Chlorine leach process
United States Patent [191 Hougen 51 Apr. 29, 1975 1 CHLORINE LEACH PROCESS [75] Inventor: Leif Reidar Hougen, Kristiansand,  
 Norway [73] Assignee: Falconbridge Nickel Mines Limited,  
 Toronto, Ontario, Canada [22] Filed: Mar. 18, 1971 [21] Appl. No.: 125,682  
 [52] US. Cl 75/101 R; 75/117; 75/118; 75/119; 75/121; 423/581; 423/562; 423/565 [51] Int. Cl.. C22b 15/00; C0lg 55/00; C22b 23/04 Primary Examiner-Edward Stern Attorney, Agent, or Firm-Richard J. Hicks P ZEFEQENTIAL fllCKEL LEACH EWClTOWI n Solution y 9 Filtration N1 Cothodcs Particles qF HICKZll erouo 1 1 ABSTRACT A method for selectively recovering metals from generally sulphidic particulate materials containing metals selected-from nickel. copper and precious metals in which the particulate material is preferentially leached in an agitated chloride solution containing cuprous ions by the action of chlorine. The redox potential of the solution increases upon feeding chlorine thereto and decreases upon feeding particulate material thereto, and the rate of feeding of chlorine is con trolled relative to the rate of feeding of material to control the redox potential substantially at or below a selected potential at which the metal is leached preferentially with respect to other metals in the material. Nickel is leached preferentially with respect to copper and precious metals in a matte, for example, to produce a nickel-rich solution and to concentrate the precious metals in a nickel-depleted residue. The leach residue, or other concentrates containing copper and precious metals may also be treated by the method to selectively dissolve the copper values preferentially to the precious metal values. Dissolved copper in the nickel-bearing leach solutions may be precipitated in a separate tank by agitating the leach solution in the presence of elemental sulphur and nickel sulphide particles having an atomic ratio of nickel to sulphur greater than one, thereby producing copper sulphide and a substantially copper-free nickel-chloride solution which can be separated and the values recovered by conventional means.  
 7 Claims, 5 Drawing Figures PCIFUCIGD of Matte Contcnnin W H r Us) pmc&#39;oufi cztella pp M g c nfomm Voter Vapour Leeched I FCI tntzd 1 4 i 1n 19 2! gg hqto tng Elemanto? 20 U p 2. fiulphur own 0 PIZECIPITA&#39;HOH PATENTEUAPRZQIQYS 3,880,653  
 SHEET 30? 3 CoppElz, CONCENTRATION 53L? IZEDOX POTENTIAL (my) lob  40 60 1&#39; a2 01/ O g 20 m o.  
 ZEDox DTEHT \AL (rm-V) 3: /EIZVENTOR PA TENT A GENT CHLORINE LEACH PROCESS This invention relates to the recovery of metal values from solid particles by chlorine leaching. and more specifically to separation and independent recovery of metals in the group including nickel. copper and precious metals. from particles of mattes. sulphide concentrates and alloys by preferential chlorine leaching of one or more metals from the others. and particularly to separation of nickel from copper and of either or both from precious metals.  
  The patent and general literature describing hydrometallurgical processes for the recovery of metals from solids in chloride solutions is extensive. The processes relate to recovery of metals. including substantially all the base metals. from a wide variety ofmattes. sulphide concentrates and ores using different combinations of many leaching reagents including chlorine. hydrochloric acid. hypochlorous acid. sodium hypochlorite. ferric chloride. cupric chloride. manganic chloride. sodium chloride. calcium chloride and other alkaline and alkaline-earth metal chlorides.  
  Few references. however. relate to the use of chlorine and a redox couple. such as cuprous-cupric chloride. to leach mattes. sulphide concentrates and alloys. particularly those containing metals selected from the group nickel. copper. and precious metals. and these will be discussed in detail hereinbelow. Reference is also made to known processes for precipitation of dissolved metal values using sulphur in elemental and combined form.  
  In US. Pat. No. 2.186.293 a process is described for recovery of nickel from matte by leaching in a solution containing cupric chloride and sufficient nickel chloride that the cuprous chloride formed upon dissolution of nickel remains in solution. The leach solution and residue are separated. nickel and copper are recovered from solution. by electrolysis. and cupric chloride is regenerated for further leaching by reacting the solution remaining from the electrolysis with the chlorine produced thereby and returning the liquor to the leaching circuit. In addition to dissolution of substantially all the nickel. over 90% of the copper and some of the precious metals are also dissolved and no means are taught for separation of metal values by preferential leaching. Furthermore large volumes of solution must be circulated relative to the matte treated. specifically over 9.3 litres of solution per kilogram of matte which implies high capital and operating costs for solution handling.  
  in contrast thereto. in the practice of the present invention there is a low flow of solution per unit of solids treated. for example only about 2.5 litres per kg of solids treated. The smaller amount of solution per unit of solids means not only improved economics but also a greater pick-up of metal during leaching.  
  A process for chlorine leaching of metals from sulphide ores is described in US. Pat. No. 1.943.337. The process is similar to that outlined above. but in this case the chlorine is fed to the same vessel in which the ore is treated thereby regenerating the redox leaching agent. such as ferric chloride. as it is consumed. As in the previous patent. however. no reference is made to preferential leaching of one metal from the solids with respect to other metals therein. The object of the process is clearly to leach as much metal value as possible from solids and there is no teaching of the possibility or desirability of preferential (or selective) leaching.  
  US. Pat. Nos. 2.829.966 and 2.835.569 relate to methods for recovery of gold from arsenuireted ores containing nickel. cobalt and iron. Ore is leached in a mixture of HCl and chlorine to dissolve all the base metals. and the progress of the leach is followed by continuous monitoring of the redox potential. After dissolution of all the metals except gold. the continued addition of chlorine to the leach slurry causes an abrupt rise in potential until gold starts to dissolve. after which sufficient additional chlorine is fed to the slurry to dissolve most of the gold. Thus substantially all the metals in the ore are leached and are present together in the same leach liquor from which they must be laboriously separated. No mention is made of either an intention or means to leach one or more (of the base) metals selectively from the others or from the gold.  
  The lack of reference in these patents to either an interest in or a means for preferential leaching of metals from sulphides is consistent with the general literature on the leaching of sulphides by chlorides and chlorine. In summary. the conclusion may be drawn that the prior art merely recognized that complete dissolution of all metal values in chloride solution is extremely rapid and therefore no attempt has been made to selectively leach one metal relative to another.  
  Various methods for separation of metals dissolved in aqueous solutions have been described. Referring specifically to the separation of dissolved nickel and copper. for example. one means that is well known in the art is precipitation of copper sulphide under the action of H 8. Another is cementation of copper metal by me tallic iron. A variation of this latter scheme is the method described in US. Pat. No. 2.180.520. in which the role of iron is replaced by nickel to avoid contaminating the nickeliferous solution with iron. According to the process of this patent. a chloride solution containing both nickel and copper is generated by leaching of matte with cupric chloride. the solution is diluted with water. and is then treated with a nickel-copper matte to precipitate dissolved copper. It is clear from the specification that the copper is precipitated as metal by metallic nickel in the matte. the presence of which is ensured by limiting the sulphur content of the matte to a maximum of one third its copper content. It is presumably for this reason that the initial relatively concentrated chloride leach solution is first diluted since the efficiency of precipitation of copper as metal from solution of high chloride ion concentration is known to be poor. Even after dilution. however. the copper is not completely precipitated in one stage. According to the examples in the patent. sufficient nickel was provided in the added matte to precipitate more than 3.100 kg ofCu while there were only 2.800 kg of Cu in solution to begin with and not all of it was precipitated.  
