 Improvement of copper electrical refining
专利摘要:
A process for copper production is disclosed which comprises the electrofining of copper in an electrolytic cell, wherein? the voltage differential across the cell is maintained at less than 1.6 volts,? the anode comprises at most 98.0 wt.% copper and less than 1.00 wt.% iron,? the current density through the cell is at least 180 A / m² cathode area,? electrolyte is removed from the cell during operation at an average refresh rate of 30-1900% per hour, by flooding a first stream of electrolyte over a cell wall, and? a gas is introduced into the cell and bubbled through the electrolyte between anode and cathode. Further disclosed is a liquid molten metal composition suitable for copper anode electrorefining and comprising at least 90.10 wt.% And at most 97 wt.% Copper, at least 0.1 wt.% Nickel, at least 0. , 0001 wt% and less than 1.00 wt% iron, and 250-3000 ppm wt. oxygen. 公开号:BE1026286B1 申请号:E20195322 申请日:2019-05-16 公开日:2019-12-18 发明作者:Visscher Yves De；Mark Vandevelde；Bert Coletti；Jan Dirk A Goris；Charles Geenen；Rafilk Jerroudi 申请人:Metallo Belgium； IPC主号:
专利说明:
Improvement of copper electrical refining FIELD OF THE INVENTION The present invention relates to the production of copper from primary sources, i.e., new ore, and from secondary base materials, also referred to as recyclable materials, or from combinations thereof, by pyrometallurgical process steps. Recyclable materials can include by-products, waste materials and materials at the end of their life. More in particular, the invention relates to the further purification by electro-refining of anodes formed from a copper current obtained by pyrometallurgy, which stream comprises impurities. BACKGROUND OF THE INVENTION In the pyrometallurgical production of copper, other metals such as nickel, antimony, bismuth, tin and / or lead, and often also small amounts of precious metals (PMs), in particular silver (Ag), are present in many of the commercially interesting base materials, including both primary and secondary raw materials. Pyrometallurgical process steps are no longer able to economically purify their copper product stream to the high purity level of> 99.97% by weight that is currently required by markets, eg the purity of> 99.995% by weight required is to enable the drawing of very thin copper wire for electronic applications. The production process for copper metal includes 2019/5322 BE2019 / 5322 2, therefore, usually an electro-refining step, usually as the final step in the purification process. In the electro refining of copper, copper (mainly due to electrochemically induced “corrosion”) from a less pure copper anode, which generally contains about 99% by weight of Cu, is dissolved in an electrolyte (mainly according to the reaction Cu Cu 2+ + 2 e - ) and deposited again on a cathode (mainly via Cu 2+ + 2 e - Cu), whereby a copper layer of higher purity is formed (at least 99.97 wt% Cu and often up to 99.99% by weight of Cu). The electrolyte is usually based on sulfuric acid. These two chemical (half) reactions are characterized by a standard potential difference under ideal conditions of 0.377 volts. By keeping the voltage difference between anode and cathode within tight limits, the metal depositing on the cathode can be controlled such that it is almost exclusively copper. The other metals in solution should not deposit electrochemically. Because the two chemical half-reactions have opposite voltage differences, an electrical refining cell theoretically requires only a very small net voltage difference to function. However, due to various resistors in the circuit as a whole, an electro-refining cell in practice requires a voltage difference of at least 0.15 volts (V) or 150 mV from cathode to anode to be usable. The electro refining (ER) of copper clearly differs from the “electrowinning” (EW) of copper. In electrowinning, copper is dissolved in an acid solution in a first step by leaching the copper (only through chemical “corrosion”) from a solid base material such as copper ore. The electrolyte loaded with copper is then, possibly after the copper concentration has been increased, for example by extraction with the aid of an organic solvent, passed through an electrolytic cell with chemically inert anodes, the copper being deposited thanks to the electric current on the cathode. At the anode of an electrowinning cell, water is electrochemically split (2 H 2 O 4 H + + O 2 + 4 e - ), resulting in 2019/5322 the hydrogen ions (H + ) remain in solution and the oxygen atoms collect in gas bubbles that rise to the surface of the electrolyte. The electrons pass through the electrical circuit from the anode to the cathode, where they are made available to deposit the copper (mainly Cu 2+ + 2 e-Cu), such as in an ER cell. With EW, the two half-reactions are therefore not opposed to each other and have different standard potentials, with the result that the EW cell requires an absolute minimum theoretical net voltage difference of 0.892 volts. In addition to this theoretical minimum, the additional voltage differences that are required to overcome the over-potentials at the anode and cathode, and the voltage losses associated with the contact points and the ohmic resistance of the electrolyte are added. The voltage difference in operation over an EW cell is therefore significantly higher than over an ER cell, rather in the order of magnitude of 1.8 to 2.5 volts from anode to cathode. An electro refining cell is typically driven in such a way that a target current (A) or current density (A / m 2 ) for the installed cathode surface is maintained throughout the cell, primarily to maintain the target cathode weight production rate. However, additional electrical resistances are built up during operation, especially in the electrolyte bath. Because that effect leads in particular to an increase in the electrical resistance at the surface of the anode, this phenomenon is often referred to as "anode passivation". Various factors may play a role in this, (i) anode mucous particles that are formed and accumulate on the anode surface and hinder the flow of copper cations from anode to cathode, (ii) erosion of the anode, thereby increasing the distance between the electrodes, (iii) ) by the additives that are added to the electrolyte that impede the flow of cations through the electrolyte, and (iv) other mechanisms. In addition, higher current densities also accelerate the passivation of the anode. In view of the current operational objective of maintaining a constant current density throughout the cell, and consequently a constant cell productivity, the voltage difference between BE2019 / 5322 2019/5322 BE2019 / 5322 cathode and anode usually increased (automatically) to compensate for any increase in electrical resistance across the cell (I = V / R). A higher voltage difference and / or a higher current density, however, can also entail other, less desirable effects in an electrical refining cell, even if it only occurs locally. With voltages that deviate from the optimum situation, less desirable (electro) chemical reactions can occur, so that some other metals can also start depositing on the cathode, which leads to a cathode with a lower purity and therefore a lower economic value. Mainly in view of the purity of the cathode, the voltage across a copper electrofining cell is usually kept within a specific range, usually 0.2-0.6 V, and certainly below a specific maximum, for example no higher than 1.6 V. voltage difference across an electrowinning cell is significantly higher than across an electro-refining cell, because the voltage difference in EW must first of all overcome the standard electrode potential of 0.34 V of the electrochemical reaction of copper, and secondly also provide the additional driving force for the electrochemical splitting of water. The voltage difference over an EW cell is therefore usually in the range of 1.8-2.5 V. Also the current density in electro-refining is usually limited to an upper limit, usually no more than about 400 A / m 2 , for the same reason of cathode purity, but also in view of other aspects of cathode quality, such as flatness, strength and hardness, and for the limiting anode passivation, as explained above. Metals that are more noble than copper and that are present in much lower concentrations in the anode and / or electrolyte, such as Pb, but also including noble metals such as Ag, Au and platinum group metals (PGMs) such as Pt and Pd, do not usually change significantly to solution. In the context of the present invention, a particular metal can be called "nobler" than the reference metal (which in this context is copper) if it has a more positive standard electrode potential (E °), i.e. the minimum voltage that is 2019/5322 BE2019 / 5322 is required to enable the electrochemical reaction “Me Me n + + ne - ”. The electrical driving force in electro-refining is generally not kept high enough to dissolve the more noble metals present in the anode via the electrochemical reaction path. However, the applicants make a distinction between, on the one hand, "electrochemical" dissolution, i.e., going into solution using the electrochemical reaction path and thus consuming electrical energy, and, on the other hand, purely "chemical" dissolving, i.e., turning into solution without consuming electrical energy. The metals that can pass into solution via this purely chemical route include Sn, As, Sb and Bi. Amounts of other metals, including the electrochemically "insoluble" metals, can still dissolve through the purely "chemical" mechanism. For example, Pb can dissolve, but in the presence of sulfate anions it forms the salt PbSO4, which has a very low solubility in the electrolyte, and therefore will tend to come out of solution and form precipitating Pb compounds. The copper around these rather "insoluble" metals dissolves, and due to the disappearance of the copper, these metals either remain as loose metal particles floating in the electrolyte and, because they usually have a higher density than the liquid, naturally go to the bottom moving the cell, or leads to the formation of a spongy film (e.g., Pb as PbSO4, a solid that is insoluble in the electrolyte) that forms on the anode surface as that surface recedes by continuously dissolving more copper . With electrowinning, no copper is dissolved at the anode. The formation of anode mucus and / or of a spongy film on the anode surface are therefore problems that are hardly known in electrowinning. They are usually problems for electrical refining, which occur almost exclusively there. In the known technique of electro refining, it is preferable to allow the anode mucus to sink through the electrolyte and to collect at the bottom of the cell as the anodes 2019/5322 dissolve ever further, and thereby withdraw, and the cathodes grow further and further. When the anodes are about to be used up, all electrodes can be pulled out of the bath, the electrolyte above the anode mucus can be pumped out, and the bottom of the cell can be cleaned by removing and recovering the anode mucus. In order to minimize the risk of anode mucus particles being encapsulated in the cathode, and thus contaminating the copper cathode, it is preferred that the anode mucus particles move to the bottom of the cell as quickly as possible under the influence of gravity. It is therefore common and preferable in the electro refining technique to allow the electrolyte to move only a little and slowly in the cell. Turbulence in the cell generally increases the risk that particles or salts of metals other than copper are trapped in the cathode and contaminate the end product. The anodes in the conventional electro refining of copper have a typical copper content of at least 98% by weight. In "The Purification of Copper Refinery Electrolyte", Journal of Metals (JOM), July 2004, pp. 30-33, consultant James E. Hoffmann shows in Table I of his article the levels of soluble elemental impurities in anode copper, in ppm, for arsenic, antimony, bismuth, iron and nickel, in various anode compositions with which he has experience. The values for individual elements can vary widely, but the total for all listed elements together amounts to a maximum of 4545 ppm, or 0.45% by weight. The article also states that the anode copper can also contain up to 0.3% oxygen. Assuming that the remainder in each composition is copper, this leads to the conclusion that the copper anode compositions described by this author in the article always contain at least 99.2455% by weight of copper, ie in accordance with the above anode purity statement for conventional copper copper refining. The article is aimed at keeping the electrolyte under control in a copper electrefining campaign. The article briefly mentions alternatives, such as solvent extraction and ion exchange, but focuses primarily on the processing of a continuous tap current, which is extracted BE2019 / 5322 2019/5322 BE2019 / 5322 7 to the circulating electrolyte. The article does not discuss the electrolyte cycle itself and how it should be performed, and does not provide details about it. Other documents attempt to conduct copper refining of copper using lower purity anodes. U.S. Pat. No. 2,286,240 discusses the recovery of metals with electro refining, starting from a typical anode containing substantially 90% copper, 3.5% tin, 5% lead, 0.5% zinc, and other metals, such as antimony, nickel and iron. As an example, anodes are discussed with at most 86.0% copper. No mention is made of oxygen in the anodes discussed in this document. The document proposes to use an electrolyte with a sulfonic acid as the main electrolytic agent, preferably in the absence of a noticeable amount of sulfuric acid or sulfates, especially when lead is present. The document does not mention anything about the removal of anode slime from the electrolytic cell. Patent DD 45843 describes a batch electro refining of copper using an anode containing 90.00 wt% Cu. The electrolyte supply of 5 liters is at a temperature of 58-59 ° C and is circulated over the cell in such a way that the bath is refreshed every 3 hours. Electro refining is continued until the increased concentrations of nickel sulfate, tin and / or antimony in the electrolyte make the liquid cloudy. The enriched electrolyte, containing 14.63 g / l Ni, is then heated to boiling temperature and treated with an oxidizing agent such that tin and antimony can be removed as a white sludge mixture (“Weissschlammenge”), and after removal copper evaporates to crystallize nickel as anhydrous nickel sulfate. The anode in DD 45843 contains a large amount of unwanted iron, up to 1.00% Fe. The method of DD 45843 has the additional disadvantage that the impurities in the anode are allowed to accumulate in the electrolyte during the batch, and thereby entail an increased risk of contamination of the cathode. DD 45843 does not provide information about the quality of the copper cathodes obtained. 2019/5322 U.S. Pat. No. 4,351,705 describes a refining process for copper-containing material contaminated with nickel, antimony and / or tin. In a first smelting furnace, a black copper is produced which contains 50-80% by weight of copper. That black copper is subjected to a series of oxidation steps until the remaining copper is of blister quality, a converter slag being formed as a by-product. The blister copper is further refined into an anode copper containing about 9899 wt.% Copper, cast into anodes, which is then treated in an electrolytic refining step 10. Selected portions of the converter slag are melted in a second smelting step 12 at a temperature of about 1200-1300 ° C under a moderately reducing atmosphere, to produce a slag residue 114 and batches of fully reduced metal product 13. The fully reduced metal products discussed as an example and cast into anodes, except those of Example 3, in which additional cobalt and nickel were added prior to casting, contained 63.9-82.10 wt% copper and at least 10 , 50 wt% nickel. In Example 4, the anodes contained 2.0 wt.% Iron, and 0.5% Fe in Example 5. For the subsequent electrolysis step, these anodes were immersed in reservoir space electrolyte extracted from a blister copper electrolytic refining section, such as step 10, or in an electrolyte with a similar copper and nickel content. Average current densities of 161 A / m 2 and 172 A / m 2 were maintained over the electrolysis cells in the examples. No mention is made of anode passivation. Mucus was formed during the electrolysis, both at the anode and at the bottom of the cell. The electrolysis was continued for up to 194 hours (Example 1, 8 days), at which time the total impurity content in the cathode had risen to 200 ppm, and the cathode purity had therefore fallen to 99.98 wt%. The composition of the electrolyte was shown to change over time, ie the copper content decreased significantly and the nickel content increased. The mucus on the anodes and at the bottom of the cell were collected, in Examples 1 and 3 even separately, presumably at the end of the electrolysis pass. The electrolysis of BE2019 / 5322 2019/5322 US 4,351,705 is performed in relatively short batch batches that must be interrupted due to the accumulation of mucus, the depletion of copper and the accumulation of nickel in the electrolyte, and an increase in the content of impurities in the cathodes produced. In the technique of electrowinning, it is standard practice to use a high circulation of electrolyte through and also within the cell, because it refreshes the bulk copper concentration in the cell, keeping the amount of stagnant films on the electrodes low, thereby reducing the availability of copper cations on the cathode surfaces is increased, and consequently the productivity of the cell is improved. Moreover, in an electrowinning cell, oxygen gas is formed on the anode surface, and the rising oxygen gas bubbles further promote fluid movement in the cell. In electrowinning it has become a common practice to introduce a gas, usually air, into the bath and to let that gas bubble pass through the electrolyte. This enhances the effect of gas bubbles that increase turbulence in the electrolyte, and furthermore dilutes the oxygen in the atmosphere above the electrolyte, thereby reducing problems that may be associated with an oxygen-rich atmosphere above the electrowinning cell. Despite the increased risk of cathode contamination, the proposal has been made in the art to also introduce gas blowing through the liquid bath into an electrical refining cell. U.S. Pat. No. 1,260,830 proposes injecting sulfur dioxide gas and directing it against the surface of the anode. We also refer to the patent specification WO 2011/085824 A1, and to several of the documents cited therein. However, neither in WO 2011/085824 A1, nor in US 4,263,120 is the increased risk of cathode contamination discussed or explained that occurs when blowing air as part of an electrical refining. In U.S. Pat. No. 3,928,152, and also in the members of the same patent family U.S. Pat. No. 3,875,041, U.S. Pat. No. 4,033,839 and U.S. Pat. BE2019 / 5322 2019/5322 141 ampere per square foot (ASF) cathode area, which amounts to 635 to 1517 A / m 2 , claiming that these current densities can be achieved thanks to the relatively small gap between the electrodes, "optimally less than one inch from plane to flat, while the insoluble anodes are provided with convection partitions 18 on their sides and protrusions 20 on the underside thereof, which are made of PVC and are therefore electrically insulating, in combination with the additional stirring effect of blowing air through. The rising air bubbles provide the energy for increased convection of the electrolyte to the cathode surfaces, thereby preventing material in particulate form from sticking to the surfaces of the cathodes. The protrusions on the underside 20 of the anode fit into lower side racks 54. Together with the convection partitions 20, these elements maintain the reduced gaps between the insoluble anodes with respect to the cathode starter cores, the edges of which are held in place by their underside to fit into the bubble tube support members 56. All detailed examples in U.S. Pat. No. 3,928,152 and the other members of the same patent family deal with electrowinning. The document states that the gas bypass system described therein has been extensively tested under electro-refining conditions where no anode passivation took place, even at current densities of up to 300 ASF, because it is claimed to be completely prevented by the high convection of electrolyte, and the cathode deposits were said not to be contaminated by anode slime in suspension. In U.S. Pat. No. 3,928,152 or in the other members of the same patent family, no information is provided about the quality of the soluble copper anodes used during these non-described electro-refinements, nor about the refresh rate of the electrolyte in the cell. Neither is mention made of measures to be taken against the depletion of copper in the electrolyte or excessive accumulation of anode slime. It must therefore be concluded that the anodes were of conventional quality, with a current content of at least 98.5% by weight of copper, which is the BE2019 / 5322 2019/5322 BE2019 / 5322 11 makes it plausible that no anode passivation was observed despite the high current densities. Many of the anode impurities that turn into solution, e.g., Ni, Fe, Co, and Mn, tend to increase the density and viscosity of the electrolyte, which has an impact on the mass and heat transfer mechanisms in the electrolytic cell, for example, moving the copper cations and the settling speed of the heavy anode mucus particles to the bottom of the bath. In particular, iron (Fe) is an element that, in solution, increases the density and viscosity of the electrolyte, thereby increasing the resistance that copper cations must overcome on their way to the cathode, as well as the resistance that anode mucus must overcome on their way to the bottom of the cell. As the anodes contain more impurities, the formation of the sponge-like film over the anode surface can become a larger factor for causing "anode passivation", ie the formation of an additional myriad / resistance that the Cu cations must overcome on their trajectory from anode surface to cathode surface. In order to maintain the desired current density through the cell, the voltage across the cell increases as the passivation of the anode gains importance. The spongy film can also fall apart into metal particles, which can collect by gravity at the bottom of the electrolytic cell if they are heavy enough, as part of what is called the anode sludge or anode mucus. Heavy anode mucus particles can form a dusty cloud that accumulates from the bottom of the cell. The particles that are to accumulate in the anode mucus should move, on their way to the bottom of the cell, along the electrodes and can be incorporated into the cathodes as impurities. They disrupt the crystal lattice of the Cu, and can cause the growth of an odd cathode surface, and the subsequent growth of dendrites, leading to short-circuiting and thereby reduced productivity. 