyte, at least two electrodes serving as anode (2) and cathode (3), which are placed alternately at a distance from each other and each it has a substantially horizontal suspension bar (4), as well as two contact rods (10) placed on the edge of the electrolyte tank, each of which has a contact bar that can be connected to a power source, in wherein at least one cathode (3) has a first end of its suspension bar (4) that rests on one of the two contact rods and the at least one anode (2) has a first end of its suspension bar (4) resting on the other of the two contact bars, characterized in that the first ends of the suspension bars (4) each rest on the contact rods by means of a contact of two lines ( 9), and in which at least one of the two contact bars (10) at least one leveling bar (11) is provided, on which rests a second end of the spacer bars (4) of the cathodes (3) and / or anodes (2).
24. 24. The electrolysis plant as claimed in claim 23, characterized in that in each of the two contact bars (10) at least one leveling bar (11) is provided, the respective second end of the suspension bars (4) of the cathodes (3) rests in a of the two leveling bars (11) and the respective second end of the suspension rods (4) of the anodes (2) rests on the other leveling bar (11).
25. 25. The electrolysis plant as claimed in claim 23 or 24, characterized in that each of the contact rods has a substantially trapezoidal notch, on which the first ends of the suspension rods respectively rest (4) of the electrodes with a contact surface having a substantially rectangular cross section.
26. 26. The electrolysis plant as claimed in any of claims 23 to 25, characterized in that at least one of the contact rods, the leveling bars and / or the intermediate rails is provided with a water channel of cooling.
27. 27. The electrolysis plant as claimed in claim 26, characterized in that the cooling water channel has a diameter of 15 to 20 mm.
28. 28. The electrolysis plant as claimed in claim 26 or 27, characterized in that to provide water, the conductor bars having a cooling water channel, are connected with a tube made of PVC or a hose made of vinyl material.
29. 29. The electrolysis plant as claimed in any of claims 26 to 28, characterized in that two separate cooling circuits, one of which (primary circuit) is at least partially provided in one of the conductive bars that is to be cooled, both cooling circuits are connected to each other by means of a heat exchanger.
30. 30. The electrolysis plant as claimed in claim 29, characterized in that the primary circuit comprises a water expansion tank.
31. 31. The electrolysis plant as claimed in any of the preceding claims, characterized in that a fluid distributor is provided within the electrolytic cell, particularly and preferably at the bottom within the electrolytic cell.
32. 32. The electrolysis plant as claimed in claim 31, characterized in that the fluid distributor consists of two tubes placed substantially parallel to the longitudinal sides of the electrolytic cell, each of which has on its surface one or more fluid outlet holes and whose first ends are connected to a conductor that supplies fluid.
33. 33. The electrolysis plant as claimed in claim 31 or 32, characterized in that the fluid distributor has about 1 to 5, particularly preferably about 1-2 fluid outlet holes per pair of electrodes provided in the electrolytic cell, whose placement is substantially adjusted to the spaces between the electrodes, which particularly and preferably have a circular shape and a diameter of 1 to 10 mm, particularly and preferably 5 to 7 mm, and in particular approximately 6 mm.