  There are references to precipitation of copper under the action of sulphides. particularly iron sulphide. but precipitation is highly inefficient. requiring many times the amount of iron sulphide stoichiometrically required to precipitate all the copper. and it is suspected that the bulk of precipitation which does occur results from the cementing action of metallic iron present in commercially available iron sulphides. rather than from the action of the iron sulphide itself. NiS can replace copper in solution but it is not known to effect substantially complete precipitation of dissolved copper as sulphide; the exchange is only partial. In one account of the precipitation of trace concentrations of copper from nickel-bearing solutions under the action of NiS that is formed in situ by precipitation under the action of sodium sulphide. it is clear that a highly active sulphide is formed by special means and is only useful for precipitation of small concentrations of copper.  
  There are further references to precipitation of copper as sulphide under the action of metals, particularly iron, in the presence of elemental sulphur, a thermodynamically more effective method than the use of sulphides such as iron sulphide or nickel sulphide. Nickel metal can, like iron, effect precipitation of copper sulphide in the presence of elemental sulphur, but there is no reference, as far as is known to applicant, to precipitation of copper sulphide in the presence of elemental sulphur by nickel sulphide with an atomic ratio of nickel to sulphur greater than one, such as that present in some nickeliferous mattes.  
  Thus, the prior art appears to be silent on processes either for preferential chlorine leaching of certain metal values from others in mattes, sulphide concentrates or alloys suspended in chloride solutions, or for separation of copper from nickel in solution under the action of elemental sulphur and nickel sulphide with an atomic ratio of nickel to sulphur greater than one.  
  It has now been discovered that by controlling the redox potential of the leach solution at specific values one metal in the material can be leached to a greater extent than another metal therein, and means are provided according to the practice of this invention to effect such control and thereby achieve preferential leaching of a selected metal. The control means are based on the discovery that the redox potential can be controlled at will by controlling the feed rate of chlorine to the solution relative to the feed rate of material thereto. Thus according to this invention such control of feed rates is effected to establish redox potentials at which a selected metal in the material is leached preferentially with respect to other metals therein, thereby advantageously effecting a separation of one metal from others in the same material.  
  It is, therefore, an object of the present invention to overcome the disadvantages of the prior art and provide.a process for preferential chlorine leaching of a metal from others in mattes, sulphide concentrates, alloys and the like.  
  Another object of the invention is to provide a process for selectively leaching nickel from copper and of either or both of them from precious metals in the solid particles.  
  Yet another object is to provide an improved process for separating copper from nickel dissolved in solution.  
  Precious metals are referred to hereinafter as PMs and the term will be understood to refer collectively to metals selected from the group gold, and the six platinum group metals, namely platinum, palladium, rhodium, ruthenium, osmium and iridium.  
  Further reference herein to redox electrodes and to redox potentials will be understood to refer to a Ptsaturated calomel electrode pair unless stated otherwise.  
  By one aspect of the present invention there is provided a process for recovering metal from particulate sulphidic and metallic materials containing metals selected from the group comprising nickel, copper and precious metals, by chlorine leaching the material as an agitated slurry in a cuprous ion-bearing aqueous chloride solution, the redox potential of which increases upon feeding chlorine thereto and decreases upon feeding particulate material thereto, the improvement for leaching a metal preferentially with respect to other metals in the material comprising, (i) controlling the rate of feeding of chlorine relative to the rate of feeding of material to the solution such that the redox potential of the solution is controlled substantially at or below a selected potential at which the metal is leached preferentially with respect to other metals in the material, and (ii) leaching the metal from the material thereby producing a leach solution and a leach residue.  
  By another aspect there is provided a process for precipitating copper sulphide from nickeliferous solution containing dissolved copper comprising, (i) feeding nickel sulphide having an atomic ratio of nickel to sulphur greater than one to the nickeliferous solution and forming an agitated slurry thereof, (ii) reacting the nickel sulphide with dissolved copper in the solution in the presence of elemental sulphur, thereby precipitating copper sulphide and dissolving nickel in the nickeliferous solution, (iii) withdrawing copper sulphide and copper-depleted solution from the slurry, (iv) separating the copper sulphide from the copper-depleted solution, and (v) recovering nickel from the copperdepleted solution.  
  By yet another aspect there is provided a process for recovering nickel from particulate sulphidic and metallic materials containing metals selected from the group comprising nickel, copper and precious metals by chlorine leaching the material as an agitated first slurry in a cuprous ion-bearing aqueous chloride solution, the redox potential of which increases upon feeding chlorine thereto and decreases upon feeding particulate material thereto comprising, (i) controlling the rate of feeding of chlorine relative to the rate of feeding of material to the solution such that the redox potential of the solution is controlled substantially at or below a selected potential at which nickel is leached preferentially with respect to copper and precious metals in the material, (ii) leaching nickel from the material thereby producing a nickel leach solution and a leach residue, (iii) withdrawing nickel leach solution and leach residue from the first slurry and forming a second agitated slurry thereof, (iv) feeding particulate nickel sulphide having an atomic ratio of nickel to sulphur greater than one to the second slurry, (v) reacting the nickel sulphide with dissolved copper in the nickel leach solution in the presence of elemental sulphur, thereby precipitating copper sulphide and dissolving nickel in the nickel leach solution, (vi) withdrawing copper sulphide and copper-depleted solution from the second slurry, (vii) separating copper sulphide from the copperdepleted solution, and (viii) recovering nickel from the copper-depleted solution.  
  The invention will be more clearly understood by reference to the following drawings.  
  FIG. 1 is a schematic representation of a particular process embodying both parts of the present invention.  
  FIG. 2 is a generalized schematic representation of that part of the present invention relating to preferential chlorine leaching of metals from solide particles.  
  FIG. 3 is a schematic representation of that part of the present invention relating to precipitation of copper sulphide from nickeliferous solutions containing dissolved copper.  
  FIG. 4 is a graphical illustration of the effect of redox potential on the separation of nickel from copper by chlorine leaching of a particular nickel-copper matte according to this invention.  
 FIG. 5 is a graphical representation of the relationship between redox potential and dissolved copper concentration in chloride leach liquors in contact with particles of a particular nickel-copper matte. on a semilogarithmic scale.  
  FIG. 1 illustrates a particular embodiment of the present invention as it applies advantageously to recov ery of metal values from nickeliferous mattes containing copper and PMs. The process utilizes the continuous aspects of the invention in the form of preferential chlorine leaching of nickel from copper and PMs in the matte followed by precipitation of dissolved copper as copper sulphide from the nickel chloride leach solution.  