2019/5322 It is clear that a higher content of other contaminating metals in the copper anodes can exacerbate the problems described above: the problem of passivation of the anode can occur faster and increase, so that the voltage across the cell will increase faster and the impurity content of the cathode can reach the maximum allowable level faster. However, a maximum allowable voltage can be imposed over the cell, for example due to limitations on purity of the cathode. Other possible limiting factors are the generation of heat in the cell, which can lead to thermal stress and even cracks in the cell walls, and / or the melting or failure of electrical insulation paths. As a result, there remains a need for a method whereby these problems are solved. The present invention is therefore directed to allowing higher levels of impurities in the copper anodes, ie allowing copper anodes of lower purity, leading to a relaxation of the parameters of the upstream process and the criteria for acceptable base materials, while the production of acceptable base materials copper cathodes of acceptable quality with an acceptable and economically attractive yield are retained, and cell productivity remains high. In C. Anderson et al., "The application of copper metallurgy in the recovery of secondary precious metals", Proceedings of Copper 99 - Cobre 99 International Conference, Volume III - Electrorefining and Electrowinning of Copper, The Minerals, Metals & Materials Society, 1999, pp. 529-543, three electro-refining tests are described in a 1 liter cell based on anodes containing less than 75.0% copper and more than 0.8% noble metals (Ag, Au, Pd, Pt) . The aim was to demonstrate the recovery of copper into salable copper cathodes while recovering all precious metals in the anode glue. The cell volume of 1 liter can be assumed to be the volume of the empty cell before electrodes have been introduced. During all tests, the total supply of 3 liter electrolyte was circulated at a flow rate of BE2019 / 5322 2019/5322 330 ml / minute, or 19.8 liters / hour, over the 1-liter cell and a capacity pot with heating, driven by a pump. The document does not state when and where the anode mucilage by-product from each of the tests was collected, separated, weighed and analyzed. Given the high electrolyte exchange rate of 1980% per hour (= 19.8 l / h: 1 l * 100%) across the cell, it is very unlikely that any anode mucus would have had the chance to precipitate in the cell itself. Some anode mucus may have accumulated in the contents jar during the test, but it is more likely that the anode mucus has continuously circulated throughout the complete test with the electrolyte, until the end of each test, the entire supply of electrolyte was drained and / or collected and the anode slime precipitated. The anode mucus was therefore probably not recovered until the end of an electrical refining operation cycle. Current densities of at most 173.65 A / m 2 were used in the tests. A first problem with the electro refining treatment described in this article is that the electrolyte exchange rate is high, and consequently the flow of liquid through the cell, making it very difficult to maintain the prescribed electrode distances in the cell and to avoid the risk of a short circuit because adjacent electrodes make physical contact. A second problem with the described electrical refining operation is the low electrical current density, which means a relatively low cell productivity. The document states that no anode passivation was observed during the last test of only 3 days, which was performed at the higher current density of 173.65 A / m 2 . The observation that no anod Passivation took place despite the high content of impurities present in the anodes is most likely explained by the very high refresh rate and the low current density used. The present invention has for its object to remedy or at least alleviate the problem described above, and / or to provide improvements in general. SUMMARY OF THE INVENTION BE2019 / 5322 2019/5322 BE2019 / 5322 14 According to the invention, a method is provided for the electro refining of copper and a composition for serving as a copper anode, as defined in any of the appended claims. In one embodiment, the present invention provides a process for the production of copper comprising electro refining copper metal in an electrolytic bath from at least one copper anode to at least one copper cathode, using an electrolyte based on sulfuric acid, characterized in that: the voltage difference between the anode and the cathode in the electrolytic cell is maintained at less than 1.6 volts, • the anode comprises a maximum of 98.0% by weight of copper, • the anode less than 1.00% by weight of iron • the current density throughout the cell is at least 180 A / m 2 cathode area, • electrolyte is removed from the electro-refining cell during the electro-refining treatment, with an average electrolyte exchange rate of at least 30% and at most 1900% per hour, and the electrolyte at least is at least partially removed by flooding a first flow of electrolyte over at least one cell wall, and • a gas is introduced in the cell and through the electrolyte is bubbled between the anode and the cathode. In another embodiment, the present invention provides a molten liquid metal composition that is suitable to be made suitable for copper anode electro refining in the process of the present invention and which is at least 90.10% by weight and at most 97% by weight. % copper, the surplus being formed by other elements such as impurities, the molten liquid metal composition comprising as a part thereof: • at least 0.1 wt% nickel, • at least 0.0001 wt% and less than 1.00 wt% iron, and • at least 250 ppm in wt. and at most 3000 ppm in wt. oxygen. 2019/5322 BE2019 / 5322 The impurities in the metal composition according to the present invention are mainly other metals, oxygen and optionally also sulfur and / or phosphorus. Metals in the context of the present invention are meant primarily the elements that are on the Periodic Table of Elements of IUPAC, dated June 22, 2007, to the left of the elements carbon, silicon, selenium, tellurium and polonium, including those elements themselves . The impurities most frequently encountered in the metal composition of the present invention are selected from the group consisting of nickel, antimony, tin, lead, bismuth, arsenic, zinc, iron, selenium, tellurium, silver, gold, platinum, palladium, oxygen , sulfur and phosphorus. Applicants have found that the metal composition of the present invention has the advantage that a metal composition is provided which, preferably after reducing the oxygen content of the composition to a lower level as is preferred in the context of the present invention, is suitable for casting anodes for an electrofining process according to the present invention that can be performed with a conventional electrolytic cycle, provided that a number of additional measures are taken. Applicants have found that the additional measures provided as part of the method of the present invention are sufficient to control the problems associated with the lower purity and higher impurity content of the anode material, e.g. when the anode is made from the metal composition of the present invention, preferably after reducing its oxygen content as prescribed. Applicants have found that keeping the oxygen content within the prescribed upper and lower limits is particularly important if the metal composition of the present invention is produced by a series of pyrometallurgical process steps, and the final production step yielding a liquid bath that consists of a heavy molten liquid metal phase in equilibrium with a supernatant liquid slag phase, 2019/5322 BE2019 / 5322 as described in our co-pending patent application PCT / EP2018 / 084374, filed December 11, 2018. The applicants have found that too high oxygen levels, ie above the indicated upper limit, contributes to an increase in the copper content of the molten liquid copper metal phase which is intended for casting the anodes, but also causes too many of the other valuable metals to end up in the slag phase. Nickel in particular, in the presence of an excess of copper and with the excessively high oxygen contents, tends to oxidize and end up in the slag phase. This nickel can then be lost in a final slag of the global process, where it has no value whatsoever, and possibly even causes problems for its disposal. In addition, most of the tin, antimony, and / or lead will tend to follow the nickel pathway under those conditions. The nickel and other metals may be recoverable from that slag, but must then find another way out of the general process. Because nickel in metallurgical processes has a strong tendency to exhibit behavior similar to that of copper, the desire to find a different way out for nickel than together with copper represents a heavy, perhaps even impossible, task. Applicants have found that by controlling the oxygen content as indicated, nickel in particular can leave the upstream metallurgical process as an anode impurity of the process of the present invention. Applicants have found that controlling the oxygen content in the molten liquid metal composition of the present invention within the indicated levels entails the advantage that a substantial amount of nickel can be accepted as part of the molten liquid metal composition of the present invention invention, wherein the majority of this amount of nickel can be recovered downstream of the electrolysis step of the method of the present invention, and converted to economic value. This brings with it the advantage that the upstream metallurgical 2019/5322 BE2019 / 5322 process steps are able to incorporate base materials that contain significant amounts of nickel, ie base materials that are more difficult to process due to a conventional copper production process, and which usually produce an anode material of high purity copper, such as "blister copper", that exceeds 98.0% by weight of Cu. Too high an oxygen content in the anode was found to increase the risk of deformation of the anode surfaces after casting and cooling. Without wishing to be bound by this theory, the applicants believe that a too high presence of oxygen at a late solidification stage can lead to the local formation of gas bubbles below the anode surface, and the pressure in these gas bubbles leads to deformations on the surface that deviate from an ideal flat surface. These deviations are undesirable because of the desire to work with small intervals between electrodes. Applicants therefore prefer to respect the upper limit on oxygen in the composition of the anode of the method of the present invention. Too high an oxygen content in the anode also means that more copper is present in the anode as copper (I) oxide, which dissolves in the electrolyte according to the chemical reaction path, and contributes to the copper content therein. The recovery of this copper is usually carried out by means of an additional electrowinning step on the electrolyte tap current, which is complex and means a substantial additional charge. High levels of oxygen in the anode also encourage anodic passivation, particularly at high current densities, as described by CAMöller et al. In "Effect of As, Sb, Bi and Oxygen in Copper Anodes During Electrorefining", Proceedings or Copper 2010, pp. 1495-1510. Applicants have therefore found that it is advantageous for a number of reasons to keep the oxygen content in the molten liquid metal composition of the present invention within the indicated levels, especially in combination with the content of non-copper impurities in the composition, especially when nickel is present. A good reason, for example, is that less 2019/5322 oxygen in the molten liquid metal composition leads to fewer gas bubbles in the anodes being poured with it. As a result, the anode surfaces are smoother and the anodes flatter, which are both factors that improve the alignment of the anodes in the cell and ensure a more uniform distance between the electrodes in the cell during the electro refining treatment. Applicants have found that it is possible without problems to further reduce the oxygen content by known means, such as "poling", to the preferred levels in the process of the present invention, thereby converting metal oxides to elemental metal, in particular the copper oxide to copper metal, the latter problem-free electrochemically dissolving in the electrolyte and passing to the cathode in the method according to the present invention. Applicants have found that the molten liquid metal composition of the present invention is the preferred route for nickel in the upstream pyrometallurgical process steps that produce the molten liquid metal composition of the present invention. The nickel is easy to accept in the method of the present invention because it concentrates in the electrolyte and a drain current can be withdrawn from the electrolyte cycle, and the nickel contained therein can be selectively recovered and upgraded to elemental nickel. In "The Purification of Copper Refinery Electrolyte", JOM, July 2004, pp. 30-33, James E. Hoffmann describes a number of practices to control the composition of electrolyte in a copper electro-refining campaign, primarily by treating such a tap current that is withdrawn from the electrolyte cycle. The impurities discussed include Sb, Bi, As, Ni, Ca, ammonia, and organic fragments created by the hydrolysis of conventional cathode growth modifying additives. As already stated above, the content of impurities in the soluble copper anodes in this article is low, and the copper purity of the anodes in the article is far above the levels indicated as part of the present invention. BE2019 / 5322 2019/5322 Applicants have found that the behavior of nickel in the electrolysis cycle is quite unique among the metal impurities that may be present in significant concentrations in the molten liquid metal composition of the present invention, and also the composition of the anode in the process of the present invention. Applicants have found that nickel is able to dissolve in the electrolyte based on sulfuric acid as nickel sulfate, and to accumulate at interestingly high concentrations before this salt could lead to operational problems and / or cathode quality problems. Applicants have also found that the nickel in the electrolyte can be recuperated quite easily from the electrolyte, preferably from a drain current withdrawn from the electrolyte cycle, and that this nickel can be easily upgraded to commercial value. Applicants have found that the nickel can be recovered and upgraded while at the same time the majority of the copper dissolved in the withdrawn electrolyte can be recovered and upgraded, and the acid can be recycled to electro refining. Applicants have found that this method of recovering and upgrading nickel is a method that is preferred to provide a way out for nickel entering an upstream pyrometallurgical method for producing the molten liquid metal composition of the present invention and / or the anode for the method of the present invention. Allowing significant levels of nickel in the molten liquid metal composition of the present invention and / or in the anode for the process of the present invention broadens the acceptance criteria for the base materials in the upstream copper refining process by which the metal composition is produced. This entails the advantage that the performer of the upstream process is able to accept larger quantities of raw materials with a high nickel content, which therefore BE2019 / 5322 2019/5322 BE2019 / 5322 may be less acceptable, or only acceptable in limited amounts, for practitioners of other methods that are not related to the method of the present invention. Such raw materials may therefore be available at more attractive conditions and in more advantageous quantities than raw materials containing less nickel. Applicants have found that the higher levels of nickel in the electrolyte that result from a higher nickel content in the molten liquid metal composition of the present invention and / or in the anode for the process of the present invention, and therefore also in the electrolyte extracted from the electrolyte cycle for the recovery of nickel leads to an improvement in the effectiveness and efficiency of the steps of recovery and upgrading of nickel, because more nickel can be recovered and upgraded in smaller equipment and with a lower consumption of energy and / or process chemicals. The applicants have also found that there is a significant advantage in limiting the iron content of the anodes as indicated. Applicants have found that dissolved iron in the electrolyte leads to significant energy inefficiencies, in the sense that they cause some of the electrical current through the cell not to contribute to the transfer of copper cations from anode to cathode. Without wishing to be bound by this theory, the applicants believe that iron cations in the electrolyte are able to readily change valence, presumably due to the half reaction Fe 2+ -> Fe 3+ + e - taking place on the anode, and after the Fe 3+ cation has passed to the cathode, the reverse half reaction Fe 3+ + e - -> Fe 2+ on the cathode, after which the Fe 2+ cation is able to return to the anode. This mechanism could explain the observation that, with significant amounts of iron in the electrolyte, part of the electrical current can pass through the cell without contributing to the transfer of copper cations. That part of the electric current therefore represents a non-productive use of an expensive source. 2019/5322 Applicants have also found that, due to the presence of iron in the anodes, and therefore also in the electrolyte, an additional amount of non-contributing electric current is required to maintain an equally high copper cathode productivity, which poses the problems that tackles and solves the present invention. The increased current causes the voltage across the cell to increase, and also to increase faster, leading to higher levels of impurities in the cathode and leading to the maximum allowable level being reached faster, as explained earlier in this document. The higher current also generates more heat in the cell, and may lead to the formation of hot spots, causing other problems described elsewhere in this document. It also boosts the current density for the same copper productivity, which increases its contribution to cathode contamination, as explained below. When iron dissolves into the electrolyte from the anode, it increases the density and viscosity of the electrolyte, which influences the mass and heat transfer mechanisms in the electrolytic cell, for example, the displacement of the copper cations on their way to the cathode and the settling speed of the heavy anode mucus particles to the bottom of the bath. A high content of Fe in the anode, and therefore also in the electrolyte, increases the resistance that copper cations must overcome on their way to the cathode, and the resistance that anode glue must overcome on their way to the bottom of the cell. For this reason, the anodes in the method of the present invention, as well as the molten liquid metal composition of the present invention, must contain iron at a level lower than the prescribed upper limit. The molten liquid metal composition of the present invention, and preferably also the copper anode in the process of the present invention, optionally contains at least 0.0001% by weight of iron, preferably at least 0.0005% by weight, with more preferably at least 0.0010% by weight, even more preferably at least BE2019 / 5322 2019/5322 0.0025% by weight, preferably at least 0.0050% by weight, more preferably at least 0.0075% by weight, even more preferably at least 0.010% by weight, preferably at least 0.015 wt%, more preferably at least 0.020 wt%, even more preferably at least 0.025 wt% iron. Applicants have found that it is not necessary to remove iron from the anode composition and / or the molten liquid metal composition of the present invention to levels below the detection limit of 1 ppm by weight, but that it is advantageous to use small amounts to preserve iron. It alleviates the limitations, strictness and operational burden of the upstream process steps where the metal is produced that forms the basis for the anodes of the method of the present invention. Therefore, it should be noted that the lower iron content limit prescribed for the molten liquid metal composition of the present invention, and prescribed for the copper anode composition used in the method of the present invention, is not an essential part of the invention that would be required to achieve the desired result. It is not technically related to the technical effects on which the present invention is based. Respecting the lower limit is preferred because of the advantages associated therewith that occur upstream of the electro-refining step. Applicants state that in pyrometallurgical processes that produce liquid molten copper products suitable for being cast into electro-refining anodes, iron metal is generally used as a reducing agent and / or as an energy source. The presence of a measurable amount of iron in the molten liquid metal composition of the present invention and / or in the anode composition of the process, as indicated, is therefore a useful indication that the composition and / or anode is made by by a pyrometallurgical process and is not the result of synthetically, usually on a laboratory scale, combining pure copper with other metals in high purity to obtain an anode with a BE2019 / 5322 2019/5322 particularly desirable composition for experimental purposes and strictly controlled tests. The applicants have found that the electro refining of copper anodes with a lower copper content, and thus contain high levels of impurities, usually other metals, and that with the high current densities as indicated, the level of impurities in the anode increases because the anode impurities and the high current densities together aggravate the problem of anode passivation. Applicants have found that this problem can be solved by the components of the present invention, in particular in combination with each other. Applicants have found that the addition of gas and the bubbling of this gas through the electrolyte between the anode and the cathode, and in this electrofining campaign, preferably on the anode side of the gap, leads to better stirring of the electrolyte. If the gas addition is performed correctly, as described below in this document, it produces this effect locally, between the electrodes where its impact is greatest, while it hardly has any influence on the fluid flows elsewhere in the cell, e.g. at the bottom of the cell, where a significant part of the anode mucus collects. This improved stirring of the liquid primarily improves the physical transport of the Cu 2+ cations from the anode to the cathode by convection. This is caused by increased turbulence in the liquid between the electrodes, whereby the transport is accelerated by convection, but also by reducing the diffusion boundary layer at the anode and / or cathode surface, which is stagnant and through which the transport takes place through diffusion. An additional advantage is a more homogeneous spread of the temperature and of the concentration of process chemicals throughout the cell, which also leads to a better homogeneity of the current distribution. These effects entail the advantage that they allow high cell productivity while maintaining a lower cell voltage difference, and that a cathode of BE2019 / 5322 2019/5322 higher purity is obtained compared to the situation without stirring or with less stirring of the bath. The lower cell voltage difference brings with it the advantage of lower energy consumption for the same product yield. Without wishing to be bound by this theory, the applicants believe that this is due to a physical reduction and a mechanical degradation of the spongy film that is constantly built up on the anode surface, and to an improved homogenization of the electrolyte concentration in terms of the levels to copper and / or the metal impurities, of the temperature, and of the additives. This reduces the risk of local hotspots in the bath with regard to each of these parameters. Such hotspots in terms of temperature and / or concentrations of copper, metal impurities and additives can be harmful. Metal impurities can accumulate locally and increase the voltage across the cell or even locally between a specific