  The preferential nickel leach is carried out in a vessel. l0. equipped with a gas entry port 11. a gas exit port 12. solution and solids entry port 13, slurry exit port 14. a rotatable impeller. 15. and a pair of reference electrodes 16. In operation the vessel contains a slurry of matte particles and an aqueous chloride solution containing dissolved nickel and copper. The chloride ion concentration of the solution is sufficiently high that the copper exists in the cuprous state. largely as anionic chloride complex ions. Chlorine is fed to the leach vessel. preferably through the bottom and under the impeller to ensure effective contact and dispersion therein. Matte particles are fed to the vessel conveniently through its side and preferably near to the impeller to ensure effective distribution and suspension of the particles in the solution. Chlorine reacts rapidly and exothermically with the solution by oxidizing dissolved cuprous copper to the cupric state and simultaneously cupric ions are reduced to the cuprous state. also exothermically, by leaching metal from the particles. The ratio of cuprous and cupric copper in solution very largely determines the redox potential generated between the electrodes. conveniently but not necessarily a platinum-saturated calomel electrode pair.  
  The redox potential is monitored and the feed rate of chlorine is controlled relative to the feed rate of matte particles to establish a redox potential at which nickel is leached preferentially with respect to copper and PM&#39;s. That is to say the ratio of concentration of nickel to copper or PM&#39;s in the leached particles is less than the corresponding ratio in the original matte feed. This definition does not preclude some leaching of copper or PMs. although substantially no PM&#39;s are leached in practice. Some copper is leached. however. and the proportion increases with the redox potential. as will be discussed in more detail subsequently. For present purposes it is sufficient to describe a particular set of condition to illustrate the practice of the invention.  
  Thus for a particular nickeliferous matte it has been found that when the relative feed rates of matte and chlorine are controlled to maintain a redox potential of about 315 mv about 80% of the nickel is leached from the matte and only about of the copper. There is no detectable dissolution of PMs whatever. The amount of heat generated by the leaching operation is sufficient that the solution boils and steam is evolved through the off-gas exit port 12. The reaction of chlorine in the slurry is so efficient that chlorine concentrations in the off-gas are only a few parts per million at most. while leaching occurs at the maximum rate that can be achieved in an unpressurized vessel, and at substantially constant temperature. The boiling point of the solution varies with the concentration of dissolved chlorides, of course. but in a continuous system in which leach slurry is withdrawn from the vessel as solution and fresh matte are fed to it. leaching occurs under nearly steady-state conditions and the temperature of the slurry is therefore substantially invariant.  
  As metal sulphides in the matte are leached and metal is dissolved. the associated sulphide sulphur is transformed in the slurry to an elemental form. Leach slurry withdrawn from the vessel therefore consists of leach solution preferentially enriched in nickel, and particles of leach residue containing elemental sulphur. It is this slurry that is treated according to the precipitation or second aspect of this invention for separation of dissolved copper as sulphide from the leach solution by reacting the solution in the presence of elemental sulphur with nickel sulphide in which the atomic ratio of nickel to sulphur is greater than one, such as the Ni S- occurring in some nickeliferous mattes. The particular combination of the higher nickel sulphide with elemental sulphur is essential for the practice of this part of the invention.  
  The copper sulphide precipitation is carried out in a vessel. 17, equipped with a leach slurry entry port. 18, a nickeliferous matte entry port. 19, a copper precipitation slurry exit port. 20. a gas offtake port. 21. a rotatable impeller. 22, and advantageously an electrode pair. 23, for the measurement of redox potential. Nickel leach slurry containing elemental sulphur and particles of nickeliferous matte containing Ni S are both fed to the vessel through their respective entry ports and dissolved copper in this solution is precipitated in sulphide form. It has been found that a rela&#39; tionship exists between the redox potential in the slurry and the concentration of dissolved copper in solution. One particular example of the relationship is presented in FIG. 5, and demonstrates the remarkable sensitivity of dissolved copper concentration to redox potential. Thus at about 50 mv the copper concentration in solution is only about 0.02 g/l; whereas at 300 mv it is about 40.0 g/l. an increase of 2000 times with only a sixfold increase in redox potential. Thus the extent of the precipitation is advantageously controlled by monitoring the redox potential and controlling the relative feed rates of leach slurry and matte to maintain a redox potential at which a selected degree of precipitation is ef fected, preferably as close to as practicable. The potential is advantageously about 100 mv. The solution. while not necessarily boiling, is nevertheless at an elevated temperature, and water evaporated therefrom is withdrawn through the gas off-take port while reacted slurry is withdrawn through the copper precipitation slurry exit port. When the solution in the withdrawn slurry is substantially devoid of dissolved copper. the net effect of the combined practice of both parts of the invention is dissolution of a major portion of the nickel in the matte treated while retaining substantially all the copper and PMs in the solids.  
  Following the novel steps of this invention. the copper-free nickel chloride solution may be separated from the solids. advantageously by filtration. further treated for removal of other dissolved impurities such as iron. cobalt. lead. zinc and other minor metal constituents in the matte that might have dissolved.  
 thereby becoming a substantially pure nickel chloride solution. and finally electrolyzed for recovery of nickel therefrom by electrowinning in conventional manner. Chlorine is generated anodically and is usually recycled to the leaching operation, while the nickel-depleted chloride electrolyte may likewise be recirculated to the leaching operation. The matte and solution fed to the leach vessel may thus conveniently and advantageously be brought together in mixing vessel, 24, and fed to the leach operation as a slurry thereby closing the process circuit. The filtered solids can in turn be treated for recovery of the remaining nickel, copper and PMs by known methods.  
  Thus a process has been described for recovery of nickel, copper and PMs from matte that advantageously embodies both parts of the present invention for separation of nickel from copper and PMs, by preferential leaching of nickel followed by precipitation of dissolved copper from the nickel-enriched leach solution. While this embodiment illustrates the combined practice of both parts of the invention, each part may be practiced independently of the other, and each will be described separately and in more detail below.  
  FIG. 2 is a schematic representation of an apparatus in which the preferential chlorine leaching can be carried out. The apparatu illustrated consists of a closed vessel. 10, a Jnorine gas entry port, 11, solid particle and aqueous chloride solution entry port, 13, leach slurry exist port. 14, gas off-take port, 12, rotatable impeller. 15, and a pair of electrodes, 16, for the measurement of redox potential. While the positions of these items as illustrated are advantageous they are not necessarily critical. Thus, for example, the chlorine could enter the side rather than the bottom of the vessel so long as it enters directly into the solution. The redox electrodes could project downwards from the top of the vessel rather than through its side. The gas offtake could be from the side rather than the top of the vessel. The particles to be leached and the leach solution could be fed independently to the vessel through separate entry ports rather than as a slurry through one port as shown, and even as a slurry they could enter the vessel through the top rather than the side. Many variations, are thus possible always provided that the chlorine is fed to the vessel below the surface of the solution and the solids are suspended therein.  
  In starting up a continuous leaching operation an aqueous chloride leach solution containing dissolved copper in the cuprous state is supplied to the vessel and agitated. ln leaching nickeliferous materials, chlorine is fed first into the solution with which it reacts rapidly thereby oxidizing cuprous copper to the cupric state and generating heat. Since the redox potential is largely a measure of the cupric/cuprous ratio in the solution, the increase in this ratio by absorption of chlorine is manifested by an increase in the redox potential. Particles are then fed to the agitated solution and as they are leached the redox potential drops indicating a decrease in the cupric/cuprous ratio. Thus when both chlorine and particles are fed simultaneously to the leach slurry at such rates that the redox potential remains constant, it is clear that cupric ions are consumed by the leach reactions as fast as they are produced by the absorption of chlorine so that the cupric/cuprous ratio remains unchanged. If the potential rises it is clear that the cupric/cuprous ratio is higher which means either that the feed rate of chlorine is higher or the feed rate of particles is lower. Whichever the case there is a relative increase in the feed rate of chlorine with respect to that of particles. The effect of such an increase in the concentration of cupric ions is more leaching of the particles, the likely consequence of which is decreased selectively of the leach. Conversely, if the potential drops the availability of cupric ions is less, the consequence of which is less extensive but likely a more selective leach.  
  Which metals are leached from a given type of particle and to what extents at a particular redox potential is a matter of experience and experimentation. Once the leaching criteria have been established for a particular material by testwork, similar particles can be treated under similar conditions with reproducible and predictable results. Without wishing to be bound by this or any other theory, it is believed that metals leach at given potentials as a function of both the electrochemical properties of the metals themselves and their association in the particles. Generally speaking, it is believed that the least noble metals tend to leach most readily and will therefore dissolve under relatively mild leaching conditions, that is to say at relatively low concentrations of cupric ions or redox potential. Progressively more noble metals are leached as the potential rises and the availability of cupric ions is increased.  
  Attention is drawn to FIG. 1 of U.S. Pat. No. 2,835,569 wherein such a relationship is depicted. It is also believed, however, that a given metal will leach at a lower potential when present in metallic form that when present in the particles as a sulphide. Thus while it is likely that in particles containing nickel, copper and PMs the order of leaching in progressing from lower to higher potentials will be nickel-copper-PMs, it is equally likely that a more effective separation can be achieved between nickel and copper, for example, if the nickel is present in metallic form and the copper as a sulphide, than the other way around. The same considerations apply to selective leaching of copper from PMs in PM concentrates, and to the separation of one metal from another in alloy particles containing any combination of the above metals.  
  What is important to emphasize is that for a given type of particle the leach under given conditions is predictable, can be preferential for one or more metals with respect to others, and can be controlled according to the practice of this invention to achieve a particular predictable result.  
  Control of redox potential during leaching is achieved by controlling the relative feed rates of chlorine and particles to the leach slurry. While such control could be exercised in a variety of ways including crude manual adjustment of feed rates made from time to time in response to periodic measurement of potential, the most effective control is automatic and continuous. in continuous operation the feed rate of the solids is advantageously fixed. and the flow of chlorine continuously adjusted to maintain a set potential by an electrically operated valve in the chlorine line. The valve is connected to a potential-recording device and activated by an electrical signal from it in accordance with any difference between the actual and set potential. Thus if the actual potential rises above the set potential the flow of chlorine is automatically decreased and the potential drops. Conversely if the actual potential falls below the set potential the flow of chlorine is automatically increased and the potential rises. in this manner the actual potential fluctuates closely about the selected potential and the leach is controlled to provide predictable results.  
  While the present invention can be applied in general to the separation of one or more metals from other metals in sulphide or metallic form. it is of particular interest for the separation of nickel from copper or of either or both from PM&#39;s in mattes. sulphide concentrates and alloys. The invention may also be applied to the separation of individual PMs from one another.  
  It will be recognized that some mattes and concentrates. particularly those of nickel and copper. contain considerable concentrations of iron. and while the invention can be applied to the treatment of such materials. it is particularly well suited to the treatment of lowiron mattes and concentrates such as described herein. PM mattes and concentrates in general contain little iron and can be treated according to the present inven tion whether they originate directly from PM ores or from nickel and copper ores containing PMs from which the bulk of the nickel and copper have previously been recovered.  
  Other materials can also be treated including nickel matte substantially devoid of copper. In this case preferential leaching of nickel with respect to copper is. of course. not an object of the leach but the invention can still be applied advantageously to recovery of the nickel. Since no copper is present in the matte to supply the leach solution with copper ions for leaching. these can be supplied independently and the leach con ducted in the manner described at a convenient redox potential. The leach slurry can then be filtered. the solution treated for precipitation of copper. also according to this invention, by using nickel matte and added elemental sulphur. The copper sulphide precipitate can then be recycled to the leach. Thus the copper required for leaching is merely recycled between leaching and precipitation while the feed is a copper-free nickel matte and the product is a copper-free nickel chloride solution.  
  The leach solution can be any chloride solution containing dissolved copper in the cuprous state. Thus the chloride ion can be provided as hydrochloric acid or as a metal chloride such as nickel chloride, for example, or as a mixture of chlorides. It is important only that sufficient chloride ions be present to permit the presence of dissolved copper in the cuprous state. While HCl can be present in the leach solution it is not necessary and this is one of the major advantages of the present method over HCl leaching of sulphides. In the recovery of nickel from matte. for example. nickel can be selectively leached according to the present invention in a nickel chloride solution substantially devoid of HCl. to form a concentrated nickel chloride solution that can be electrolyzed directly for recovery of nickel by electro-winning without any prior costly neutralization of acid.  
  The temperature of the leach is advantageously the boiling temperature of the solution. Sufficient exothermic heat is generated by both the absorption of chlorine and the leach reactions to boil the solution. Not only is no additional heat required to effect boiling but heat may have to be removed from the solution by some cooling means to prevent the solution from boiling over. Boiling is an advantage. however. not only because reaction rates are a maximum under atmospheric conditions. but a convenient means of temperature control is automatically provided, and in addition a considerable contribution to the suspension of particles in the leach slurry is provided by the boiling action.  
  The leaching operation can be conducted in either batch or continuous mode. While continuous operation is preferred as discussed below. particularly for the treatment of large tonnages of nickel-copper matte. for example, batch or semi-continuous operation is quite appropriate for the relatively small quantities of some materials such as PM mattes or concentrates. Whether the leach is conducted in batch or continuous mode. however. the same method applies the feeding of chlorine and particles to the leach slurry is controlled to establish redox potentials at which a selected metal is leached preferentially to other metals.  
  ln continuous operation with chlorine and particles being fed continuously to the leach vessel and slurry being removed continuously therefrom. the redox potential is held substantially constant for consistency of results. while in batch operation the redox can vary throughout the leach so long as the redox at the end of the leach is at or below the preselected value. Thus batch leaching can be done with continuous feeding of chlorine, particles, and solution, as in continuous operation, until the vessel is full, or it can be done by supplying the particles either altogether near the beginning of the leach or from time to time during the leach and feeding chlorine until the redox potential has risen to the preselected value. Thus there can be. and generally are. periods during batch leaching operations when chlorine is fed to the solution while the feed rate of particles is zero. The converse can also occur but is less common.  