pair of electrodes or between different points on the same electrode, and thereby may decrease cell productivity and cathode quality. A shortage of copper at the cathode end can lower the deposition rate. Local hotspots of a soluble metal such as nickel can lead to local deposits of salts of that metal. Local temperature results can cause damage to cell walls and / or to the insulation paths that provide electrical insulation between different cell parts or elements. Local temperature results may also accelerate the deterioration of some of the process chemicals or additives, and may even lead to premature stripping of the cathode, i.e., prematurely loosening, already during electrofining, of the cathode copper layer of its substrate. This premature stripping can easily lead to a short circuit and loss of production. The applicants state that the prescribed upper limit on the presence of iron in the anode contributes to the advantages discussed here, such as the lower voltage, the lower energy consumption and the less occurrence of hotspots. By limiting iron in the electrolyte BE2019 / 5322 2019/5322, the current efficiency is increased and the transfer of mass and heat through the electrolyte is improved. Applicants have found that the characteristic that indicates that the rate at which electrolyte is removed from the electrolytic cell must meet the indicated lower limit further contributes to an increase in the stirring of the bath. As a result, the advantages discussed above are further enhanced in combination with the introduction and bubbling of a gas through the electrolytic bath. The applicants have found that the high electrolyte rates in the bath, caused by the high speed at which electrolyte is removed from the bath, and / or by the extra turbulence due to the gas bubbling through the bath, produce surprisingly strong effects, because it prevents the accumulation, and therefore limits the thickness, of any spongy films, and / or the risk of a slime particle being deposited on the surface of the anode and / or cathode. Applicants have observed that the spongy film is quite brittle, and believe that gas bubbling can also have a mechanical impact on the spongy film. Applicants believe that the high liquid velocities in the electrolyte also greatly contribute to the degradation of the sponge-like film on the anode, and to moving the particles of anode mucus in suspension away from the electrodes. The high rate at which the electrolyte is removed from the bath also limits the accumulation of solid particles in the electrolyte present in the space between anode and cathode. The high removal rate makes it possible to remove at least a portion of the formed anode mucus particles from the removed electrolyte before the cleaned electrolyte is recycled to the electro refining cell as part of the present invention. The aspects of the present invention have been found to greatly limit the effect of "anode passivation," as set forth elsewhere in this document. The electrolyte removed from the electro-refining cell contains anode slime particles in suspension. While heavy anode mucus particles can still easily fall through the electrolyte, BE2019 / 5322 2019/5322 against the displacement of the gas bubbles by the electrolyte, lighter anode mucus particles may not settle as easily, and may be more inclined to move upward toward the surface where they are entrained and removed from the cell by the electrolyte overflow. The high speed at which the electrolyte is removed therefore also means a high removal speed of at least a part of the lighter anode mucus. This entails the advantage of a high removal rate of anode mucus from the cell. This entails the advantage that the total amount of anode mucus that can accumulate over time in the cell remains limited. Frequent or continuous removal of anodic adhesives, for example because they are entrained with the removed electrolyte, reduces the chance of metal impurities being incorporated into the cathodes. Another advantage of more frequent access to the anode slime than only at the end of an electro-refining campaign, and therefore only after the anodes have been exhausted, is the availability of anode slime spread over a longer period of time. This entails the advantage that any further processing of the anode adhesives can be spread more evenly over time, which entails the advantages of a smaller size of equipment and lower investment costs, in combination with easier use and planning thereof, insofar as even that the processing of anode mucus can be performed in continuous mode. An additional advantage is that, due to the considerable value that these anode adhesives can represent, which is largely due to the presence of PMs, including PGMs, the improved access to the anode adhesives leads to a reduction in the amount of working capital which on average - can be trapped in the continuous inventory of anode glue in the operational installation. However, applicants have found that an excessively high electrolyte current through the electro-refining cell can lead to other problems. Usually the anodes and cathodes hang loosely and strictly vertically under their own weight, side by side and in alternating order in the cell, at the distance intended in the design to their closest neighbors. The physical BE2019 / 5322 2019/5322 distance between anode and cathode surfaces determines the distance that cations must bridge through the electrolyte. The resistance encountered by this physical flow of cations through the electrolyte is an important element in the global electrical resistance across the cell, and therefore makes a significant contribution to the voltage difference required to overcome and provide for the global electrical resistance for the desired current density and therefore the desired cell productivity. Physical movement or movement of electrodes in the cell can cause the distance between the electrodes to be no longer uniform, leading to an uneven spread of current density, a locally increased cathode growth rate and locally unsuitable levels of additives, resulting in a lower cathode quality . Moreover, the adjacent electrodes should not come into physical contact with each other, because that means an electrical short circuit. A short circuit between an anode and a cathode in electrical refining eliminates the electrical potential difference between the two, which is the driving force for the electrolysis, and therefore stops the electrochemical solution at the anode and the deposition of copper at the cathode, while a large amount electrical energy is converted into local dissipation of heat, which can even lead to strong connection between the two electrodes. By moving fluid in the cell, an electrode can be pushed closer to its neighbor, which can create the problems described above, including a higher risk of physical contact. This problem is made even more complicated in that the growth of metal on a cathode can take place unevenly. Dendrites can be formed which can protrude perpendicular to the cathode surface. Inequalities can also form on the anode surface, such as the spongy film described elsewhere in this document. The distance between the electrodes for which a particular electrolytic cell has been designed is therefore usually an acceptable compromise between, on the one hand, the desire to reduce the required potential difference across the cell, and, on the other hand, the desire to limit the risk of physical contact between adjacent electrodes , with a short circuit as a result, BE2019 / 5322 2019/5322 BE2019 / 5322 for the duration of a complete electrolytic cycle. The electrodes that are more subject to movement due to the displacement of electrolyte in electro refining are in particular the cathodes at the start of an electrolytic cycle and / or the cathodes that are closest to the inlet for electrolyte, because they then have the lowest weight and / or may experience a higher liquid flow pressure. Similarly, the anodes at the end of the cycle, which are called the spent anodes, also represent a significant risk due to their reduced weight. In the art, also in some of the documents discussed above, the proposal has been made to limit the movement of electrodes in an electrolytic cell by physical means, such as by means of conductors against the cell wall or bottom into which the electrodes fit when they are lowered in the electrolytic cell. A problem, however, is that the growth of metal on the cathode can cause the cathode to become stuck to the conductor or rack, such that it becomes difficult or even impossible to release the cathode at the end of the electrolytic cycle of the conductors and / or racks in the cell. The problem becomes even more difficult with electro refining when the starting anodes are less pure, ie when more anode mucus is formed and more spongy film can form on the anode surface, and also because there are more particulate contaminants present that could be encapsulated in the cathode. The cathode surface can grow unevenly, and the cathode growth can become stronger on the protrusions created due to the smaller distance from the anode, thereby creating "dendrites" that will grow from the rest of the cathode surface as they grow. In particular, when the anodes are relatively rich in tin and antimony, Sn / Sb intermetal compounds and / or oxides can be formed which tend to grow strongly on the cell walls and side strips of the starter cores and detach the finished cathode to complicate any connections or clamps that are provided on the cell wall or floor. Another problem associated with providing conductors or terminals for, among other things, the movement of electrodes 2019/5322 relative to the cell wall or bottom is that they are a hindrance to the removal of heavy anode mucus from the cell, especially if it is preferred to carry out that removal during the electrolytic cycle. Such electrode conductors can form obstacles for the displacement of, for example, a suction head for the extraction of sludge from the bottom of the cell. Every physical element at the bottom of the cell prevents the extraction of sludge from the cell unless it is first removed. And vertical electrode conductors along the cell walls pose potential obstacles to any horizontal wall mounts to guide the suction head for sludge extraction. The possibilities to provide electrode conductors are therefore limited in combination with a provision for the removal of heavy anode adhesives during the electrolytic cycle. Applicants have found that, due to the high impurity content of the anodes, the electro refining method of the present invention limits the options for providing conductors to limit the movement of electrodes in the cell. The purpose of the upper limit indicated for the rate at which electrolyte is removed from the cell in the method of the present invention is, therefore, to limit the movements of electrodes during operation, and thus to avoid the risk of short circuiting, and at the same time extensive physical electrode conductors must be provided, such as along cell walls or at the bottom of the cell, so that the extraction of sludge is not impeded. Limiting the electrolyte exchange rate in the cell also leads to a saving on investment and operating costs for the equipment and energy required for circulating electrolyte. Applicants have thus found that electro refining can be successfully carried out to produce high quality cathodes based on lower purity anodes, provided that gas is introduced and bubbled through the electrolyte, and that the flow of electrolyte through the electrolytic cell is sufficiently high to control the concentration of the lighter anode mucus in the cell, yet remains sufficiently low for the movement BE2019 / 5322 2019/5322 BE2019 / 5322 30 of electrodes caused by the pressure of the liquid flow remains low, and it is not necessary to provide physical conductors to limit the movement of electrodes, such that the extraction of heavy anode mucus from the cell is not impeded. . The present invention thus reduces the negative effects on cathode quality that can be caused by an increased content of impurities in the copper anodes. Accordingly, the present invention permits the processing of less pure copper anodes, i.e., anodes with a significantly higher impurity content. Applicants have found that the method according to the present invention considerably relaxes the purity requirements for the copper current to be suitable to be cast into anodes which can be further refined via electro-refining into high-purity copper quality cathodes. The method of the present invention allows much higher concentrations of metal impurities in the anodes compared to the prior art. That is, the upstream method by which the anodes are produced can be performed less strictly, e.g. with less stringent quality standards, which can yield an advantage of higher productivity. Applicants have found that the method of the present invention makes it possible to obtain this advantage without significant compromises regarding the recovery of copper in the copper cathode. The applicants have furthermore found that the method according to the present invention makes it possible to obtain this advantage while the amount of other metals which end up in the copper cathode is limited to commercially acceptable levels. The applicants have furthermore found that the method according to the present invention possibly creates the possibility of extracting as many of the contaminating metals as possible. 2019/5322 recover in the anode metal, including Bi, Sn, Pb, As and Sb, but also precious metals such as Ag, Au, Pd, Pt, as part of the anode mucilage. The applicants have furthermore found that the method according to the present invention possibly creates the possibility of recovering as much nickel as possible that may be present in the anode metal from the electrolyte. The advantages of the improved anode metal quality requirements are that (a) the upstream pyrometallurgical steps for the recovery of copper can accept basic materials with a much lower purity, and / or that the operational window for the production of a refined copper suitable for the electro refining step is broadened, and (b) the composition restrictions imposed on the raw materials considered acceptable for this upstream copper recovery by pyrometallurgical steps are relaxed. The present invention thereby also brings with it the advantages of (a) broadening the acceptable quality requirements for the base materials of the upstream pyrometallurgical process steps, such that base materials can be processed that are more heavily contaminated with the listed metals, and therefore more readily available meet more economically advantageous conditions, and (b) reducing operating problems and costs in the upstream pyrometallurgical steps to produce a refined copper stream that is suitable for the electro refining of copper from less Cu-rich raw materials. The present invention appears to provide these advantages while still offering the advantages of an electro refining capable of operating with long anode renewal cycles, with high productivity, high current density and low energy consumption. Applicants have found that the method according to the present invention can be carried out in such a way that it only needs to be BE2019 / 5322 2019/5322 BE2019 / 5322 32 interrupted for replacing the anodes, but, as will be explained later in this document, that the electrolyte concentration can be well controlled, as well as the accumulation of anode mucus in the cell and in the electrolyte, and that even cathodes can be replaced while the electrolysis is being operated. The invention achieves this object by reducing the effect of anode passivation and of the accumulation of impurities in the electrolyte. Other advantages, such as the possible selective recovery of Ni from Cu, and of other metals via the anode slime, are also realized. BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 shows a flow chart of the core portion of an embodiment of the method according to the present invention. DETAILED DESCRIPTION The present invention will be described below in specific embodiments and with possible reference to specific drawings; however, it is not limited to that, but is only determined by the conclusions. The described drawings are only schematic and are non-limiting. In the drawings, the size of some elements for illustrative purposes may be magnified and not drawn to scale. The dimensions and relative dimensions do not necessarily correspond to actual practical embodiments of the invention. Furthermore, the terms first, second, third, and the like, in the description and claims, are used to distinguish between similar elements, and not necessarily to describe a sequential or chronological order. The terms are interchangeable under appropriate conditions, and the embodiments of the invention may function in sequences other than described or illustrated herein. Furthermore, the terms upper, lower, top, bottom, and the like are used in the description and claims 2019/5322 BE2019 / 5322 descriptive purposes, and not necessarily to describe relative positions. The terms thus used are interchangeable under appropriate circumstances, and the embodiments of the invention described herein may function in orientations other than described or illustrated herein. The term "comprising", used in the claims, should not be interpreted as being limited to the means listed in its context. It does not exclude other elements or steps. The term is to be interpreted as the required presence of the stated properties, numbers, steps or components, but does not exclude the presence or addition of one or more other properties, numbers, steps or components, or groups thereof. The scope of the expression "an item comprising means A and B" should therefore not be limited to an object composed solely of components A and B. It means that for the subject matter of the present invention, A and B are the only relevant components. Accordingly, the terms "include" or "enclose" also include the more restrictive terms "consist essentially of" and "consist of". Therefore, when "include" or "contents" is replaced with "consist of," these terms represent the basis of preferred but narrowed embodiments, which are also provided as part of the contents of this document relating to the present invention. Unless otherwise specified, all values specified in this document include the range up to and including the end points indicated, and the values of the components or components of the compositions are expressed in percent by weight, or percent by weight, of each ingredient in the composition. In addition, each compound used in this document can be interchangeably discussed based on its chemical formula, chemical name, abbreviation, etc. The present invention is directed to the electro refining of copper, i.e. the purification of a copper stream containing impurities, in particular other metals, from which anodes 2019/5322 BE2019 / 5322 are made into copper cathodes with a higher copper purity. This differs significantly from copper electrowinning. In the hydrometallurgical recovery of copper from ore or other basic materials, metals from the solid starting material are leached into a liquid lye solution, the metals being dissolved by means of strong acid solutions (such as sulfuric acid, hydrochloric acid). In the downstream copper electrowinning step, copper can be recovered from the liquid lye solution, or from a concentrate derived therefrom, by selectively driving the copper cations out of solution and depositing the copper on a cathode, under the driving force of an electric voltage difference between the cathode and a chemically inert anode, which is usually made of lead, water on its surface being electrochemically split into oxygen gas (O2 escaping from the cell) and protons (H +) that remain in solution. One electron is released for each proton formed. These electrons travel through the electrical circuit from the anode to the cathode, and are picked up at the cathode for depositing copper metal (mainly through the Cu 2+ + 2 e-Cu reaction), which is similar to what happens at the cathode during electrical refining. Because electrowinning must also split water into oxygen and protons, the theoretical minimum set out in this document is the copper electrocining cell required. copper electrowinning cell is significant It therefore in the voltage difference higher than voltage difference practice at least over for over 1.6 V, and one in practice, differences in the range of 1.6-2.5 volts are used to also overcome the additional resistances in the electrowinning electrolyte. In the context of the present invention, the electrolyte refresh rate of an electrolytic cell means the rate at which electrolyte is removed in percent, relative to the liquid volume of the empty electrolytic cell per unit time, usually per hour. By an empty electrolytic cell is meant the amount of liquid that the cell can contain when it is still empty, i.e. the cell before the electrodes or other elements or submerged auxiliary elements 2019/5322, such as conductors for electrodes and / or suction nozzles, and / or manifolds and / or manifolds for incoming and / or outgoing fluids, gas and / or liquid. The refresh rate, as defined in the context of the present invention, is the refresh rate of the electrolytic cell, or of one or more cells belonging to the same electro refining unit, and therefore completely independent of the volume of a tap current that is usually continuously withdrawn. to the circulating electrolyte, which some might also call a "refresh rate," but in proportion to the electrolyte cycle as a whole, and without any relation to the refresh rate as defined in the context of the present invention. The refresh rate regulations in the context of the present invention relate to the average refresh rate in the course of a complete electrolytic cycle, i.e., the operating period between two consecutive anode replacements. Later in this document, we will explain that more than one single current of electrolyte can be removed from the cell, and that such a removal current may not necessarily be continuous, but may also be discontinuous. As a result, it is possible that, during certain periods of operation, the rate at which electrolyte is removed from the cell can be increased considerably periodically. The requirement for the average refresh rate in the context of this invention is therefore the average over the entire electrolytic cycle, including any periods in which the electrolyte removal rate is higher. The time span for the average refresh rate relates only to operating time, i.e. the time in which the cell is at least partially in operating mode, with the electrical current passing through the cell. In an embodiment of the present invention, the voltage difference between the cathode and the anode in the electrolytic cell is at most 1.5 V, preferably at most 1.4 V, more preferably at most 1.3 V, even more preferably at most 1.2 V, preferably at most 1.1 V, more preferably at most 1.0 V, with BE2019 / 5322 2019/5322 more preferably at most 0.9 V, preferably at most 0.88 V, more preferably at most 0.85 V, even more preferably at most 0.83 V, preferably at most 0.80 V , more preferably at most 0.7 V, even more preferably at most 0.6 volts. Preferably, the prescribed voltage upper limit is observed for a complete electrolytic cycle, including the end of the cycle, when the anodes are nearly exhausted and ready to be replaced, and when the voltage across the cell is usually highest. Applicants prefer to keep the voltage in the cell below the prescribed upper limit because it reduces cathode contamination and improves cathode quality while reducing the risk of excessive accumulation of resistance in the cell, which can lead to temperature increases that can