  Since the redox potential rises upon feeding of chlorine and falls upon feeding of particles. it will be understood that with irregular feeding of particles and continuous feeding of chlorine. it is possible for the redox potential to rise above the preselected value from time to time during a batch leach. Addition of further quantities of particles will cause a drop in the redox potential. however. and will tend to reprecipitate metal values that dissolved while the potential was above the preselected value. Thus, while such fluctuation of redox potential is not desirable and can be readily avoided merely by controlling the feeding of chlorine according to the redox potential. it is the final redox potential in a batch leach operation that must be at the preselected value if the predicted results of the leach are to be expected and achieved.  
  Thus. whether chlorine and particles are fed together at substantially constant rates or separately at varying rates. the relative feed rates of both are controlled to establish a preselected redox potential for the leach. With continuous operation the selected potential is continuously maintained whereas with batch operation it need only exist at the end of the leach and must be established anew in each batch.  
  Continuous operation is preferred because fluctuations in solution levels. concentrations. temperatures. specific gravities and other properties are minimized and there are no interrupted flows of solid, liquids. or gases. Materials are continuously fed to the system and removed therefrom while conditions within the vessel remain substantially steady. This fact is of particular advantage if the solution fed to the leach vessel contains no copper as in the case with the spent nickel chloride electrolyte described in relation to FIG. 1. ln  
 such a case it is clear that with batch operation copper would have to be supplied to each batch of starting solution whereas with continuous operation the leach is only started up once, after which a concentration of copper is retained in the leach solution by the leach itself unless, of course, there is no copper to be leached, as in the case of the copper-free nickel matte described above. In this latter case. of course, copper must be provided from another source, but otherwise the leach solution is not dependent on recirculated solution for copper.  
  While it is recognized that in theory chlorine leaching can be effected under the action of any redox couple including ferric-ferrous, manganic-manganous and oth ers, this discussion is limited to the use of the cupriccuprous couple because copper is more noble than nickel and can therefore be separated conveniently from nickel by precipitation according to this invention. Because copper is the leaching agent it must of course remain in solution for leaching to occur and this is the reason why. in starting up a leach of nickeliferous matte. for example, chlorine is fed to the solution before the matte particles. By this means the presence of cupric ions is ensured. When particles are fed before chlorine, cupric ions in solution are consumed immediately by leaching of nickel, for example. from the particles and the resulting cuprous chloride is in turn reduced and copper precipitated. When chlorine is then supplied to such a solution devoid of cuprous copper, it simply passes through the solution unabsorbed and no leaching occurs.  
  The particular redox potential that is maintained depends on both the type of particles being leached and the object of the leach. In the process of FIG. 1, for example, in which it is intended to leach nickel preferentially with respect to copper and PMs in a nickelcopper matte, FIG. 4 illustrates clearly the relationship between redox potential and leach selectivity for chlorine leaching of a particular nickel-copper matte. It can be seen that at a potential of about 315 mv about 85% of the nickel is leached but only about 15% of the copper. At lower potentials less metal is leached but a greater proportion of it is nickel. At 280 mv, for example, about 75% of the nickel is leached but only about 5% of the copper. At higher potentials the reverse is true; thus, at about 350 mv, for example, about 90% of the nickel is leached with about 40% of the copper. As the potential is allowed to rise, more and more nickel and copper are dissolved and the leach becomes progressively less selective for nickel with respect to copper. The upper limit for selectivity of nickel over cop per from the above matte is about 400 mv. In low copper mattes selectivity against copper is not a problem, and redox potentials can therefore be as high as about 500 mv or so before significant dissolution of PMs occurs. In the absence of PMs as well, potentials can go as high as 1,000 mv but substantially all dissolved copper is then in the cupric state and the solution therefrom has no capacity to absorb chlorine beyond that corresponding to the leach rate. Thus chlorine might begin to appear in the off-gases and in addition sulphation increases with redox potential, both features representing process inefficiencies. The lower practical limit of redox potential is about 250 mv. At potentials below about 250 mv there is not enough copper in solution to absorb sufficient chlorine and generate sufficient cupric ions to sustain sufficient leach rates and throughput. In summary, there is just not enough leaching agent available below about 250 mv to sustain an acceptable leaching operation. The redox limits quoted above and in FIG. 4 apply to a specific matte and could be different for another material. Particular limits are established by experiment and thereafter can be used for control purposes to achieve a predictable result in the treatment of a particular material. In the treatment of certain PM concentrates containing copper and only minor or negligible concentrations of nickel, separation of copper from PMs is effected by conducting the leach at potentials up to about 450 mv or so, under which conditions copper is substantially completely dissolved while PMs are retained and concentrated in the leach residue. The elemental sulphur resulting from the leaching of copper sulphide is removed from the leach residue conveniently by dissolution in a sulphur solvent such as trichloroethylene and the PMs are then recovered by leaching in aqua regia and precipitation by known methods.  
  FIG. 3 is a schematic representation of an apparatus in which the part of this invention relating to precipitation of dissolved copper from nickel-bearing solutions can be carried out. The apparatus as illustrated consists ofa closed vessel, equipped with entry port, 18, for elemental sulphur and nickel-bearing solution containing dissolved copper, entry port, 19, for nickel-sulphidebearing particles in which the atomic ratio of nickel to sulphur in the sulphide is greater than one, an exit port, 20, for slurry of copper sulphide and copper-depleted solution, a gas exist port, 21, a rotatable impeller, 22, and advantageously an electrode pair, 23, for the measurement of redox potential. As in the case of the apparatus of FIG. 2, the positions of the various items described for the present apparatus need not be as shown in FIG. 3. It is necessary only that means be provided to bring together as an agitated slurry, the solution. nickel sulphide and elemental sulphur, and to remove reacted slurry and water vapour from the vessel.  
  The solution can be any nickeliferous solution containing copper from which copper can be at least partially precipitated by prior art methods as described above. Concern is largely with the treatment of chloride and sulphate solutions, and particularly with chloride solutions of such chloride ion concentration that dissolved copper is present in the cuprous state, such as solutions resulting from the chlorine leaching of nickeliferous mattes. Nickel sulphide with an atomic ratio of nickel to sulphur greater than one is conveniently supplied in the form of nickeliferous matte containing Ni S- as in the process indicated in FIG. 1. Elemental sulphur can be provided in any convenient form. In a process such as that indicated in FIG. I, for example, the sulphur is conveniently provided by supplying to the precipitation vessel the sulphur-bearing leach residue resulting from chlorine leaching of a matte. In the absence of such a sulphur-bearing material, however, sulphur in some other form may be used. such as, for example, sulphur flowers.  
  To effect the precipitation of dissolved copper from nickeliferous solutions according to this invention, the solution, nickel sulphide, and elemental sulphur are brought together as an agitated slurry and copper is precipitated as copper sulphide. The temperature is not critical but the higher it is, of course, the faster is the rate of precipitation. Reacted slurry is removed from the vessel and filtered, thereby separating a copper sulphide precipitate, and a copper-depleted nickeliferous solution. Any portion of the dissolved copper can be precipitated but the principal advantage of this invention is that substantially all the copper can be precipitated from solution. This is of particular advantage in the treatment of chloride solutions of high chloride ion concentration in which copper is dissolved in the cuprous state, and from which complete precipitation of copper in metallic form cannot be accomplished.  
  The extent of copper precipitation can be effectively&#39; controlled by control of the redox potential of the solution. It has been discovered that the redox potential of a solution in contact with solid sulphides is a measure not only of the cupric/cuprous ratio but also of the absolute concentration of dissolved copper. The lower the redox potential. the lower the cupric/cuprous ratio and the lower the total concentration of dissolved copper. Thus if the feed rate of solution to the vessel is increased relative to that of nickel sulphide and elemental sulphur. copper concentration in solution will rise and so. therefore, will the redox potential. Conversely, if the feed rates of nickel sulphide and elemental sulphur are increased relative to that of solution, the copper concentration in solution will fall and so will the redox potential.  
  By monitoring the actual redox potential and adjusting the relative feed rates of solution. nickel sulphide and elemental sulphur with respect thereto to maintain a preselected potential. the extent of copper precipitation and the resulting copper concentration of the solution are controlled at will. In the treatment of a nickel chloride solution containing about 40 g/l of dissolved copper. for example. it was found that when nickeliferous matte containing Ni S was supplied for precipitation and the relative feed rates were controlled to maintain the redox potential at about 100 mv. the residual copper concentration in solution was a maximum of about 0.2 g/l and in some cases was as low as about 0.020 g/l. thereby indicating precipitation of at least about 99.5% of the copper. When the feed rate of matte was decreased. however. such that the redox potential was increased to about 250 mv. the residual copper concentration of the solution was about g/l. thereby indicating precipitation of only about 75% of the copper. Conversely when the feed rate of matte was increased to produce a redox reading of about 50 mv. the copper was substantially completely precipitated to a residual copper concentration in solution of at most about 0.050 g/l and as low as about 0.010 g/l. This rela tionship between redox potential and concentration of dissolved copper is more clearly illustrated in Table 9 and in FIG. 5.  
  Redox control is of particular advantage when applying the invention to the substantially complete precipitation of copper because oversupply of reagents is avoided. When more nickelsulphide is fed to the solution than is needed to precipitate the dissolved copper to a selected residual copper concentration. for example. the redox reading falls and the supply of nickel sulphide is automatically cut back by similar control means to those described above in relation to FIG. 2. Thus. the minimum amount of nickel sulphide is used and consequently the minimum amount of residual nickel remains in the copper sulphide precipitate.  
  The mechanism of the precipitation is not definitely known, but because precipitation of copper by nickel sulphide with an atomic ratio of nickel to sulphur greater than one is not effected in the absence of elemental sulphur, the reaction mechanism for precipitation of cuprous sulphide from high chloride solution by Nigsg and elemental sulphur is believed to be:  
 S 2 CU 3 CD 5 3 According to this mechanism the precipitation occurs by the continuous generation and consumption of 5* ions. the net effect of which is:  
 w s. 2 (311 s s 2 NiS Ni c11 5 (3) NiS 2 Cu S CUgS Ni In the absence of elemental sulphur. precipitation of copper by Ni S occurs presumably according to some reaction such as:  
 Nigsg 2 Cu* S 2 NiS Ni 2 Cu It is a matter of record, however. that no significant precipitation of copper does occur by Ni S- in the absence of sulphur and it appears. therefore. that the equilibrium concentration of copper metal in reaction (5) is negligible. The additi&#39;onal thermodynamic drive to form copper sulphide in the presence of elemental sulphur as in reaction (3) is apparently necessary to effect precipitation of copper by Ni S In using a nickeliferous matte containing Ni S as a precipitant for copper according to this invention. it has been found that some copper is precipitated in the absence of elemental sulphur, but this precipitation is attributed to the effect of metallic nickel also present in the matte rather than to an effect of Ni S according to a reaction such as (5) above.  
  While M 8 is apparently effective in precipitating copper as sulphide only in the presence of elemental sulphur. the overriding advantage of Ni S is that by its use substantially all dissolved copper can be precipitated whereas only partial precipitation can be effected by exchange with NiS or by cementation with metallic nickel. The advantage of M 5 is particularly significant in the treatment of high-chloride solutions in which dissolved copper is present in the cuprous state because in such solutions metallic nickel can reduce copper in solution to only about 2 grams per litre. Even when the solution is diluted to decompose cuprous complexes to cupric ions. metallic nickel is not as effective in precipitating copper metal as is Ni S together with elemental sulphur in precipitating copper sulphide.  
  Thus a method and a possible mechanism therefor has been described for precipitation of copper as sulphide from nickel-bearing solutions by the combined action of elemental sulphur and nickel sulphide with an atomic ratio of nickel to sulphur greater than one. Such nickel sulphide is conveniently available in nickeliferous matte in which nickel is present as M 5 The notable advantage of the method is its capacity for substantially complete precipitation of copper from chloride and sulphate solutions and particularly chloride solutions of high chloride ion concentration in which dissolved copper is present in the cuprous state such as solutions resulting from the chlorine leaching of nickeliferous mattes. I  
  It will be understood that while both parts of the present invention can be combined advantageously in the practice of a process such as that described in relation to FIG. 1, both parts can also be practised independently. Thus the chlorine leaching part can be applied. for example, to separation of copper from PMs in sulphidic or metallic materials that contain&#39;little if any nickel, and to which the precipitation part of the invention therefore has no relevance. Conversely the copper sulphide precipitation part can be applied, for example, to precipitation of copper from nickeliferous sulphate solutions that clearly do not derive from the practice of the chlorine leaching part of this invention. The following examples illustrate specific practices of each part of the invention independently and of both parts combined.  
 Cu Ni Fe 5 PM&#39;s A series of chlorine leach tests was performed to illustrate the effect of redox potential on dissolution of copper and PMs from this material. In each test 100 g of the leach residue were treated in one litre of leach solution analyzing in g/l:  
 Ni NCI Chlorine was fed to the slurry at a rate of 70 ml/min s and the temperature was controlled at 100C. The  
 TABLE l PERCENTAGE OF METALS LEACHED VERSUS FINAL REDOX POTENTIAL EXAMPLE 1 The independent practice of the leaching part of this invention is advantageously applied to selective chlorine leaching of copper from PM concentrates and mattes. Such materials may derive from a variety of sources notably PM ores and nickel and copper ores containing PMs. From PM ores a PM concentrate or matte may be recovered directly whereas from nickel and copper ores it is recovered indirectly following prior recovery of the bulk of the nickel and copper. In the case of nickel ores in which the last stage of nickel recovery is electrorefining of soluble nickel anodes, for example, the anode slimes constitute a PM concentrate. Whatever the source of the PM concentrate or matte, the bulk of any nickel therein is advantageously recovered prior to application of the present invention for separation of copper and PMs. A PM matte result ing from treatment of a PM ore containing nickel and copper had the following analysis in Wt7rt Ni Cu Fe 5 PM s The figure for, P&#39;Ms is the total of Au Pt Pd Rh Ru lr. The nickel was first recovered by preferential leaching in HCl solutions according to the method described in US. Pat. No. 3,085,054, and the resulting leach residue had the following analysis in wt%:  
  These data indicate clearly that although substantially all the copper was dissolved at 480 mv, there was substantially no dissolution of PM&#39;s at 515 mv. Thus, copper and PMs can be almost totally separated by maintaining the redox potential at about 500 mv (equivalent to about 450 mv using Pt-saturated calomel electrodes).  