cause thermal stresses, degradation of additives and other undesirable effects. In an embodiment of the present invention, the anode comprises at most 97.5% by weight of copper, preferably at most 97.0% by weight, more preferably at most 96.5% by weight, even more preferably at most 96.0% by weight, preferably at most 95.5% by weight, more preferably at most 95.0% by weight, even more preferably at most 94.5% by weight, at preferably at most 94.0% by weight, more preferably at most 93.5% by weight, even more preferably at most 93.0% by weight, preferably at most 92.5% by weight, more preferably at most 92.0% by weight, even more preferably at most 91.5% by weight of copper. Applicants have found that several of the advantages of the present invention become even stronger when the anodes are less pure, i.e. leave more room for metals other than copper. This broadens, for example, the quality requirements for accepting the basic materials of the upstream pyrometallurgical process steps, as well as the operational window for the upstream pyrometallurgical steps with which the anode metal is produced. In an embodiment of the present invention, the anode and / or molten liquid metal composition of the present invention comprises at most 0.90% by weight of iron, preferably BE2019 / 5322 2019/5322 at most 0.80% by weight, more preferably at most 0.70% by weight, even more preferably at most 0.60% by weight, preferably at most 0.50% by weight %, more preferably at most 0.40% by weight, even more preferably at most 0.30% by weight, preferably at most 0.25% by weight, more preferably at most 0.20% by weight %, even more preferably at most 0.15% by weight, preferably at most 0.10% by weight, even more preferably at most 0.050% by weight of iron. This entails the advantage that the electrolyte will also contain less iron, and that the problems associated with the presence of iron cations in the electrolyte are easier to contain, to the extent that they are acceptable or even practically absent. . In an embodiment of the present invention, the current density throughout the cell is at least 190 A / m 2 , preferably at least 200 A / m 2 , more preferably at least 210 A / m 2 , even more preferably at least 220 A / m 2 , preferably at least 230 A / m 2 , more preferably at least 240 A / m 2 , even more preferably at least 250 A / m 2 , preferably at least 260 A / m 2 , more preferably at least 270 A / m 2 , even more preferably at least 280 A / m 2 . A higher current density throughout the cell usually entails the advantage that the productivity of the cell is increased, in particular if the contribution of the current to the transfer of copper cations is kept high, and the part of the current used by mechanisms that do not contribute to the transfer of copper cations from anode to cathode is kept low, e.g. by keeping the amount of iron cations in the electrolyte low, such as by using anodes containing iron at a level below the prescribed limit. In one embodiment of the present invention, the current density throughout the cell is at most 400 A / m 2 , preferably at most 390 A / m 2 , more preferably at most 380 A / m 2 , even more preferably at most 370 A / m 2 , preferably at most 360 A / m 2 , more preferably at most 350 A / m 2 , even more preferably at most 340 A / m 2 , preferably at most 330 A / m 2 , more preferably at most 320 A / m 2 , even more preferably at most 310 A / m 2 , preferably BE2019 / 5322 2019/5322 BE2019 / 5322 at most 300 A / m 2 , more preferably at most 290 A / m 2 , even more preferably at most 280 A / m 2 . Applicants have found that observing the prescribed upper limit for the current density across the cell entails the advantage that the problems raised by a higher current density are kept manageable, and that the advantageous effects of the present invention are easier to achieve to be achieved. These problems are described elsewhere in this document, and anode passivation is a good example of such a problem. In an embodiment of the present invention, the electrolyte is removed from the cell with an average refresh rate of more than 30%, preferably at least 35%, more preferably at least 40%, even more preferably at least 45%, preferably at least 50%, more preferably at least 55%, even more preferably at least 60% per hour, preferably at least 70%, more preferably at least 75%, even more preferably at least 80%, preferably at least 85%, more preferably at least 90%, even more preferably at least 95%, preferably at least 100%, more preferably at least 105%, even more preferably at least 110% per hour. The refresh rate and its average are as defined above. The indicated refresh rate only applies to the volume of the first flow of electrolyte leaving the cell due to flooding. Any other current of electrolyte leaving the cell, such as the second current of electrolyte containing anode glue introduced later in this document, is additional to the refresh rate of the first current. Applicants have found that a higher rate of electrolyte refresh rate greatly contributes to controlling the amount of anode mucus in the cell. That is an important factor to keep the cathode quality high, despite high levels of impurities in the anodes. It also brings other benefits, such as faster access to the valuable anode glue for further upgrading. A higher refresh rate also contributes to a stronger stirring in the liquid bath in the electrolytic cell. The higher fluid flows can already be achieved 2019/5322 BE2019 / 5322 cause a certain amount of liquid turbulence, at least locally, on top of the contribution of gas addition and bubbling, and thereby help to reduce the thickness of the still liquid films that inevitably form on the surfaces of anode and / or or cathode, and promote the displacement of copper cations from anode to cathode. Thanks to the indicated upper limit of iron for the composition of the anode, the higher refresh rate does not lead to a significant increase in any loads caused by iron cations in the electrolyte. In one embodiment of the present invention, the electrolyte is removed from the cell at an average refresh rate of at most 1700% per hour, preferably at most 1500%, more preferably at most 1200%, even more preferably at most 1000%, preferably at most 800%, more preferably at most 600%, even more preferably at most 400%, preferably at most 300%, more preferably at most 290%, even more preferably at most 250%, preferably at most 200%, more preferably at most 175%, even more preferably at most 150%, preferably at most 125% per hour. Applicants have found that compliance with the prescribed upper limit for the electrolyte refresh rate entails the advantage that the liquid pressure on the electrodes can remain limited. This entails the advantage that it may not be necessary to provide conductors for all electrodes in the bath to limit the movement of electrodes in the cell and to keep the distance between adjacent electrodes within narrow limits with respect to the desired (and usually provided for in the design) values. Limiting the electrolyte exchange rate below the indicated upper limit entails the advantage that heavy anode mucuses are more likely to precipitate at the bottom of the cell, where they can be removed during operation, as explained later in the document. In an embodiment of the present invention, the amount of gas introduced into the cell and bubbled through the electrolyte between the anode and the cathode is at least 2019/5322 BE2019 / 5322 an effective amount, i.e. an amount effective to lead to better stirring of the electrolyte. An effective amount of gas leads to a noticeable reduction of the cell voltage at the desired current density compared to the voltage that is set without adding gas. The gas should be supplied at a pressure that is at least sufficiently high to overcome the hydrostatic pressure represented by the liquid column in the cell above the level where the gas is introduced, and preferably higher. Applicants prefer to use a pressure that is at least 0.1 bar above this minimum required pressure, preferably at least 0.3 bar, more preferably at least 0.5 bar above the hydrostatic pressure, together with a plurality of flow restrictions, such as small holes or pipes through which the gas is sprayed into the cell, such that a pressure drop occurs over flow restrictions and the gas flow is better distributed over the plurality of flow restrictions, and consequently the resulting gas bubbles are also more evenly distributed over the cell. In an embodiment of the present invention, the metal composition comprises at least 90.5% by weight of copper, preferably at least 91.0% by weight, more preferably at least 91.5% by weight, preferably at least 92.0 wt%, more preferably at least 92.5 wt%, even more preferably at least 93.0 wt% copper. Preferably, the molten liquid metal composition of the present invention also meets, where possible, the prescribed concentration limits for the composition of the anode as part of the process of the present invention, preferably also the concentration limits that are preferred for the composition of the anode. the anode, but excluding the oxygen content. The advantages associated with these prescribed concentration properties for the molten liquid metal composition in accordance with the present invention are the same as those described in the context of the composition of the anode as part of the method of the present invention. 2019/5322 BE2019 / 5322 In one embodiment, the molten liquid metal composition of the present invention comprises at least 0.25 wt% nickel, preferably at least 0.50 wt%, more preferably at least 0.75 wt%, with more preferably at least 1.00 wt%, preferably at least 1.25 wt%, more preferably at least 1.50 wt%, even more preferably at least 2.00 wt% , preferably at least 2.10 wt%, more preferably at least 2.25 wt%, even more preferably at least 2.50 wt% nickel. A higher nickel content in the metal composition allows the upstream process to accept more base materials that contain substantial amounts of nickel. Such base materials are difficult to process for most electrical refining processes, and are therefore easier to obtain at more economically favorable conditions. Optionally, the metal composition comprises at most 10.0% by weight of nickel, preferably at most 9.0% by weight, more preferably at most 8.0% by weight, even more preferably at most 7.00% by weight %, preferably at most 6.00% by weight, more preferably at most 5.50% by weight, preferably at most 5.00% by weight, more preferably at most 4.50% by weight %, preferably at most 4.00% by weight, more preferably at most 3.50% by weight nickel. At lower levels of nickel in the composition of the anode, the tapping current can be kept smaller, which simplifies its further processing and reduces the associated operating costs. Lower levels of nickel also reduce the need to add additional copper cations to the electrolyte. Less nickel also reduces passivation of the anode, which makes it possible to apply the measures taken to prevent anode passivation less strictly and / or less intensively. Applicants have found that it is important to make the oxygen content of the molten liquid metal composition in accordance with the present invention meet the indicated upper limit, preferably less than 3000 ppm in weight, more preferably at most 2800 ppm in weight. even more preferably at most 2600 ppm by weight, preferably at most 2019/5322 2500 ppm in weight, more preferably at most 2400 ppm in weight, even more preferably at most 2300 ppm in weight, more preferably at most 2200 ppm in weight, even more preferably at most 2100 ppm in weight , preferably at most 2000 ppm in weight, more preferably at most 1800 ppm in weight, even more preferably at most 1600 ppm in weight, and even more preferably at most 1400 ppm in weight On the other hand applicants claim that it is also important to have the oxygen content meet the stated lower limit, preferably at least 300 ppm in weight, more preferably at least 400 ppm in weight, even more preferably at least 500 ppm in weight and, even more preferably, at least 600 ppm in weight, preferably at least 700 ppm in weight, more preferably at least 800 ppm in weight, even more preferably at least 1000 ppm in weight, preferably at least 1250 ppm by weight, more preferably at least 1500 ppm by weight, even more preferably at least 1750 ppm by weight, and even more preferably at least 2000 ppm by weight. In an embodiment of the present invention, the anode comprises at least 75.0% by weight of copper, preferably at least 77.5% by weight, more preferably at least 80.0% by weight, even more preferably at least 82.5% by weight, preferably at least 85.0% by weight, more preferably at least 87.5% by weight, even more preferably at least 90.0% by weight, at preferably more than 90% by weight, more preferably at least 91.0% by weight, even more preferably at least 91.5% by weight, preferably at least 92.0% by weight, more preferably at least 92.5% by weight, even more preferably at least 93.0% by weight copper. This has the advantage that the copper production of the cell is higher, and that the measures taken to reduce the problems caused by impurities in the anode are easier to implement and to keep under control. It thus entails the advantage that less anode mucus must be removed and processed, that less anode passivation takes place, and that the cathode quality is higher, both in terms of composition and in terms of physical aspects and the ease with which they can be stripped. BE2019 / 5322 2019/5322 In an embodiment of the present invention, at least a portion of the anode mucus in the cell is removed from the cell with the first flow of electrolyte. The applicants have found that the first flow of electrolyte via the overflow of electrolyte over a cell wall is extremely suitable for carrying part of the anode glue, which for a number of reasons are continuously generated during the electrolytic cycle, in particular the impurities in the anode, as explained above. The applicants have found that especially the mucus particles with a lower density, which are therefore lighter, are more easily entrained with the first flow of electrolyte. In one embodiment of the present invention, the flow of the first electrolyte current is kept positive throughout the electrolytic cycle. Applicants prefer to maintain a positive liquid overflow throughout the entire electrolytic cycle such that the cell is kept full of liquid at any time during the electro refining treatment. This reduces and possibly avoids the risks associated with a decrease in fluid level in an electrolytic cell, allowing electric arcs to be drawn, for example, between naked electrodes or between an electrode and the overhead tap above the cell, which may cause damage to the equipment or pose a safety risk. In one embodiment of the present invention, the cell wall flooded by the first electrolyte current is a side wall that intersects the surfaces of the largest surfaces of the electrodes, the cell preferably having a rectangular base surface (or a horizontal layout) and the side wall that is flooded extends approximately perpendicular to the orientation of the electrodes. Such a side wall is usually the longest in comparison with the end cell walls, which entails the advantage that the liquid flows per unit of cell wall length can be kept lower during flooding. This also has the advantage that the flow direction BE2019 / 5322 2019/5322 BE2019 / 5322 of the electrolyte leaving the cell via the flooding has less influence on the electrode surfaces, which reduces the risk of the electrodes moving due to the outflow of electrolyte. Preferably, the direction of flow of the outflow of electrolyte is parallel to the electrode surfaces, and the lateral pressure of the outflow of electrolyte on the electrodes can be virtually non-existent. Therefore, applicants prefer to have the electrolyte overflow over substantially the full length of at least one cell sidewall, possibly interrupted here and there over limited distances to allow structural elements to pass through for any superstructure of the cell . The applicants have furthermore found that this feature entails the advantage of a more homogeneous spread of the additives in the electrolyte throughout the entire cell, as compared to supplying the electrolyte to one end of the cell and allowing the flooding at the opposite end face of the cell, ie an arrangement where all electrolyte passes through the entire length of the cell and the consumption of additive gradually decreases from supply to outlet due to its consumption. The concentration of these additives is usually checked at the inlet point for the electrolyte in the cell. Because these additives are gradually consumed and / or degraded at the cathode surfaces as the electrolyte moves through the cell from inlet to outlet, this arrangement of electrolyte overflow improves the distribution of the additives over the bath. In an embodiment of the present invention, the first flow of electrolyte is passed through at least one depositing device, ensuring a sufficiently high residence time with a sufficiently low liquid velocity for anode glue to settle on the bottom of the depositing device. Applicants have found that a depositing device is extremely suitable for collecting and removing a large part of the anode mucus entrained in the cell overflow before this electrolyte can be recirculated to the electrolytic cell. This step of removing anode mucus from the electrolyte overflow, especially when cleaned 2019/5322 BE2019 / 5322 electrolyte is recirculated, is a first step to control the concentration of anode mucus in the electrolytic cell, in particular the fine and / or light anode mucus particles that are formed during the electrolytic cycle. This greatly contributes to the ability of the anodes to contain higher levels of impurities. Applicants prefer to provide a plurality of precipitation devices. In one embodiment, a flocculant is added to the electrolyte on the way to the depositing device. This promotes the solidification of particles and the settling of the anode mucus on the bottom of the precipitation device. It entails the additional advantage that less fine anode adhesives are recirculated to the electrolytic cell, thereby improving control of the presence of anode adhesives in the cell, and consequently also the quality of the cathodes produced. In an embodiment of the present invention wherein the method comprises the depositing device on the first current electrolyte, a third current electrolyte containing anode glue is removed from the bottom of the depositing device. The formation of this third electrolyte current is a second step in controlling the anode mucus concentration in the electrolytic cell, in particular the fine and / or light anode mucus particles that are formed during the electrolytic cycle. This second step allows for continuous operation of the depositing device, which facilitates its use and at the same time allows more frequent access to the anode slurries that collect at the bottom of the depositing device, with the associated advantages discussed elsewhere in this document which concerns easier access to anode adhesives. Applicants prefer to periodically generate this third flow of electrolyte containing anode adhesives from the same depositing device. Because the time is provided for a layer of anode glue to accumulate at the bottom of the depositing device, the third flow of electrolyte can be richer in anode glue, and further processing can be more efficient, simpler, more efficient and more rewarding. 2019/5322 In an embodiment of the present invention, a second stream of electrolyte containing anode glue is removed from the bottom of at least one electrolytic cell. The applicants have found that part of the anode mucus succeeds in sinking to the bottom of the cell and reaching the space in the cell below the level at which the gas is introduced. In this lower zone, the liquid moves much less, and the anode mucus particles that reach this zone easily form a layer of electrolyte on the bottom of the cell that is very rich in anode mucus. Applicants also prefer to remove this anode mucus by withdrawing the second stream of electrolyte containing anode mucus from the bottom of the electrolytic cell. In an embodiment of the present invention, the second flow of electrolyte is removed during the electrofining treatment from a bottom portion of the cell provided below the electrodes for collecting anode mucus. Applicants have found that it is advantageous to remove the second current from the cell during the electrolytic cycle, and more preferably while the electro refining is in operating mode, i.e. with the electrical current passing through the cell. Applicants have found that it is possible to remove the second stream from the cell while the cell is in full operation. This entails the advantage, in comparison with many of the methods described in the art, that the cell does not have to be taken out of service to remove the anode mucus layer that collects at the bottom of the cell, and that it it is easier to control the presence of anode mucus in the cell throughout the electrolytic cycle. Applicants prefer to provide a space under the electrodes in the cell, more preferably also under any equipment provided for introducing gas into the cell. In this soil space, the liquid flows slower and with less turbulence, due to the absence of gas bubbles. Applicants prefer to provide the supply of electrolyte to the cell at a level above this bottom portion such that even the shortest fluid path between this fluid inlet point and the BE2019 / 5322 2019/5322 BE2019 / 5322 47 electrolyte overflow over the at least one cell wall does not pass along the bottom space which is provided for collecting the heavy part of the anode mucus that is formed, and therefore does not disturb that space either. In an embodiment of the present invention, the second and / or third stream of electrolyte containing anode glue is sucked up from the bottom of the cell and / or from the bottom of the depositing device, preferably by a suction head moving over the bottom of the cell and / or precipitation device. Applicants, preferably at regular intervals during the electrolytic cycle and while the electrolytic cell is in operating mode, cause a nozzle to pass through the cell in a space provided under the electrodes and also under any equipment provided for introducing gas into the cell, but above a space provided in the bottom portion of the cell for collecting the anode mucus particles. A suitable method for removing the second and / or third flow of electrolyte containing anode slime is by sucking up the flow by means of a suction nozzle that is moved over the bottom of the cell and / or depositing device, preferably above the space that is provided for collecting the anode mucus layer. A suitable method for this is described in WO 00/79025 A1. Applicants prefer to remove the bottom layer of anode slime in the cell before the top of the layer reaches the level in the cell at which the gas is introduced, preferably before the top of the layer reaches the level at which the nozzle passes through the cell is moved to suck up the second stream of electrolyte, which is preferably rich in anode mucus, from the bottom of the cell. Applicants also prefer to provide similar facilities and precautions in the depositing devices through which the first flow of electrolyte runs, the anode adhesives of which are considered to settle largely on the bottom of the depositing device, thereby producing an electrolyte poorer in anode adhesives in comparison with the first electrolyte current leaving the electrolytic cell. 2019/5322 In an embodiment of the present invention, the second electrolyte current is combined with the first and / or with the third electrolyte current to form a combined electrolyte current containing anode adhesives. This entails the advantage that these flows can be processed together, which facilitates downstream processing. In one embodiment of the present invention, the method comprises recirculating to the electrolytic cell electrolyte removed from the cell. This recirculation entails considerable advantages. Recirculating electrolyte entails the advantage that process chemicals in the electrolyte, such as sulfuric acid, are reused. An additional advantage is that compounds that remain soluble in the electrolyte but tend to accumulate during electro-refining are able to concentrate to higher concentrations, making the downstream recovery of these compounds more efficient. In an embodiment of the present invention, the method comprises the removal of an electrolyte tap stream from the electrolyte recirculation. Such a tap current brings about the advantage that the rate at which it is removed is able to control the concentration of compounds in the electrolyte that tend to accumulate in the electrolyte and remain in solution. Such a compound is nickel sulfate, for which the solubility limit is considerable. In one embodiment of the present invention, the drain current is subjected to at least one electrowinning step. Applicants have found that it is advantageous to recover certain metals from this tap stream. The draw-off current contains considerable levels of copper, and a large part of it can be selectively recovered without difficulty by the electrowinning of copper. The draw-off current can also contain substantial nickel contents. These too can be selectively recovered by nickel electrowinning, a method that is similar to, but also somewhat BE2019 / 5322 2019/5322 differs from copper electrowinning, and which functions better once the copper content of the electrolyte has been reduced to a level that is at most 20 grams / liter, preferably at most 15 grams / liter, more preferably at most 10 grams / liter, even more preferably not more than 5 grams / liter, and even more preferably not more than 1 gram per liter, preferably not more than 750 milligrams / liter, more preferably not more than 500 milligrams / liter, more preferably at most 250 milligrams / liter, preferably at most 100 milligrams / liter, more preferably at most 50 milligrams / liter, even more preferably at most 10 milligrams / liter. In one embodiment of the present invention, most of the metals are removed from the drain stream, thereby forming a stream of "black acid", i.e., a stream of concentrated acid. This stream of black acid usually and advantageously has a higher concentration of acid than the electrolyte. Applicants prefer to remove the metals, in particular the nickel, by evaporating water from the drain stream, preferably after reducing the copper content as described above. As a result of this evaporation, nickel sulfate is concentrated above its solubility limit, and it crystallizes. The nickel sulfate crystals can then be recovered by sedimentation, filtration, centrifugation or combinations thereof. In one embodiment of the present invention, the black acid stream is recirculated to the electrolytic cell, the black acid stream preferably being recirculated after additional copper cations have been added to the black acid. This entails the advantage that most of the acid in the draw-off stream can be reused, and less acid compensation is required to maintain the acid concentration in the electrolyte at the desired level. The applicants have furthermore found that the black acid, because of its high acid concentration, in particular when it is higher than that of the electrolyte in the cell, is extremely suitable for dissolving copper in it, as discussed later in this document. In addition to its contribution to maintaining the acid concentration in the electrolyte, the BE2019 / 5322 2019/5322 black acid recycle stream containing additional copper cations to maintain the concentration of copper cations in the electrolyte at the desired operating concentration. In an embodiment of the present invention, anode glue is separated from at least one of the first, second and / or third electrolyte current, preferably from the combined electrolyte current containing anode glue, preferably upstream of the removal of an electrolyte tap current from the electrolyte recirculation wherein the anode adhesives are preferably removed as a solid, more preferably with the aid of a filter press or a tube press. This entails the advantage that the anode mucus concentration in the electrolytic cell is kept under control. Applicants prefer to carry out this separation of anode glue from the electrolyte as pure as possible, in order to reduce the presence in the anode glue by-product of copper and / or nickel, at least the copper and / or nickel dissolved in the electrolyte. In an embodiment of the present invention wherein the anode slime is removed as a solid and wherein the solid anode slime is rinsed with water before the anode slime by-product is recovered from the general process, the rinse water is recirculated to the electro refining process. The same rinsing water can be further used, after the described rinsing step, and / or may have already been used before the described rinsing step, for other useful purposes such as rinsing the spent anodes and / or cathodes after they have been removed from the electrolytic cell, and / or for dissolving components to be added to the electrolytic cycle, such as additives or additional copper cations, before being recirculated to the electro refining process. The rinsing of the solid anode mucus brings with it the advantage that a smaller amount of the soluble metals, in particular copper and / or nickel, leaves the process with the anode mucilage product, in which they do not contribute much value but usually form a burden. By recirculating this used BE2019 / 5322 2019/5322 BE2019 / 5322 rinsing water, more of these soluble metals can be kept in the process, after which they can be more advantageously removed as part of the tapping stream, from which they can be recovered more easily. In an embodiment of the present invention in which the solid anode adhesives are flushed with water, the flushing of the anode adhesives with water is carried out at a temperature of at least 40 ° C, preferably at least 50 ° C, more preferably at least 60 ° C, even more preferably at least 65 ° C, and at most 90 ° C, preferably at most 85 ° C, more preferably at most 80 ° C, even more preferably at most 75 ° C. Applicants have found that a higher rinse water temperature helps to rinse the sulphate salts from the solid anode slime, in particular the copper sulphate and / or nickel sulphate. Because the used rinsing water is fed back into the electrolyte cycle, it is advantageous if the rinsing water has a temperature close to the desired electrolyte temperature, since this reduces the need for possible heating and / or cooling with a view to suitable heat management in the electrolyte cycle. . Applicants have also found that compliance with the specified upper temperature limit reduces the risk of damage to the building material of the equipment. For example, the filter plates of the filter or filter press used to stop the anode mucus while flushing with water may be made of polypropylene, and applicants have found that this material is less susceptible to wear at a temperature corresponding to the indicated upper limit. In an embodiment of the method of the present invention, the anode slips that have been recovered, preferably after water rinsing, are treated with a sufficient amount of base, preferably NaOH, to convert the majority of the metal sulfates to a soluble sulfate salt, such as Na 2 SO 4, and insoluble metal hydroxides. In this way the sulfur content of the anode mucus can be reduced, which improves their acceptability for the downstream recovery of the metals, inter alia because the concentration of their metals is higher. Processes for the recovery of metal are 2019/5322 generally provide better for the processing of metal oxides and / or hydroxides. Other types of base materials are often preferably roasted to obtain their oxides before the metals can be recovered. The hydroxides are preferably heated to form oxides, and in a pyrometallurgical process step carried out in an oven, using a reducing agent such as iron, a multi-metal solder can be recovered from the anode slime, and a slag containing iron oxide as a by-product. To extract Sn from the slag to the metal phase, and to improve the physical phase separation between the soldering phase and the slag phase, additional lead may be added, preferably until the tin / lead weight ratio in the metal phase approaches 1/3. In one embodiment of the present invention, additional copper cations are introduced into the electrolyte in the cell. Applicants have found that various metal impurities in the anode consume electrical current when they dissolve into the electrolyte, in addition to the current consumed by the anode copper that turns into solution. At the cathode, this extra current leads to more copper being deposited than copper was dissolved at the anode. So more copper is deposited on the cathode than copper comes into solution at the anode. This imbalance means that net copper is consumed from the electrolyte. To compensate for this net consumption, extra copper cations are added to the electrolyte in the electrolytic cell. Applicants have found that the copper imbalance gains in importance as the content of impurities in the anode increases. While conventional electro-refining processes, starting with anodes comprising 98-99 wt.% Copper, usually work without the addition of additional copper cations to the electrolyte, the applicants have found that that addition is extremely advantageous in the method of the present invention, wherein the anodes contain less copper and more other metals. Applicants have found that the addition allows the method to function over a long period of time, with intensive recirculation of BE2019 / 5322 2019/5322 electrolyte, and with a high concentration of copper cations in the electrolyte, which is particularly advantageous at the cathode, where the high concentration contributes to high productivity of the process with lower energy consumption and better cathode quality. The applicants have even found that adding extra copper cations to the electrolyte helps to keep the concentration of copper cations within the desired levels, which is important to maintain the production of high quality copper cathodes in the long term without causing additional operating problems or to arise. Applicants have found that this issue is more important with anode compositions that contain a higher content of impurities. Applicants have also found that this feature makes it possible not to have to stop the process due to depletion of the copper concentration in the electrolyte below the minimum desired level, as in several of the methods disclosed in the art. In an embodiment of the present invention wherein additional copper cations are added to the electrolyte, the additional copper cations are introduced into the electrolyte supply to the cell, preferably into the electrolyte that is recirculated to the electrolytic cell. Applicants have found that this is an extremely convenient method of controlling the copper concentration in the electrolyte at the desired level. In an embodiment of the present invention where additional copper cations are added to the electrolyte, a liquid stream comprising at least a portion of the recirculated electrolyte, and / or a stream with an even higher concentration of acid, such as at least a portion of the recirculated black acid, or at least part of the tap stream after the removal of copper by electrowinning, if present, or at least part of the acid compensation for the process, contacted with a copper-containing solid to dissolve more copper in the liquid stream, preferably in a leaching vessel, before the liquid stream with the additional copper cations is transferred to the electrolytic cell. The applicants BE2019 / 5322 2019/5322 BE2019 / 5322 find these currents extremely suitable for dissolving copper from a copper-containing solid and thus picking up additional copper cations that are useful for controlling the copper concentration in the electrolyte in the electrolytic cell. Applicants prefer to use a current that is available and that has a higher acid concentration than the electrolyte. Eligible streams are, for example, the black acid recirculation stream, because that stream is more acidic and therefore more easily dissolves copper from a solid source. However, the volumes of this black acid recycle stream are relatively small compared to the process electrolyte supply, and may also be available only intermittently. The process also usually requires acid compensation, e.g., to compensate for the loss of acid in the formation of nickel sulfate and / or lead sulfate. Such an acid compensation stream can also be a highly concentrated acid stream, such as at least 50% by weight sulfuric acid, possibly even 96% by weight sulfuric acid, which in that case is also able to more easily dissolve copper from a solid source, compared to with the electrolyte being recycled to the cell. The compensation volumes are also relatively small, and may not be added continuously. Applicants therefore prefer to use an acid stream with a higher concentration than the electrolyte that is recirculated to the cell, such as the black acid recirculation stream and / or the sulfuric acid compensation stream, if available, but otherwise they prefer it to use the electrolyte recirculation current to pick up an amount of additional copper cations on the way to the cell. In one embodiment of the present invention, the copper-containing solid is in the form of beads, the beads preferably being hollow and open, the beads optionally being produced in a pyrometallurgical process step upstream of the process. Applicants have found that the copper-containing solid is preferably in a finely divided form, as compared to large blocks, because the finely divided form offers more contact surface to the extraction fluid for the same amount 2019/5322 BE2019 / 5322 solid. Applicants have found that granules are easier to process than powder. Granules can be easily stacked in a leaching vessel, and can be held in the vessel through a simple sieve provided on the liquid outlet nozzle. Preferably, the grains are hollow, providing more contact surface for the same weight of solid material. Applicants have found that it is extremely practical if the grains of copper-containing material are produced in a pyrometallurgical process step that is upstream of the method of the present invention. Most practically, this upstream process step is part of the process by which the copper intermediate is used that is used for casting the anodes used in the electrolytic step of the process of the present invention. The material of the beads may be identical to the material used for the anodes, or may have other characteristics. Preferably, the grains are of copper material with a higher purity than the anodes. Applicants prefer to produce small, large surface copper grains by splashing molten molten copper onto a refractory brick above the liquid level of a large reservoir containing a cold liquid such as water. The liquid molten copper current is broken up on the refractory brick and spreads in the cold liquid. This brings with it the advantage of locally strong steam development, resembling an explosion, and leading to the formation of small, large surface copper grains, or "shots", which are highly suitable for dissolving in an acidic liquid. Applicants prefer to provide at least one leaching vessel or tower for the addition of additional copper cations in the process. Such a vessel can be a vertically cylindrical vessel. The vessel can be open at the top to the atmosphere such that the copper-containing solids can be easily introduced into the vessel. The solids can form a layer on a support at the bottom of the vessel, above the inlet for the supply of liquid. The fluid inlet is advantageously provided under the layer support. The 2019/5322 BE2019 / 5322 liquid flows up through the layer of solids and leaves the vessel via an overflow line. The vessel is preferably designed such that the upward velocity of the liquid is low, and the specific gravity of the copper-containing solids is sufficiently high to prevent solids from the leaching vessel from being entrained with the liquid outlet. Preferably the copper-containing solids are of high purity, such as blister copper, with at least 98% by weight of Cu. As the copper dissolves, the height of the layer decreases, and the supply of solid copper parts can be replenished via the open top of the vessel. In an embodiment of the present invention, oxygen-containing gas is added to the step of contacting the liquid stream with the copper-containing solid. The applicants have found that the copper from the grains is more easily dissolved in the acid leaching liquid under an oxidizing atmosphere. Preferably, the applicants inject air or enriched air, more preferably commercially available oxygen gas, into the bottom portion of the leaching vessel, preferably under the support of the layer on which the solids are retained. The applicants have found that the presence of oxygen in the leaching step greatly promotes the pick-up of copper cations by the leaching liquid. In an embodiment of the present invention, additional sulfuric acid is introduced into the process, preferably into the recirculated electrolyte, if present, preferably together with or upstream of the introduction of the additional copper cations, if present. This feature yields a sulfuric acid compensation current which is useful for controlling the electrolyte sulfuric acid content that would otherwise run out due to the consumption of sulfate anions in lead and / or nickel sulfate. As discussed above, applicants prefer to use for this compensation a concentrated source of sulfuric acid, such as 96% by weight sulfuric acid, and prefer to introduce this compensation acid where it comes into contact with the copper-containing solids 2019/5322 BE2019 / 5322 to pick up extra copper cations. Compensation with a high acid concentration entails the advantage that it entails little risk that undesired elements are introduced into the process. An additional advantage is that it takes up much less volume and its processing is much less difficult compared to a less concentrated stream, and that the copper dissolves into it more easily. In one embodiment of the present invention, the gas introduced into the cell is air. Applicants prefer to use air for bubbling through the electrolytic cell, instead of the possible alternatives nitrogen, carbon dioxide, or even sulfur dioxide (SO 2 ) as proposed in U.S. Pat. No. 1,260,830 and by EN Petkova in Mechanisms or floating slime formation and its removal with the help of sulphur dioxide during the electrorefining of anode copper ”, Hydrometallurgy, Vol. 46, Number 3, October 1997, pp. 277-286. Applicants prefer air because of its ease of use and the aspects of improved safety and industrial hygiene. The use of nitrogen and / or carbon dioxide would entail the risk that staff would be inadvertently exposed to clouds of an oxygen-poor atmosphere. Sulfur dioxide is also a toxic gas with a sharp, irritating odor, and therefore requires stricter safety and industrial hygiene measures. Air entails the additional advantage that it is an oxidizing agent, which is extremely advantageous because it is able to oxidize As 3+ to As 5+ and / or to oxidize Sb 3+ to Sb 5+ , so that these metals are be able to form compounds, usually salts, such as arsenals, or oxides, that sink more easily to the bottom of the cells and / or the depositing devices and collect in the layer of anode slime. These phenomena are described in more detail by CAMöller et al. In “Effect of As, Sb, Bi and Oxygen in Copper Anodes During Electrorefining,” Proceedings of Copper 2010, pp. 1495-1510. Air is a much more practical oxidizing agent for applicants than sulfur dioxide for the reasons explained above. 2019/5322 In one embodiment of the present invention the gas introduced into the cell is at a temperature in the range of the electrolyte temperature +/- 30 degrees Celsius. This reduces any temperature effects that the introduction of gas could locally cause into the cell. Preferably, the gas temperature differs at most 25 degrees Celsius from the temperature of the electrolyte in the cell, more preferably at most 20 degrees Celsius, even more preferably at most 15 degrees Celsius. Local decreases in temperature are undesirable because they may cause some salts to crystallize locally, such as around the holes in the gas distributor, which could hamper gas flow through those holes. A local increase in temperature is also undesirable because it can lead to a faster degradation of some of the additives in the process. Applicants prefer to introduce the gas into the cell at a temperature of about 45 ° C. Applicants prefer to maintain the electrolyte in the cell at a temperature in the range of 65-70 ° C, preferably about 68 ° C. In one embodiment of the present invention, the gas introduced into the cell is at least saturated with water at the temperature at which the gas is introduced. This reduces the risk of crystallization in and around the opening through which the gas enters the electrolyte. In one embodiment of the present invention, water is injected into the gas, preferably as an aerosol, before the gas is introduced into the cell. Applicants prefer to inject sodium-poor water, preferably below the detection limit, the injected water preferably being obtained by reverse osmosis. Applicants have found that this feature reduces the formation of salts at the injection points of the gas into the electrolyte, and also at any microporous polymer jacket that may be provided around the tubes of the gas diffusion device. In one embodiment of the present invention, the gas bubbles that pass through the electrolyte have one BE2019 / 5322 2019/5322 BE2019 / 5322 average diameter in the range of 1 to 3 mm. Applicants have found that gas bubbles of up to 3 mm in diameter are more effective at removing depleted electrolyte at the surfaces of the cathodes to allow fresh electrolyte to come into contact with the cathodes. The small gas bubbles also usually minimize the formation of acid mist above the electrolysis cell. Smaller gas bubbles are also preferred because they set up a cell regime similar to a so-called “Dissolved Air Flotation” regime (DAF regime) such that small particles of anode mucus are easily brought to the surface of the liquid column and easily leave the cell via the flood. The size of the gas bubbles can be determined, for example, as set forth by Reza Al Shakarji et al., In "The sizing of oxygen bubbles in copper electrowinning", Hydrometallurgy, 109 (2011), pp. 168-174. In an embodiment of the present invention, the gas is introduced into the cell via a gas diffusion device located below the electrodes, but above the space provided in the bottom of the cell to collect the layer of anode glue, the gas diffusion device preferably comprises selectively perforated diffusion pipes connected to the gas supply pipe. The location of the gas diffusion device divides the vertical height of the electrolyte volume into two parts, the upper part, through which gas bubbles rise which cause more turbulence, and the lower part without gas bubbles, which is more stationary, in particular as well as the electrolyte supply approximately at the height. is provided with the gas diffusion device. The extra turbulence in the upper part brings with it the advantages that are discussed in detail above. The lower movement of fluid in the lower part