 EXAMPLE 2 In the recovery of PMs from nickel anode slimes, the slimes were first smelted with iron suphide and borax to slag off silica and other gangue constituents. The resulting PM matte had the following composition in Wt%2 Precious Metals Cu Ni Fe 3 sio Au Pt 53.5 7.2 4.0 20.5 l.() 0.21 0.44  
  Rh Ru lr Total 0.20 (H3 ().l L5? TABLE 2 PERCENTAGE DISSOLUTION OF BASE METALS AND PMS VERSUS FINAL REDOX POTENTIAL The data show that while practically all of the copper in the matte was dissolved, substantially no dissolution of PM&#39;s occurred. They were concentrated in the leach TABLE 3 Continued CONCENTRATIONS OF (&#34;OPPER IN SOLUTION VERSUS REDOX POTENTIAL residue as a higher grade PM concentrate with the fol- Concenlmlio&#34; Dissolved g/l lowing Composition in zy 15 Potential (u Cu&#39; Total (u Ratio 420 70 l8.0 25.0 2.0 Preclous Metals 430 85 231) 3 15 2&#39;7 440 1 1.0 29.0 40.0 2.6 (u Ni Fe S SiO Au Pt Pd Rh Ru lr Total 450 17 360 53o 11 3.5 3.0 0,3 85 0.0 0.8 2.0 2.l 0.9 (L 0.3 0.0 4 0 5H) 75 g5 13 30 470 47.0 84.0 l3 1.0 1.8 4x0 300 95.5 131.5 2.7  
  The concentrate was largely sulphur, a major portion of which was in elemental form and removable in a va- 510 10 1331 5.6 rietyof ways including roasting at low temperatures. if: sublimation in a stream of nitrogen. reaction with hy- 540 7.0 124.0 131.0 17.7 drogen to H5. dissolution in carbon disulphide or sodium sulphide. reaction with sodium sulphite to sodium thiosulphate, and extraction with trichloroethylene.  
  As a result of sulphur removal. the PM s were further upgraded in the remaining solids from which they could The data indicate that leaching of PP from the be leached in aqua regia and eparately recovered slimes was substantially complete at 470 mv 215 the total therefrom by known methods In fact a particular ad- CU in solution did not increase beyond I31 g/I CU. The vantage of the application of this invention to the treat- Concentration of uhivaleht Copper reached a maximum ment of sulphidic PM concentrates and rnuttes is that Llt 460 mv and thereafter the effect Of continued ChIO- all the PMS are present in a form soluble in aqua regia 35 rine addition W215 apparentlymerely t0 oxidize cuprous from which they can be readily and separately recovpp r to h pri state. Th cupric-cuprous ratios ered. ln existing processes for recovery f PM f are given the righthand column of the table and as it is such materials only gold, platinum and palladium are known from the Previous examples that In Such di fl l bl i aqua regia Th other l i materials do not dissolve substantially below about 515 group metals are rendered insoluble in aqua regla and mv, It IS concluded that while dissolution Of copper IS must be additionally treated before they can be sepa- Substantially Completed at a Cu /CU ratio less than rately recovered. PMs do not dissolve significantly at a ratio less than about 6 or 7. EXAMPLE 3 Another method of concentrating the PMs in nickel EXAMPLE 4 anode slimes is to smelt the slimes, cast what is gener- The PM-bearing materials in the previous examples ally referred to as a PM anode, and electrolyze the were sulphidic concentrates and mattes. It is instructive anode to recover nickel and thereby produce an upto record the outcome of chlorine leaching on similar graded PM concentrate referred to as PM anode materials after reduction to the metallic state. A PM slimes. A sample of such slimes was chlorine-leached in so anode slime similar to that referred to in Example 3 was a manner similar to the procedures described in the roasted at 750C to remove sulphur and then reduced previous examples. and the solution was analyzed for in hydrogen at 500C to produce a metallic material both univalent and divalent copper at various redox powith the following composition in wt%.  
 Cu Ni Fe S Au Pt Pd Rh Ru Ir tentials as measured between Pt-saturated Ag/AgCl The leach solution contained 20 g/l Ni and 12 g/l Cu electrodes. The results are tabulated below: initially and the temperature was maintained at 100C. TABLE 3 The feed rates of chlorine and solids were controlled to CONCENTRATONS OF COPPER IN SOLUTION VERSUS maintain a redox potential of 400 mv. (Pt-saturated REDOX POTENTIAL Ag/AgCl) until 500 g of sample had been added, after I Diswh&#39;ed CUM/91+ which the potential rose as feeding of chlorine was conf ll Cm Cw Tom] tinued. Samples of slurry were taken at 450. 475 and 400 M) mu 6&#39;0 L7 500 mv and the percentage dissolutions of the different 410 6.5 14.0 20.5 2.2 metals at these potentials are tabulated below.  
 TABLE 4 PERCENTAGE OF METALS LEACHED VERSUS REDOX POTENTIAL Comparison of these data with those in Table 2 reveals that while dissolutions of Au. Pt and Pd were little different in the reduced than in the sulphidic material. the dissolutions of Rh. Ru and Ir in the reduced material were over 8% at 500 mv whereas in the sulphidic material they were only a few tenths of a percent even at 525 mv. This test emphasized the preferred separation of base metals from PMs in sulphidic materials and the importance of the form in which the Pms are present in the concentrate on their behaviour in the chlorine leach.  
  The four examples above indicate the variety of PM- bearing materials to which this invention can be applied for preferential chlorine leaching of copper and the simultaneous concentration of PMs in the leach residue from which they can be recovered. after removal of sulphur. by dissolution in aqua regia and precipitation therefrom. For the sake of completeness it is pointed out that while silver was present in the materials treated. it is not included in reference to PMs because it dissolves to a large extent along with copper and is recovered from solution by cementation.  
 EXAMPLE The independent practice of the copper precipitation part of this invention is illustrated by its application to the separation of dissolved copper from nickel in sulphate solutions. Solution that contained 105 g/l Ni and 40 g/l Cu was treated in three pairs of tests using 150 or 100 gm of a coarse or a fine matte containing Ni S and metallic Ni having a size distribution of:  
 Tyler Screen It is clear that much more copper was precipitated in the presence than in the absence of elemental sulphur. The mattes had the following compositions in wt%:  
 Matte Type Ni Cu 5 Coarse 43.7 31.6 2L9 Fine 50.0 23.1 23.3  
 The balance of the mattes was comprised of iron. cobalt. oxygen and gangue constituents such as silica, alumina and lime. It is well known that the copper and nickel in such low-iron. high-sulphur mattes are present as Cu S. Ni S- and a Ni-Cu alloy containing about 80% Ni. The division of nickel in the matte between Ni S and the alloy phase can be estimated conveniently on the basis that all copper is present as Cu S. the balance of the sulphur is present as Ni S and the balance of the Ni is present as alloy. As some of the Cu is present as alloy, however. and some of the iron and cobalt are present as sulphide. the basis for the calculation is. of course, not strictly correct, but as the concentration of alloy is relatively small. the amounts of copper. iron. cobalt and sulphur involved are also small and the division of nickel between sulphide and alloy form as indicated by this estimate is therefore relatively accurate. Thus the amounts of nickel in each run that were present in the matte in sulphidic and metallic form were calculated on the above basis and are tabulated below in Table 6 together with the amounts of copper precipitated. and the equivalent amounts of nickel.  