promotes the settling of anode mucus particles on the bottom of the cell. Applicants prefer to use a diffusion device as described in WO 2005/019502 A1, using a plurality of hoses made of microporous material, and / or which comprise that material, which, when used, the spray gas in capable of passing through this microporous material such that it forms a plurality of fine bubbles in the electrolyte in the cell. 2019/5322 Applicants have found that the diffuser preferably has a uniformly distributed presence of gas bubbles provided by the entire upper portion of the electrolyte volume. A non-uniform presence of gas bubbles can cause differences in hydrostatic pressure on an electrode, which entails the risk that the electrode can be tilted sideways and cause a contact, and thus an electrical short circuit, with an adjacent counter-electrode. Applicants prefer to provide a gradient in the density at which the gas is introduced, wherein less gas is introduced closer to the cell wall with the flood and more gas closer to the opposite cell wall. This entails the advantage that the gas gradient creates an additional driving force for the flow of liquid in the direction of the flood. In an embodiment of the present invention, the gas is introduced into the cell by means of a pressure, in the supply line at the level of the liquid in the cell, in the range of at least 0.5 bar gauge (barg), preferably at least at least 0.6 barg, more preferably at least 0.7 barg. This overpressure is necessary to overcome the hydrostatic pressure at the point where the gas is introduced into the cell, preferably under the electrodes. Applicants prefer to provide an overpressure rather than just the hydrostatic pressure, to enhance the spraying of the gas into the liquid and to promote the formation of smaller gas bubbles. The pressure at the indicated point in the feed line is preferably at most 3.5 barg, preferably at most 3.0 barg, more preferably at most 2.5 barg, even more preferably at most 2.0 barg, at preferably at most 1.75 barg, more preferably at most 1.50 barg, even more preferably at most 1.25 barg. Compliance with this upper limit reduces the risk of electrolyte being blown out of the cell and also of nickel aerosols being formed. Blown electrolyte can cause equipment damage, and the formation of nickel aerosols leads to industrial hygiene problems. BE2019 / 5322 2019/5322 Mainly for industrial hygiene reasons, applicants prefer to provide a lid over the cell that is equipped with an exhaust gas extractor and a drip catcher to prevent drops of acid, possibly containing metal particles, from entering the workspace. In one embodiment of the present invention, the electrolyte in the cell is maintained at a temperature in the range of 20 ° C to 75 ° C. Preferably the electrolyte temperature in the cell is at least 25 ° C, more preferably at least 30 ° C, even more preferably at least 35 ° C, preferably at least 40 ° C, more preferably at least 45 ° C, even more preferably at least 50 ° C, preferably at least 55 ° C, more preferably at least 60 ° C, even more preferably at least 65 ° C, preferably above 65 ° C. At higher temperatures, the diffusion rate of copper is improved, and that is particularly conducive to the distribution of the copper cations by the still or laminar flowing films that are usually present on the surfaces of anode and / or cathode. Higher temperatures also increase the solubility of sulfates in the electrolyte, and therefore reduce the risk of crystallization, especially in sensitive locations. Applicants prefer to keep the electrolyte at a temperature below 75 ° C, preferably at most 72 ° C, more preferably at most 70 ° C. This entails the advantage that the additives that are temperature sensitive, such as gelatin and / or many flocculants, are more stable and less susceptible to degradation. A lower temperature also reduces the risk that the cathode would be stripped prematurely, i.e. the deposited copper layer would come loose from the stainless steel start core while the cathode is still in the electrolytic cell. A lower temperature also lowers the energy required to maintain the temperature of the electrolyte, which is usually above the ambient temperature and thus requires heat input. In an embodiment of the present invention, the anode composition and / or the molten liquid metal composition of the present invention comprises at least BE2019 / 5322 2019/5322 0.25 wt% nickel, preferably at least 0.50 wt%, more preferably at least 0.75 wt%, even more preferably at least 1.00 wt%, preferably at least 1.25% by weight, more preferably at least 1.50% by weight, even more preferably at least 2.00% by weight, preferably at least 2.10% by weight, with more preferably at least 2.25 wt%, even more preferably at least 2.50 wt%, preferably at least 2.75 wt%, more preferably at least 3.00 wt% nickel. A higher nickel content in the anode allows the upstream process to accept more base materials that contain substantial amounts of nickel. Such base materials are difficult to process for most electrical refining processes, and are therefore easier to obtain at more economically favorable conditions. Optionally, the composition of the anode comprises at most 10.0% by weight of nickel, preferably at most 9.0% by weight, more preferably at most 8.0% by weight, even more preferably at most 7 00% by weight, preferably at most 6.00% by weight, more preferably at most 5.50% by weight, preferably at most 5.00% by weight, more preferably at most 4 , 50% by weight, preferably at most 4.00% by weight, more preferably at most 3.50% by weight of nickel. At lower levels of nickel in the composition of the anode, the tapping current can be kept smaller, which simplifies its further processing and reduces the associated operating costs. Lower levels of nickel also reduce the need to add additional copper cations to the electrolyte. Less nickel also reduces passivation of the anode, which makes it possible to apply the measures taken to prevent anode passivation less strictly and / or less intensively. Less nickel also reduces industrial hygiene problems associated with nickel aerosols. In an embodiment of the present invention, the anode composition and / or the molten liquid metal composition of the present invention comprises at least 0.25% by weight of lead, preferably at least 0.50% by weight, more preferably at least 0.75% by weight, even more preferably at least 1.00% by weight, preferably at least 1.25% by weight, more preferably at least 1.50% by weight BE2019 / 5322 2019/5322 BE2019 / 5322 lead. Allowing a higher level of lead in the anode allows the upstream process to be carried out with a lower strictness regarding the separation between lead and copper, and also to accept more base materials containing substantial amounts of lead. Such base materials are difficult to process for many copper production processes, and are therefore easier to obtain at more economically favorable conditions. Optionally, the composition of the anode comprises at most 6.00% by weight of lead, preferably at most 5.00% by weight, more preferably at most 4.00% by weight, even more preferably at most 3 00% by weight, and even more preferably not more than 2.50% by weight, preferably not more than 2.00% by weight, more preferably not more than 1.80% by weight, even more more preferably at most 1.60% by weight, and even more preferably at most 1.50% by weight of lead. At lower levels of lead in the composition of the anode, less lead sulfate is formed in the cell. The consumption of acids towards lead sulphate is thereby reduced. Lead sulfate has a very low solubility in the electrolyte and will therefore crystallize easily in the cell. The crystals entail the risk that they end up in the cathode. A lower level of lead in the anode therefore reduces the risk that lead is entrained as an impurity in the cathode. The precipitated lead is preferably removed from the cell as part of the anode mucus in the first electrolyte current and / or in the second electrolyte current. Since the presence of lead does not contribute significantly to the value of the anode slurries produced by the method, but does contribute to the operating load for processing the anode slime, a lower presence of lead in the anode is advantageous because it reduces the volume of the reduces anode mucus, and therefore its operating load, without reducing the value of the anode mucilage from the process. A lower level of lead in the composition of the anode also reduces the risk of lead being released into the work area during human intervention, eg when the anode slime comes loose from the filter press, with which industrial hygiene hazards are associated. 2019/5322 BE2019 / 5322 In an embodiment of the present invention, the anode composition and / or the molten liquid metal composition of the present invention comprises at least 0.25% by weight of tin, preferably at least 0.50% by weight, more preferably at least 0.75% by weight, even more preferably at least 1.00% by weight, preferably at least 1.25% by weight, more preferably at least 1.50% by weight of tin. Allowing a higher tin content in the anode allows the upstream process to be carried out with a lower strictness regarding the separation between tin and copper, and also to accept more base materials containing substantial amounts of tin. Such base materials are difficult to process for many copper production processes, and are therefore easier to obtain at more economically favorable conditions. In addition, the tin in the anode mucus is relatively easy to recover therefrom, and represents a significant portion of the commercial value available from the anode mucus by-product of the method of the present invention. Optionally, the composition of the anode comprises at most 6.00% by weight of tin, preferably at most 5.00% by weight, more preferably at most 4.00% by weight, even more preferably at most 3 , 00% by weight, and even more preferably at most 2.50% by weight, preferably at most 2.00% by weight, more preferably at most 1.80% by weight, even more more preferably a maximum of 1.60% by weight of tin. At lower levels of tin in the composition of the anode, the volume of anode mucus is reduced, since tin essentially leaves the process as an oxide of tin or tin plus antimony, both of which are expected to end up in the anode mucus. Less tin in the anode therefore lowers the burden of processing the anode slime. A lower tin content in the anode reduces the risk that tin is entrained as impurity in the cathode. Less tin also reduces the risk of growth of solid SnSb compounds on the wetted surfaces of the electrolytic cycle, especially in and around the electrolytic cells. In an embodiment of the present invention, the composition comprises the anode and / or the molten liquid 2019/5322 metal composition according to the present invention at least 0.10% by weight of antimony, preferably at least 0.15% by weight, more preferably at least 0.20% by weight, even more preferably at least 0.25% by weight, preferably at least 0.30% by weight, more preferably at least 0.35% by weight, preferably at least 0.40% by weight, more preferably at least 0.50% by weight antimony. Allowing a higher level of antimony in the anode allows the upstream process to be conducted with a lower strictness regarding the separation between antimony and copper, and also to accept more base materials containing substantial amounts of antimony. Such base materials are difficult to process for many copper production processes, and are therefore easier to obtain at more economically favorable conditions. Optionally, the composition of the anode comprises at most 3.00% by weight of antimony, preferably at most 2.50% by weight, more preferably at most 2.00% by weight, even more preferably at most 1 , 50% by weight, and even more preferably at most 1.25% by weight, preferably at most 1.00% by weight, more preferably at most 0.90% by weight, even more more preferably at most 0.80% by weight of antimony. At lower levels of antimony in the composition of the anode, there is less risk of forming SnSb oxide compounds, which may come out of solution and form solid deposits and grow on the wetted surfaces of the electrolytic cycle, especially in and around the electrolytic cells. A lower level of antimony in the anode reduces the risk that antimony is included as impurity in the cathode. The antimony is preferably removed from the cell as part of the anode mucus in the first electrolyte stream and / or in the second electrolyte stream, usually in the form of a metal-metal oxide, e.g., tin with antimony. Because the presence of antimony hardly makes any contribution to the value of the anode glue produced by the method, but does contribute to the operating load for processing the anode glue, a lower presence of antimony in the anode is advantageous because the volume of the anode slime is reduced, and therefore the burden of its processing is reduced without the value BE2019 / 5322 2019/5322 BE2019 / 5322 66 to reduce the anode mucilage by-product obtained from the process. In an embodiment of the present invention, the anode composition and / or the molten liquid metal composition of the present invention comprises at least 0.010% by weight of bismuth, preferably at least 0.015% by weight, more preferably at least 0.020% by weight %, even more preferably at least 0.025% by weight, preferably at least 0.030% by weight, more preferably at least 0.035% by weight of bismuth. Allowing a higher bismuth content in the anode allows the upstream process to be carried out with a lower strictness regarding the separation between bismuth and copper, and also to accept more base materials containing substantial amounts of bismuth. Such base materials are difficult to process for many copper production processes, and are therefore easier to obtain at more economically favorable conditions. Optionally, the composition of the anode comprises at most 0.50% by weight of bismuth, preferably at most 0.25% by weight, more preferably at most 0.200% by weight, even more preferably at most 0.150% by weight. %, and even more preferably not more than 0.100% by weight, preferably not more than 0.090% by weight, more preferably not more than 0.080% by weight, even more preferably not more than 0.070% by weight of bismuth . A lower bismuth content in the anode reduces the risk that bismuth is included as impurity in the cathode. The bismuth is preferably removed from the cell as part of the anode mucus in the first electrolyte stream and / or in the second electrolyte stream, presumably as a metallic bismuth and / or as an arsenate, such as BiAsO4, if sufficient arsenic is present. Since the presence of bismuth hardly makes any contribution to the value of the anode adhesives produced by the method, but does contribute to the operating load for processing the anode adhesives, a lower presence of bismuth in the anode is advantageous because it reduces the volume of the anode mucus is reduced, and therefore the burden of its processing is reduced, without reducing the value of the anode mucilage product obtained from the process. 2019/5322 In an embodiment of the present invention, the anode composition and / or the molten liquid metal composition of the present invention comprises at least 0.0010% by weight of zinc, preferably at least 0.0050% by weight, more preferably at least 0.0075 wt%, even more preferably at least 0.010 wt%, preferably at least 0.015 wt%, more preferably at least 0.020 wt% zinc. Allowing a higher zinc content allows the upstream process to be carried out with a lower strictness regarding the removal of zinc from the copper-containing currents leading to the composition of the anode, and also to accept more base materials that have significant amounts of zinc. Such base materials are difficult to process for many copper production processes, and are therefore easier to obtain at more economically favorable conditions. Optionally, the composition of the anode comprises at most 0.50% by weight of zinc, preferably at most 0.25% by weight, more preferably at most 0.200% by weight, even more preferably at most 0.150% by weight. %, and even more preferably not more than 0.100% by weight, preferably not more than 0.090% by weight, more preferably not more than 0.080% by weight, even more preferably not more than 0.070% by weight, preferably at most 0.050% by weight, more preferably at most 0.025% by weight of zinc. A lower zinc content in the anode reduces the risk that zinc is included as impurity in the cathode. The zinc is preferably removed from the process as part of the tap current from the electrolyte cycle and / or as part of the anode slime in the first electrolyte current and / or in the second electrolyte current. Since the presence of zinc makes hardly any contribution to the value of the anode glue and / or the drain current produced by the method, but does contribute to the operating load for processing the anode glue and / or the drain current, a lower presence is of zinc in the anode is advantageous because it reduces the volume of the anode mucus, and consequently reduces the burden of its processing, without reducing the value of the anode mucus by-product obtained from the process. BE2019 / 5322 2019/5322 The same applies to the value of the tap current and the processing load thereof. In an embodiment of the present invention, the composition of the anode comprises at least 0.005% by weight of arsenic, preferably at least 0.010% by weight, more preferably at least 0.020% by weight, even more preferably at least 0.025 % by weight, preferably at least 0.050% by weight, more preferably at least 0.060% by weight, even more preferably at least 0.070% by weight, and even more preferably at least 0.075% by weight % arsenic. Allowing a higher level of arsenic in the anode allows the upstream process to be carried out with a lower strictness regarding the removal of arsenic from the copper-containing currents that lead to the composition of the anode, and also to produce more base materials containing significant amounts of arsenic. Such base materials are difficult to process for many copper production processes, and are therefore easier to obtain at more economically favorable conditions. Arsenic is also said to decrease anode passivation, and it is capable of forming intermetal compounds, such as arsenates, such as SbAsO4 and BiAsO4, that easily come out of solution and introduce other metal impurities into the anode mucus. A higher content of arsenic can therefore also have the advantage of a reduced anodic passivation and a smoother removal of other metal impurities by causing them to end up in anodic adhesives. Optionally, the composition of the anode comprises at most 0.40% by weight of arsenic, preferably at most 0.30% by weight, more preferably at most 0.250% by weight, even more preferably at most 0.200% by weight. %, and even more preferably not more than 0.175% by weight, preferably not more than 0.150% by weight, more preferably not more than 0.125% by weight, even more preferably not more than 0.100% by weight of arsenic . A lower arsenic content in the anode reduces the risk that arsenic is included as impurity in the cathode. The arsenic is preferably removed from the cell as part of the anode mucus in the first electrolyte stream and / or in the second electrolyte stream, e.g. as an arsenate of another metal impurity such as antimony or bismuth, or as BE2019 / 5322 2019/5322 a mixed oxide such as 2As 2 O 5,3Sb 2 O 3, or by being bound and / or entrapped in the oxides of tin and / or tin plus antimony. Since the presence of arsenic makes hardly any contribution to the value of the anode mucus produced by the method, but does contribute to the operating load for processing the anode mucus, a lower presence of arsenic in the anode is advantageous because the volume of the anode mucus is reduced, and therefore the burden of its processing is reduced, without reducing the value of the anode mucilage product obtained from the process. In an embodiment of the present invention, the anode composition and / or the molten liquid metal composition of the present invention comprises at least 0.0001% by weight of silver, preferably at least 0.0010% by weight, more preferably at least 0.0050 wt%, even more preferably at least 0.0100 wt%, preferably at least 0.0150 wt%, more preferably at least 0.0200 wt%, with even more preferably at least 0.0250 wt%, preferably at least 0.0300 wt%, more preferably at least 0.0350 wt%, even more preferably at least 0.0400 wt- % silver. Silver leaves the method of the present invention without problems, usually as part of the anode mucus, and silver greatly contributes to the value of the anode mucous by-product of the method of the present invention. A higher content of silver is therefore preferred because it makes the processing of the anode slime, and the recovery of the metals present therein, more economically rewarding. Optionally, the composition of the anode and / or molten liquid metal composition according to the present invention comprises at most 0.50% by weight of silver, preferably at most 0.25% by weight, more preferably at most 0.200% by weight %, even more preferably not more than 0.150% by weight, and even more preferably not more than 0.100% by weight, preferably not more than 0.075% by weight, more preferably not more than 0.060% by weight, with even more preferably at most 0.050% by weight of silver. A high presence of silver increases the risk of silver being absorbed into the cathodes. The silver in the copper anode contributes no additional economic value and BE2019 / 5322 2019/5322 therefore means a deterioration compared to silver in the anode slime. Silver is an undesirable impurity in cathode copper because it poses technical problems with the main end-use copper, i.e. copper wire drawing. In an embodiment of the present invention, the composition of the anode comprises at most 0.0500 wt% or 500 ppm in wt. oxygen, preferably at most 0.0400% by weight, more preferably at most 0.0300% by weight, even more preferably at most 0.0200% by weight, and even more preferably at most 0 , 0180% by weight, preferably at most 0.0150% by weight, more preferably at most 0.0125% by weight, even more preferably at most 0.0100% by weight or 100 ppm in weight . oxygen. Applicants prefer that the oxygen content remains below the indicated limit because an excessively high presence of oxygen increases the risk of malformation of the anode during casting and cooling, as explained elsewhere in this document. For this reason, the applicants prefer that the composition of the anode contain oxygen below the indicated upper limit. Optionally, the composition of the anode comprises at least 0.0005 wt% or 5 ppm in wt. oxygen, preferably at least 0.0010 wt%, more preferably at least 0.0015 wt%, even more preferably at least 0.0020 wt%, preferably at least 0.0025 wt. %, more preferably at least 0.0030% by weight, even more preferably at least 0.0040% by weight, preferably at least 0.0050% by weight, more preferably at least 0.0075 wt%, even more preferably at least 0.0100 wt% or 100 ppm in wt. oxygen. Applicants have found that it is preferable not to reduce the oxygen content in the anode composition to very low levels. The burden and the effort required to obtain very low levels of oxygen in the composition of the anode are not compensated by an equivalent economic advantage. On the contrary, the additional efforts that are usually made to further reduce the oxygen content below the indicated lower limit are usually difficult, BE2019 / 5322 2019/5322 BE2019 / 5322 complicated, and often also cause some valuable metals to be removed from the anode composition, thereby reducing their volume and creating lower value side currents. For that reason, applicants prefer that the oxygen content in the anode composition satisfies the stated lower limit. In one embodiment of the present invention, the anode composition is the molten liquid metal composition of the present invention whose oxygen content is further reduced, preferably to make it fall within the concentration range indicated for the anode composition of the process according to the present invention, for example from 5 ppm in wt. up to and including 500 ppm in weight .. In an embodiment of the present invention, the electrolyte composition satisfies at least one and preferably all of the following conditions: • copper in the range of 20 to 55 grams / liter, • nickel in the range of 25 to 90 grams / liter, • sulfuric acid in the range of 130 to 200 grams / liter, preferably at most 190 grams / liter, more preferably at most 180 grams / liter, even more preferably at most 170 grams / liter, and even more preferably at most 160 grams / liter, and optionally at least 140 grams / liter, tin in the range of 0.4 to 1.4 grams / liter, preferably at most 1.2 grams / liter, more preferably at most 1.0 grams / liter, even more preferably at most 0.90 grams / liter liters, and even more preferably at most 0.80 grams / liter, and arsenic in the range of 10 to 200 milligrams / liter, preferably at least 15 milligrams / liter, more preferably at least 20 milligrams / liters and optionally at most 175 milligrams / liter, preferably at most 150 milligrams / liter, more preferably at most 100 milligrams / liter, even more preferably at most at least 75 milligrams / liter, and with even more preference at most 2019/5322 milligrams / liter. Applicants have found that it is advantageous to keep the dissolved copper content of the electrolyte within the prescribed limits, because that range provides an excellent balance between its positive action at the cathode, where a high concentration helps for diffusion through the still film on the cathode surface, and its possible negative effect at the anode, where a high concentration reduces the driving force for diffusion through the still film on the anode surface. Applicants prefer to keep the nickel content in the electrolyte within the prescribed limits, preferably at least 30 grams / liter, more preferably at least 35 grams / liter, even more preferably at least 40 grams / liter liters, preferably at least 45 grams / liter, more preferably at least 50 grams / liter, even more preferably at least 55 grams / liter, preferably at least 60 grams / liter, more preferably at least 65 grams / liter . A higher nickel content increases the value of the drain stream from which the nickel can be recovered by its further processing, due to the higher amount of nickel present, but also because its recovery becomes more efficient. On the other hand, a higher nickel content in the electrolyte also increases the risk that locally, for example in cold zones or in drops of electrolyte that are splashed on parts of equipment that are not immersed in the electrolyte but that can be hot, nickel sulphate comes out of solution and forms a solid that can interfere with or even hinder proper operation of the equipment. For these reasons, applicants prefer to keep the nickel content in the electrolyte at a level of at most 85 grams / liter, preferably at most 80 grams / liter, more preferably at most 75 grams / liter, even more preferably at most 70 grams / liter. The applicants have found that it is advantageous to keep the sulfuric acid content of the electrolyte within the prescribed limits, because that range provides an excellent balance between its positive action, on the one hand, and metals BE2019 / 5322 2019/5322 BE2019 / 5322 to dissolve the electrolyte from the anode and to impart electrical conductivity to the electrolyte, and on the other hand to its possible negative effect by increasing the density and viscosity of the electrolyte, which is detrimental to the transfer of mass and heat and the sedimentation rate of anode glues, and the risk of damage to the equipment that may come into contact with the electrolyte. Higher concentrations of sulfuric acid may involve the need to choose rarer and therefore more expensive construction materials, i.e., additional investment costs that can be avoided by meeting the indicated upper limit. Applicants have found that tin dissolved in the electrolyte tends to form so-called "floating mucus", anode mucus particles that do not sink to the bottom in the electrolytic cell, nor do they sink to the bottom in a precipitator where the residence time is significantly higher and the fluid rates may be significantly lower than in the cell. Thus, such floating slime is not removed from the electrolyte by the various features of the method as described for the removal of anode slime. Applicants wish that the content of arsenic in the electrolyte remains below the indicated upper limit. The presence of arsenic above the indicated lower limit may be advantageous because the anode passivation mechanism reduces, and is able to introduce more of other contaminating metals into intermetal compounds that are solid and become part of the anode mucus. However, more arsenic than the indicated upper limit in the electrolyte can be disadvantageous because it leads to more arsenic in the tap stream that requires further processing to recover most of the metal contained therein, and also causes more arsenic to end up in the anode mucilage by-product. More arsenic can lead to additional burdens for the further processing of the anode mucus and / or the drain current which is removed from the electrolytic cycle, to the extent that it can even lead to the need for an additional step in the respective 2019/5322 BE2019 / 5322 further processing thereof. More arsenic does not provide any additional value for the by-product streams, and its content is therefore preferably kept below the indicated upper limit. On the other hand, applicants have found that low levels of arsenic, in accordance with the indicated lower limit, are acceptable because the additional burden or restrictions that would entail demanding an even lower arsenic content are not fully offset by the additional benefits of the lower presence of arsenic. In an embodiment of the present invention, at least one and preferably all of the following process chemicals are added to the electrolyte as indicated: Surfactants (e.g. gelatin) in the range of 25 to 900 grams / tonne cathode copper produced, preferably at least 50 grams / tonne, more preferably at least 100 grams / tonne, even more preferably at least 150 grams / ton, preferably at least 200 grams / ton, more preferably at least 250 grams / ton, preferably at least 300 grams / ton, more preferably at least 350 grams / ton, even more preferably at least 400 gram / ton, and even more preferably at least 450 gram / ton, preferably at least 500 gram / ton, more preferably at least 600 gram / ton and optionally at most 800 gram / ton, preferably at most 700 gram / ton, more preferably not more than 600 grams / ton, even more preferably not more than 500 grams / ton, even more preferably not more than 400 grams / ton, preferably not more than 350 grams / tonne of cathode copper produced, • hydrochloric acid (HCl ) in the range of 25 to 250 grams of HCl per tonne of cathode copper produced, hydrobromic acid (HBr) in the range of 25 to 400 grams of HBr per tonne of cathode copper produced, • at least one flocculant in the range of 800 to 3000 milligrams per tonne of cathode copper produced, preferably at least 1000, possibly at most 2500, preferably at most 2000, more preferably at most 1500 milligrams / ton 2019/5322 BE2019 / 5322 75 produced cathode copper, and thiourea in the range of 15-150 grams per tonne produced cathode copper. Applicants prefer to add at least one surfactant to the electrolyte. Applicants have found that the surfactants reduce / prevent the growth of dendrites on the cathodes, thereby reducing the risk of short circuit formation. Applicants have found that gelatin is a very suitable surfactant component. Applicants have found that the prescribed dosage range, and typically 650 grams of gelatin per tonne of cathode copper produced, is sufficiently effective without causing additional problems or irresponsible operating costs. Applicants prefer to add hydrochloric acid (HCl) to the electrolyte. The hydrochloric acid entails the advantage that the polymerization of gelatin that may be added is prevented, and that its polymer chains are cut into smaller pieces so that the gelatin retains its activity. More importantly, the chlorine of the hydrochloric acid is able to bind silver (Ag) in an insoluble form (AgCl), which easily ends up in the anode slime, and can be removed from the process in a practical manner such that a large part of the silver can be recovered economically. Applicants prefer to add at least 30 grams of hydrochloric acid per tonne of cathode copper produced, preferably at least 50 grams, more preferably at least 75 grams, even more preferably at least 100 grams per tonne of cathode copper produced, and optionally at most 225 grams, preferably at most 200 grams, more preferably at most 175 grams, preferably at most 150 grams per tonne of cathode copper produced. Applicants find it most practical to add the hydrochloric acid as a 30 wt% solution, and prefer to add about 430 milliliters thereof 2019/5322 per tonne of cathode copper produced, but other concentrations can also be used if that is practical. Applicants prefer to also add hydrobromic acid (HBr) to the electrolyte, in the indicated dosage range. Applicants prefer to add at least 30 grams of hydrobromic acid per tonne of cathode copper produced, preferably at least 50 grams, more preferably at least 75 grams, even more preferably at least 100 grams per tonne of cathode copper produced, and optionally not more than 350 grams, preferably not more than 300 grams, more preferably not more than 250 grams, preferably not more than 200 grams per tonne of cathode copper produced. Applicants prefer to typically add about 125 grams of HBr per tonne of cathode copper produced. The hydrobromic acid has the same advantages as the hydrochloric acid. The addition of hydrobromic acid has the additional advantage that its silver salt (AgBr) is even less soluble than the chloride. The hydrobromic acid therefore has the advantage that it is able to remove more silver from the electrolyte to the anode slime. Applicants prefer to use HBr as a 48 wt% solution, but other concentrations may also be used if that is practical. Applicants prefer to use both the HCl and the HBr as indicated. Applicants prefer to add at least one flocculant to the electrolyte, preferably where the electrolyte enters the depositing devices, in the indicated dosage range and typically about 1035 milligrams per tonne of cathode copper produced. We prefer to use a cationic polyacrylamide, based on adipic acid, which is for example available under the trademark ZETAG®, type 7565. Applicants also prefer to add thiourea to the electrolyte, preferably where the electrolyte enters the depositing devices, at a dosage ratio of 15150 grams per tonne of cathode copper produced, preferably at least 18, with BE2019 / 5322 2019/5322 BE2019 / 5322 more preferably at least 20, even more preferably at least 25, and even more preferably at least 30 and optionally at most 125 grams, preferably at most 100 grams, more preferably at most 75 grams, with still more more preferably at most 50 grams, and even more preferably at most 49 grams, and typically about 32 grams of thiourea per tonne of cathode copper produced. The thiourea is added to (together with the above-mentioned process chemicals) influence the deposition morphology (roughness and / or formation of nodules), the crystal form (round and / or sharp) and the grain type (elongated and / or field oriented), which is largely results in the avoidance of lumps, porosity and dendrites in the cathode. More information about the functions of thiourea and other additives in electro refining are described by Baumback J, Bombach H and Stelter M, "Investigations of the Behavior of Thiourea and alternative Additives in Copper Electrorefining", Proceedings EMC, 1 (2015), p 151-160. Applicants prefer not to exceed the indicated upper limit in order to keep the amount of sulfur in the cathodes low. In one embodiment of the present invention, the cathode starter cores are made of stainless steel, preferably SS316L steel or "duplex steel". Applicants have found that the deposited copper layer can be stripped without problems from a starter core in stainless steel, and that the starter cores that remain thereby can be reused without any problems with a minimum of reprocessing for a new cathode campaign in the electrolytic cell. In one embodiment of the present invention, the cathode spacing is at least 95 mm, preferably at least 100 mm, more preferably at least 105 mm, even more preferably at least 110 mm, preferably at least 115 mm, more preferably at least at least 120 mm. Although a smaller cathode spacing is advantageous for the electrical resistance through the cell, and therefore also for the energy required for the electro refining treatment, the applicants have found that the high content of impurities in the composition of the anode entails additional risks on the formation 2019/5322 BE2019 / 5322 and growth of dendrites, which cause a short circuit between a cathode and a neighboring anode. In order to reduce the interventions by operators required to remedy such a short circuit, the applicants prefer to maintain the cathode distance as indicated. The applicants have furthermore found that a higher cathode distance entails the advantage of a higher cathode purity, despite a lower anode purity. In the context of the present invention, cathode distance is understood to mean the distance from the center of one cathode starter core to the corresponding center of the adjacent cathode starter core, which means the thickness of one cathode and one anode, added to twice the distance between a cathode surface and the cathode surface. surface of the neighboring anode facing the cathode surface. In an embodiment of the present invention, the at least one cathode is refreshed with a frequency that is higher than the refresh frequency of the anode. Applicants prefer to replace the cathodes in the cell at a higher frequency with new starter cores than the spent anodes in the same cell are replaced with newly cast anodes. This entails the advantage that the cathodes are easier to strip because the layer of deposited copper is less thick. An additional advantage is that the thinner copper layer on the cathode reduces the risk of damage to the starting core during stripping. An additional advantage is that a higher cathode replacement frequency reduces the risk of a short circuit occurring in the cell during the electro refining treatment. Such a short circuit requires intervention by operating personnel, which is labor intensive. Applicants have found that it is possible and advantageous to partially replace the cathodes from a particular electrolytic cell, e.g. only one third of the cathodes at a time. This entails the advantage that the electrolytic cell can be operated during cathode replacement even at its full production rate. Applicants consider it advantageous to replace cathodes number 1,4, 7, 10, etc. with starter cores, and if that 2019/5322 BE2019 / 5322, once cathodes number 2, 5, 8, 11, etc. have been replaced by starting cores, and once they have been replaced, the remaining cathodes numbers 3, 6, 9, 12, etc. replaced by starter cores. Applicants have found that it is possible to keep the electrolytic cell in operation during a cathode replacement performed in this way. Applicants have found that the cell can be kept in full operation, and that the 2/3 of the cathodes present in the cell can handle the full current density during the short periods of time required to replace 1/3 of the cathodes with new ones starter cores. Applicants have found that it is possible without problems to reduce the oxygen content of the metal composition of the present invention to a preferred level for the composition of the anode as part of the process of the present invention. The benefits obtained by bringing the oxygen content of the metal composition in accordance with the present invention within the limits of the composition of the anode as part of the process of the present invention are described elsewhere in this document. Applicants prefer to reduce the oxygen content of the metal composition of the present invention by a process step called "poling". In a "poling" step, the molten liquid metal composition is contacted with a source of carbon. The carbon reacts with the oxygen in the metal composition and forms carbon oxides, CO + CO2, gases escaping from the molten liquid metal composition and forming a reducing atmosphere above the liquid metal bath. The carbon source can be any practically carbonaceous material, such as any hydrocarbon, such as natural gas or a liquid hydrocarbon, carbon black, charcoal, coal, any organic material, including wood. Applicants prefer to use natural gas because of its ease of use. Due to the operating conditions in which the composition melted 2019/5322 BE2019 / 5322 and is liquid, it is easy to create intensive contact and the carbon in the carbon source reacts easily with the oxygen in the composition to form carbon oxides (CO or carbon dioxide) escaping as gas from the molten liquid metal composition, wherein the metal bound to the oxygen remains in its elemental form. The "poling" is preferably carried out at a temperature of at least 1150 ° C, such that the molten liquid bath becomes very fluid, and any slag is preferably first removed from the liquid metal bath. The off-gas from the "poling" step is preferably subjected to a post-combustion step to convert the carbon monoxide into carbon dioxide before it is discharged. Applicants have found that it is very practical to correctly dose the carbon source to reduce the oxygen content to within the desired range for the composition of the anode as part of the method of the present invention. The molten liquid metal composition of the present invention preferably further comprises, as part of the impurities, at least one and more preferably all of the following elements in a content that meets the respective limit indicated for each element: • at least 0.10% by weight and / or at most 3.00% by weight of antimony, • at least 0.010% by weight and / or at most 0.5% by weight of bismuth, • at most 6 .00% by weight of tin, • at most 6.00% by weight of lead, • at least 0.0001% by weight and at most 0.50% by weight of silver, • at least 0.005% by weight and at most 0.40% arsenic by weight, • at least 0.001% by weight and at most 0.100% by weight of sulfur, and • at most 0.50% by weight of zinc. In one embodiment, the molten liquid metal composition of the present invention comprises sulfur within the indicated range, preferably at least 0.005% by weight, more preferably at least 0.010% by weight and optionally at most 2019/5322 0.080% by weight, preferably at most 0.070% by weight, more preferably at most 0.060% by weight. Applicants have found that a limited amount of sulfur can be allowed in the molten liquid metal composition, and that it entails the advantage that the acceptability criteria are broadened for the base materials of the upstream process, which is therefore able to absorb more sulfur. in its raw materials. Applicants have also found that it is advantageous to keep the sulfur in the molten liquid metal composition in accordance with the upper limit, because more sulfur increases the risk that more sulfur ends up as cathode impurity, and also causes more sulfur to end up in the anode slime. The latter may be undesirable if the anode adhesives are to be further processed by means of a method comprising a pyrometallurgical step, because the sulfur in the anode adhesives can then generate sulfur oxide gases (SO2 and / or SO3). In an embodiment of the method according to the present invention, at least a part of the method is electronically monitored and / or controlled, preferably by a computer program. Applicants have found that electronically controlling steps of the method of the present invention, preferably through a computer program, entails the advantage of much better processing, with results that are much more predictable and that are closer to the objectives of the method. method. For example, the driver can be based on temperature measurements, and if desired also based on measurements of pressures and / or levels, and / or in combination with the results of chemical analyzes of samples taken from process flows and / or analytical results obtained online , control the equipment with regard to the supply or consumption of electrical energy, the supply of heat or a cooling medium, or a flow and / or pressure control. Applicants have found that such monitoring or control is particularly advantageous in steps performed in continuous mode, but that it can also be advantageous in BE2019 / 5322 2019/5322 BE2019 / 5322 steps that are executed in batch or semi-batch mode. In addition and preferably, the results of monitoring obtained during or after performing steps in the method are also useful for monitoring and / or controlling other steps forming part of the method of the present invention, and / or of methods used upstream or downstream of the method of the present invention, as part of a global process of which the method of the present invention is only a part. Preferably the entire global process is electronically monitored, more preferably by at least one computer program. The global process is preferably controlled electronically as much as possible. Applicants prefer that the computer control also means that data and instructions are passed from one computer or computer program to at least one other computer or other computer program or other module of the same computer program, for monitoring and / or controlling other methods, including but not limited to the methods described in this document. EXAMPLE The following example shows a preferred embodiment of the present invention. The example is further illustrated by the Figure, showing a flow diagram of the core part of an embodiment of the method according to the present invention. In that part of the process, starting from the composition of the anode 1, a cathode product 6, an anode slime product 4, a drain product 5 and a spent anode product 7 are recovered. The figure shows the figures for the following elements of the conclusions: 1. Anodes 2. Copper shots 3. Black acid 4. Anode gluing 2019/5322 5. Drain current 6. Cathodes 7. Used anodes A crude, molten, copper-based, liquid metal composition that further contained nickel, tin, lead, and other minor metals was prepared in accordance with the method described in our related patent application PCT / EP2018 / 084384 filed December 11 2018. The composition is shown in more detail in Table I. Table I: Crude molten liquid metal composition BE2019 / 5322 % by weight Cu 92.80 Ni 3.08 Sn 1.39 Pb 1.71 Sb 0.65 Ag 0.04 Ash 0.10 Bi 0.05 Fe 0.02 S 0.02 Zn 0.03 Oxygen 0.10 Total 99.99 The composition further contained about 5 ppm by weight. in gold (Au). The crude, molten, liquid copper-based metal composition was introduced into an oven, and brought to a temperature of about 1200 ° C by burning natural gas in the oven. Remaining slag that floated on the molten metal was poured off. Natural gas was injected into the liquid metal until the oxygen content of the liquid metal was reduced to the range of 20-170 ppm by weight. The liquid molten metal with the reduced oxygen content was then cast into thin, flat plates that formed the anodes 1 for subsequent electro refining, and allowed to cool to ambient temperature. 2019/5322 BE2019 / 5322 A total of 52 anodes with an average weight of 444 kg and 51 stainless steel plate start plates (starter cores) were immersed in each of 100 electrolytic cells (200) containing an acidified copper sulfate solution at 68 ° C, which acted as the electrolyte. The average electrolyte composition during the entire electrolysis cycle is shown in Table II, in grams / liter for the major components and in ppm in wt. for the less important components. Table II: Average electrolyte composition gram / liter Cu 39.8 Ni 67.7 Sn 0.93 ppm by weight Sb 344.7 Ash 63.1 Bi 9.0 Fe 403.1 Already 152.5 CD 29.7 The concentration of sulfuric acid was maintained at an average concentration of 160 grams / liter by introducing concentrated sulfuric acid (96%), when and if required, into the leaching vessel described below. The following feed additives flow rates were maintained on average throughout the electrolysis cycle, by introducing them into the electrolyte inlet to the depositing devices (300): • Gelatin at approximately 650 grams / tonne of cathode copper produced, • HCl in a solution of 30% by weight, at approximately 430 milliliters / tonne of cathode copper produced, • HBr in a solution of 48% by weight, at approximately 176 milliliters / tonne of cathode copper produced, 2019/5322 BE2019 / 5322 • ZETAG® type 7565 flocculant, a cationic polyacrylamide, at approximately 1035 milligrams per tonne of cathode copper produced, • Thiourea at approximately 32 grams per tonne of cathode copper produced The average composition of the anodes (stream 1) is shown in Table III. Table III: Average anode composition % by weight Anodes1 Cu 92.90 Ni 3.08 Sn 1.39 Pb 1.71 Sb 0.65 Ag 0.04 Ash 0.10 Bi 0.05 Fe 0.02 S 0.02 Zn 0.03 Oxygen 0.02 Total 100.01 The anodes further contained about 5 ppm by weight. in gold (Au). The anodes (current 1) and stainless steel starter cores were alternately arranged (120 mm spacing) in an electrically parallel arrangement, while the electrolytic cells themselves were connected in series. An average current density of 290 A / m 2 was applied, whereby an average electrical potential was generated between the anodes (positive electrodes) and the cathodes (negative electrodes) of 0.46V. The passage of the electric current causes copper to oxidize and to pass into solution via the electrochemical reaction path. However, a quantity of copper will also pass into solution via the purely chemical reaction path. All elements (metals) that are present in the 2019/5322 anodes and which are less noble than copper in the given process conditions will also to some extent pass into solution at the anodes. The electrochemically and chemically dissolved metals other than copper were continuously removed by means of a drain current of electrolyte. This tap stream was subjected to a further purification step (not shown) in which the metals were selectively removed and a purified electrolyte remained. This prevents the impurities from accumulating in the electrolyte during electro refining and prevents the impurities from depositing on the cathodes. The purified draw-off stream, also called black acid, was recirculated in the electrolyte circuit as stream 3. The average composition of the draw-off current and the average composition of the black acid are shown in Table IV. Table IV: Average composition of tapping stream and black acid BE2019 / 5322 % by weight Drain current5 Black acid3 Cu 3.32 0.0000 Ni 5.15 0.0930 Sn 0.02 0.0000 Pb 0.0013 0.0000 Sb 0.0001 0.0000 Ag 0.0001 0.0000 Ash 0.0014 0.0390 Bi 0.0000 0.0000 Au 0.0000 0.0000 Fe 0.03 0.0155 Pt 0.0000 0.0000 S 6.57 22.0501 Zn 0.03 0.0000 The copper that dissolved from the anodes flowed through the electrolyte solution to the cathodes, where the copper was plated on the stainless steel starter plates to produce copper cathodes. The electrolyte was supplied to one end of the cell. The cell wall with the flood was a side wall, perpendicular to the orientation of the electrodes. The flow of electrolyte was kept positive throughout the electrolytic cycle. An average refresh rate of approximately 2019/5322 55% cell volume per hour for each cell was used in combination with the blowing of heated air under the electrodes to prevent anode passivation. The incoming air was saturated with water vapor at a temperature close to that of the electrolyte before spraying via a gas diffuser and was introduced into each cell with an average pressure of 0.75 barg. All cells were regularly inspected during electro refining to detect short-circuit anode / cathode pairs using a Gaussmeter mounted on the overhead tap. Short circuits were repaired by repairing the gap between the anodes and cathodes involved or by removing electro-deposited copper lumps that had formed between the shorted anode / cathode pairs. Properly controlling all of these parameters led to high quality cathodes. The average cathode composition (stream 6) is shown in Table V. The cathode deposits obtained during electro-refining were clarified and smoothed by continuously supplying the organic additives gelatin and thiourea (stream 8) just upstream of the pump system to achieve a good mix. Table V: Average cathode composition BE2019 / 5322 % by weight Cathodes6 Cu 99.9761 Ni 0.0025 Sn 0.0069 Pb 0.0020 Sb 0.0029 Ag 0.0063 Ash 0.0007 Bi 0.0001 Au 0.0000 Fe 0.0002 Pt 0.0000 S 0.0016 Zn 0.0001 Total 99.99994 2019/5322 Gold and the metals from the platinum group did not dissolve in the sulfate electrolyte and therefore did not end up in the electrolyte or were not plated at the cathode, as seen in Table II and Table V. Silver was dissolved to some extent from the anodes but was caused to precipitate from the electrolyte as AgCl and AgBr by adding small amounts of HCl and HBr to the electrolyte (stream 8). The fact that silver still appears in the cathode is probably mainly due to the inclusion of a small amount of anode residues. Lead and tin formed compounds that are insoluble in the electrolyte, and therefore these metals barely end up in the electrolyte. The majority of the insoluble impurities from the anodes accumulated as undissolved mucus at the bottom of the electrolytic cells. These mucus were periodically removed from the cells (400) during the electro-refining treatment by a suction head that moved over the bottom portion of the cell, and which was provided under the electrodes. Some insoluble impurities were lighter and left the cells via the cell overflows to the precipitators (300). These lighter mucus were also periodically removed from the bottom of the depositing devices (400), after the mucous had been allowed to settle after adding flocculant to the electrolyte on its way to the depositing device. In this way, all anode adhesives were collected in a combined electrolyte stream containing anode adhesives, after which they were further processed by a filter press (500) that separated the anode adhesives (stream 4) from the clear electrolyte. A portion of this clear electrolyte was recirculated to the circulation reservoirs (100). Another portion of the clear electrolyte was removed as a tap current (stream 5) to remove impurities such as copper and nickel that would otherwise accumulate in the electrolyte by electrowinning. The anode adhesives were flushed with heated water at 70 ° C to reduce the amounts of copper and nickel that were present in the electrolyte. The rinsing water was recirculated to the electro refining process. The average anode adhesive composition (stream 4) is shown in Table VI. It BE2019 / 5322 2019/5322 BE2019 / 5322 additional part of the composition is probably formed by oxygen and an amount of carbon, probably from the organic process additives. Table VI: Average composition of anode adhesives % by weight Anode gluing4 Cu 5.40 Ni 1.87 Sn 17.17 Pb 21.21 Sb 8.05 Ag 0.43 Ash 1.29 Bi 0.62 Fe 0.07 S 6.98 Zn 0.12 The anode adhesives were furthermore found to be approximately 60 ppm by weight. to gold and about 5 ppm by weight. to contain platinum. To compensate for the electrochemical dissolution of impurities at the anodes, which would otherwise lead to the depletion of copper in the electrolyte, copper-containing hollow and open nuggets (stream 2) obtained from an upstream process step were leached (600) into a leaching vessel by contacting the copper-containing nuggets with the concentrated sulfuric acid used for compensation, the black acid stream that returned from processing the tap stream, and also with a portion of the electrolyte. The liquid product from the leaching vessel was recirculated in the electrolyte circuit during the electro refining process. The average composition of the nuggets used (stream 2) is shown in Table VII. The dissolution of the copper nuggets was promoted by introducing oxygen gas to the bottom of the leaching vessel. 2019/5322 Table VII: Average composition of copper nuggets BE2019 / 5322 % by weight Copper nuggets 2 Cu 95.75 Ni 1.63 Sn 0.98 Pb 1.13 Sb 0.31 Ag 0.03 Ash 0.03 Bi 0.03 Fe 0.01 S 0.02 Zn 0.09 The gold and platinum content in the copper nuggets was less than 1 ppm by weight. At the end of an anode cycle, approximately 75% of each anode was dissolved. The undissolved residues of the anodes (anode scrap) were removed from the electrolytic cells as spent anodes (stream 7) and, after rinsing, weighing and stacking, were melted and re-cast as fresh anodes. The average composition of the spent anodes was of course the same as the average anode composition shown in Table III. The method described above made it possible to work with standard electrolysis cycles of 24 days per cell, i.e. a period of 24 days of continuous operation between the introduction of a new series of anodes. The cathodes were pulled out approximately every 8 days, and they were replaced by 1/3 at a time, while the electrolysis was continued, and at full current density. The anode slips were removed from the bottoms of the cells, with a frequency as needed, which could vary from once every 3 days to once every 10 days, also while the electrolysis was continued at full current density. Now that this invention has been fully described, it should be apparent to those skilled in the art that the invention can be practiced within a wide range of parameters within what is claimed, without 2019/5322 fall outside the scope of the invention as defined by the claims.
权利要求:
Claims (42) [1] CONCLUSIONS A method for the production of copper comprising electro refining from copper metal in an electrolytic cell of at least one copper anode to at least one copper cathode, using an electrolyte based on sulfuric acid, characterized in that • the voltage difference between the anode and the cathode in the electrolytic cell is maintained at less than 1.6 volts, • the anode comprises at most 98.0% by weight of copper, • the anode comprises less than 1.00% by weight of iron, • the current density through it the cell is at least 180 A / m 2 cathode area, • electrolyte is removed from the electro-refining cell during the electro-refining treatment with an average electrolyte exchange rate of at least 30% and at most 1900% per hour, and the electrolyte is removed at least partially by flooding of a first flow of electrolyte over at least one cell wall, and • a gas is introduced into the cell and bubbled through the electrolyte between the anode and the cathode. [2] The method of claim 1 wherein the anode comprises at least 75.0 wt% copper. [3] The method of claim 1 or 2 wherein at least a portion of the anode mucus in the cell is removed from the cell with the first electrolyte stream. [4] The method of any one of the preceding claims, wherein the flow of the first electrolyte current is kept positive throughout the electrolytic cycle. [5] The method of any one of the preceding claims, wherein the cell wall flooded by the first flow of electrolyte is a side wall that intersects the surfaces of the largest surfaces of the electrodes, the cell preferably having a rectangular base surface and the side wall that is flooded extends approximately perpendicular to the orientation of the electrodes. BE2019 / 5322 [6] The method according to any of the preceding claims, wherein the first flow of electrolyte is passed through at least one depositing device, ensuring a sufficiently high residence time with a sufficiently low liquid velocity for anode mucus to settle on the bottom of the depositing device . [7] The method according to the preceding claim wherein a flocculant is added to the electrolyte, preferably on the way to the precipitation device. [8] The method of claim 6 or 7, wherein a third stream of electrolyte containing anode glue is removed from the bottom of the depositing device. [9] The method of any one of the preceding claims, wherein a second stream of electrolyte containing anode glue is removed from the bottom of the at least one electrolytic cell. [10] The method according to the preceding claim wherein the second flow of electrolyte is removed during the refining treatment from a bottom portion of the cell provided below the electrodes for collecting anode mucus. [11] The method according to any of claims 8 to 10 wherein the second and / or third stream of electrolyte containing anode glue is sucked up from the bottom of the cell and / or from the bottom of the depositing device, at preferably by a suction head that moves over the bottom of the cell and / or precipitation device. [12] The method according to any of claims 8 to 11, wherein the second electrolyte current is combined with the first and / or with the third electrolyte current to form a combined electrolyte current containing anode adhesives. [13] The method of any one of the preceding claims, comprising recycling to the electrolytic cell electrolyte removed from the cell. [14] The method of the preceding claim, which comprises removing an electrolyte tap stream from the BE2019 / 5322 electrolyte recirculation. [15] The method of the preceding claim wherein the drain current is subjected to at least one electrowinning step. [16] The method of claim 14 or 15 wherein most of the metals are removed from the tap stream, thereby forming a stream of "black acid", i.e., a stream of concentrated acid. [17] The method of the preceding claim wherein the black acid stream is recycled to the electrolytic cell, the black acid stream preferably being recycled after additional copper cations have been added to the black acid. [18] The method according to any of the preceding claims, wherein anode glue is separated from at least one of the first, second and / or third electrolyte current, preferably from the combined electrolyte current containing anode glue, preferably upstream of the removal of an electrolyte tap stream from the electrolyte recirculation, wherein the anode adhesives are preferably removed as a solid, more preferably with the aid of a filter press or a tube press. [19] The method according to the preceding claim wherein the anode slime is removed as a solid and wherein the solid anode slime is flushed with water before the anode slime by-product is recovered from the general process, wherein the rinsing water is recirculated to the electro refining process. [20] The method according to the preceding claim wherein the water rinsing of the anode slime is carried out at a temperature of at least 40 ° C and at most 90 ° C. [21] The method of any one of the preceding claims, wherein additional copper cations are introduced into the electrolyte in the electrolytic cell. [22] The method of the preceding claim wherein the additional copper cations are introduced into the BE2019 / 5322 electrolyte supply to the cell, preferably in the electrolyte that is recirculated to the electrolytic cell. [23] The method according to the preceding claim wherein a liquid stream comprising at least a portion of the recirculated electrolyte, and / or a stream with an even higher concentration of acid, is contacted with a copper-containing solid to absorb more copper release into the liquid stream, preferably into a leaching vessel, before the liquid stream that is enriched with the additional copper cations is transferred to the electrolytic cell. [24] The method according to the preceding claim wherein the copper-containing solid is in the form of beads, the beads preferably being hollow and open, the beads optionally being produced in a pyrometallurgical process step upstream of the process. [25] The method of any one of claims 23 to 24 wherein oxygen-containing gas is added to the step of contacting the liquid stream with the copper-containing solid. [26] The method of any one of the preceding claims, wherein additional sulfuric acid is introduced into the process, preferably into the recirculated electrolyte, if present, preferably together with or upstream of the introduction of the additional copper cations, if present. [27] The method of any one of the preceding claims, wherein the gas introduced into the cell is air. [28] The method of any one of the preceding claims, wherein the gas introduced into the cell is at a temperature in the range of the electrolyte temperature +/- 30 degrees Celsius. [29] The method of any one of the preceding claims, wherein the gas bubbles passing through the electrolyte have an average diameter in the range of 1 to 3 mm. BE2019 / 5322 [30] The method of any one of the preceding claims, wherein the gas is introduced into the cell via a gas diffusion device located below the electrodes, but above the space provided in the bottom of the cell around the layer collecting anode glue, wherein the gas diffusion device preferably comprises selectively perforated diffusion pipes connected to the gas supply pipe. [31] The method according to any of the preceding claims, wherein the gas is introduced into the cell by means of a pressure, in the supply line at the level of the liquid in the cell, in the range of at least 0.5 barg . [32] The method of any one of the preceding claims, wherein the electrolyte in the cell is maintained at a temperature in the range of 20 ° C to 75 ° C. [33] The method of any one of the preceding claims, wherein the anode composition meets at least one and preferably all of the following conditions: • comprising nickel in the range of 0.25% by weight up to and including 10.0% by weight, • including lead in the range of 0.25% by weight up to and including 6.00% by weight, including tin in the range of 0.25% by weight up to and including 6.00% by weight, including antimony in the range of 0.10% by weight up to and including 3.00% by weight, including bismuth in the range of 0.010% by weight up to and including 0.50% by weight, • including at least 0.0001% by weight of iron, • including zinc in the range of 0.0010% to 0.50% by weight, Comprising arsenic in the range of 0.005% by weight up to and including 0.40% by weight, including silver in the range of 0.0001% by weight up to and including 0.50% by weight, and BE2019 / 5322 • comprising oxygen in the range of 5 ppm in wt. up to and including 500 ppm in weight .. [34] The method according to any of the preceding claims, wherein the anode is made from the molten liquid metal composition according to any of claims 40-41. [35] The method of any one of the preceding claims, wherein the electrolyte composition satisfies at least one and preferably all of the following conditions: • copper in the range of 20 to 55 grams / liter, • nickel in the range of 25 to 90 grams / liter, • sulfuric acid in the range of 130 to 200 grams / liter, • tin in the range from 0.4 to 1.4 grams / liter, and • arsenic in the range of 10 to 200 milligrams / liter. [36] The method of any one of the preceding claims, wherein at least one and preferably all of the following process chemicals are added to the electrolyte as indicated: • surface-active components (eg gelatin) in the range of 25 to 900 grams / tonne of cathode copper produced, • hydrochloric acid (HCl) in the range of 25 to 250 grams of HCl per tonne of cathode copper produced, • hydrobromic acid (HBr ) in the range of 25 to 400 grams of HBr per tonne of cathode copper produced, • at least one flocculant in the range of 800 to 3000 milligrams per tonne of cathode copper produced, and • thiourea in the range of 15-150 grams per tonne of cathode copper produced. [37] The method according to any of the preceding claims, wherein the cathode starter cores are made of stainless steel, preferably SS316L steel or "duplex steel". [38] The method of any one of the preceding claims, wherein the cathode spacing is at least BE2019 / 5322 Is 95 mm. [39] The method of any one of the preceding claims, wherein the at least one cathode is refreshed with a frequency that is higher than the refresh frequency of the anode. [40] The method according to any of the preceding claims, wherein at least a portion of the method is electronically monitored and / or controlled. [41] 41. A molten liquid metal composition which, preferably after reducing the oxygen content of the composition, is suitable for casting anodes for copper anode electro refining in the process according to any of the preceding claims, and which has at least 90.10 % by weight and up to 97% by weight of copper, the surplus being formed by other elements such as impurities, the molten liquid metal composition comprising as a part thereof: • at least 0.1 wt% nickel, • at least 0.0001 wt% and less than 1.00 wt% iron, and • at least 250 ppm in wt. and at most 3000 ppm in wt. oxygen. [42] The molten liquid metal composition of the preceding claim, further comprising, as part of the impurities, at least one and more preferably all of the following elements in a content that meets the respective limit indicated for each element: • at least 0.10% by weight and at most 3.00% by weight of antimony, • at least 0.010% by weight and at most 0.50% by weight of bismuth, • at most 6.00% by weight. -% tin, • at most 6.00% by weight of lead, • at least 0.0001% by weight and at most 0.50% by weight silver, • at least 0.005% by weight and at most 0 , 40 wt.% Arsenic, • at least 0.001 wt.% And at most 0,100 wt.% Sulfur, and • at most 0.50 wt.% Zinc.
类似技术:
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引用文献:
公开号 | 申请日 | 公开日 | 申请人 | 专利标题 US1260830A|1916-07-18|1918-03-26|Franz Edward Studt|Electrolytic deposition of copper from acid solutions.| US2286240A|1938-03-21|1942-06-16|Nassau Smelting & Refining Com|Refining of nonferrous metals| US3753877A|1970-05-28|1973-08-21|Boliden Ab|Elimination of floating slime during electrolytic refining of copper| US3875041A|1974-02-25|1975-04-01|Kennecott Copper Corp|Apparatus for the electrolytic recovery of metal employing improved electrolyte convection| US3928152A|1974-02-25|1975-12-23|Kennecott Copper Corp|Method for the electrolytic recovery of metal employing improved electrolyte convection| US4033839A|1975-02-26|1977-07-05|Kennecott Copper Corporation|Method for series electrowinning and electrorefining of metals| DE2846692A1|1978-10-26|1980-05-08|Norddeutsche Affinerie|ANODE| CA1152943A|1980-11-13|1983-08-30|Shinichiro Abe|Activity of unrefined copper anodes| US4351705A|1981-06-30|1982-09-28|Amax Inc.|Refining copper-bearing material contaminated with nickel, antimony and/or tin| FI107811B|1999-06-17|2001-10-15|Outokumpu Oy|Device for cleaning the bottom of an electrolysis pool| WO2005019502A1|2003-08-22|2005-03-03|Bhp Billiton Innovation Pty. Ltd.|Gas sparging| CL2010000023A1|2010-01-13|2011-10-07|Ancor Tecmin S A|System for supplying air to a group of electrolytic cells comprising; an air blower, a supply pipe, a flow meter with a flow regulator and connected between a first hose and a second hose; and a process for the operation of a system.| KR101844771B1|2016-12-09|2018-04-05|엔코|A method recovered of high purity copper and valuable metal from the crude copper|BE1027001B1|2019-01-30|2020-08-24|Metallo Belgium|Improved tin production| BE1027795B1|2019-11-22|2021-06-23|Metallo Belgium|Improved copper smelting process|
法律状态:
2020-01-23| FG| Patent granted|Effective date: 20191218 |
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