 - Material +80 80 +325 325 TAB E 6 P PRECIPITATION OF COPPER BY M 8 and METALLIC NICKEL Fme NW Run Nickel in Matte. g Cu Precipitated. g  
 No. As Ni;,S As Alloy Cu Ni Equivalent One test in each pair was made in the absence of eleg mental sulphur and the other with 30 g sulphur flowers. 3 38.5 5.2 3.0 2.8 For each test the solids were added to one litre of the l solution and agitated at 100C for 2 hours. Operating a 48.1 1.9 26.5 24.5 details are tabulated below together with the copper analyses and weights of copper precipitated.  
 TABLE 5 REAGENT WEIGHTS AND SOLUTION ANALYSES As the amount of nickel stoichiometrically equivalent to the copper precipitated in the even-numbered runs with elemental sulphur far exceeded the amount of nickel available in metallic form. it is clear that the bulk of the copper was precipitated by Ni S- and elemental sulphur as copper sulphide. thereby substantiating the aforementioned theoretical basis of the present invention. If it is assumed that in Runs 2. 4 and 6 all the nickel present in metallic form was dissolved in precipitating part of the dissolved copper. then the proportion of nickel present in the matte as Ni S- that was equivalent to the balance of the precipitated copper in each case is shown in Table 7 below.  
 TABLE 7 fed into the leach slurry through the bottom of the tank at a rate controlled continuously and automatically to PROPORTION OF Ni AVAILABLE AS Ni S FOR Cu PRECIPITATION AND DISSOLVED THEREBY EXAMPLE 6 The combined practice of both parts of this invention may advantageously be applied to preferential chlorine leaching of nickel from mattes. sulphide concentrates and alloys containing copper and/or precious metals maintain a redox potential in the solution of 350 mv. Agitation of the slurry was effected by both an impeller and the boiling action of the solution, while the temperature of the slurry remained substantially constant at the boiling point of about I 12C. Steam was removed from the top of the tank and sampled from time to time for C1 analysis. The displacement rate of leached slurry was equivalent to I43 litres/hr of nickel-enriched solution and 32 kg/hr of leach residue. Samples of the leached slurry were filtered and the Solution and residue analyzed with the following results:  
 followed by separation of dissolved copper and nickel by precipitation of the copper as sulphide. A nickeliferous matte containing both copper and PMs that was treated according to this invention had the following analysis in wt Ni Cu PMs The matte was ground and fed to a system similar to that described earlier in reference to FIG. 1. The particle size distribution of the matte feed is given below in wt -35 80 l50 +35 +80 +l50 +325 -325 (Tyler mesh).  
 Calculations of the weights of nickel and copper fed to the leach in matte compared to the corresponding weights leaving the leach in residue indicate that of the nickel was leached but only 41.5% of the copper. Cobalt and iron were also leached but PMs remained undissolved. As the chlorine concentration of the steam was characteristically only about 10 ppm. the overall chlorine input rate was readily calculated from solution analysis to be about 34.5 kg/hr. At 350 mv only about 1% of the dissolved copper or less than 0.5 g/l was present in the cupric state and thus nearly 50 g/l of cuprous copper were continuously available for the efficient absorption of chlorine.  
  The leached slurry was next subjected to a simple but advantageous extension of the process described above in relation to FIG. 1. Rather than being fed directly to the copper precipitation tank it was instead passed through an intermediate holding tank in which it was merely agitated. The retention time was similar to that of the chlorine leaching operation, that is to say about two and one half hours. Since no chlorine was fed to the slurry in the holding tank the temperature was lower. at about l06C. than that during chlorine leaching. The redox potential was also lower, at about 320 mv. suggesting. as was confirmed by analysis. that the copper concentration in solution was decreased. At the same time there was a corresponding increase in dissolved nickel as shown by the analysis. in the tabulation below, of the solution and solids of the exchanged slurry leaving the holding tank compared to those tabulated above for the leached slurry:  
 Thus about 9 g/l of copper were precipitated while about g/l of nickel were dissolved thereby achieving additional leaching of nickel without any additional consumption of chlorine and simultaneously effecting partial precipitation of copper. The amounts of copper and nickel exchanged in the holding tank suggest that undissolved NiS in the leach residue reacted with disevery case substantially all dissolved copper was subsequently precipitated under the action of additional matte containing N1 5. in the presence of the elemental sulphur generated during leaching. As all the copper in the matte reported in the final&#39;solids, the copper was a convenient titre for calculation of the overall proportion of nickel dissolved, as shown in the following tabusolved cuprous copper according to reaction (4) lation:  
 TABLE 8 REDOX POTENTIAL OF CHLORlNE LEACH VERSUS OVERALL Ni DISSOLUTION Redox Ni/Cu ratio Matte Ni/Cu ratio Potential in CI. Leach Added Matte Solids Diff. Overall of (1. Solution for Cu Before after &#34;/2 Ni Leach. m\&#39; Precipi- Leach Precipi- A Dissolved tation tation position as that given above was fed to the precipitation slurry at a rate controlled to maintain a redox potential of 100 mv. which amounted to 13.0 kg/hr. The temperature of the slurry was about 104C and retention time was again about 2.5 hrs. Precipitated slurry was displaced from the tank at a rate equivalent to 143 litres/hr of solution and 50.6 kg/hr of solids with the following compositions:  
  The effect of increasing redox potential on decreasing the selectivity of the leach for nickel with respect to copper is reflected by the steadily decreasing Ni/Cu ratios in the leach solution with rising redox. Similarly the increasing dissolution of copper with increasing redox is reflected by the increasing amount of matte required for copper precipitation with increasing redox potential of the leach. It will be noted that the overall proportion of nickel dissolved remained relatively constant at close to about 80% regardless of leach redox. Thus the increased proportion of nickel leached initially at increased redox was offset by the increased proportion of undissolved nickel in the larger quantities of matte that had to be provided to precipitate the increased quantities of copper dissolved at the higher Thus substantially all the dissolved copper was precipitated. only 20 mg/l or about 0.05% remaining in solution. If it is assumed that all metallic nickel in the matte was consumed in the precipitation operation, then calculation shows that about of the nickel present as Ni -,S- in the matte was also consumed together with elemental sulphur.  
  As some of the nickel in the added matte remained undissolved, the overall net dissolution of nickel was calculated to be just over 80% but this was present in a substantially neutral chloride solution at a high concentration (over 230 g/l Ni) that was substantially free of dissolved copper. After further purification of the solution to remove the remaining impurities the solution was fed to an electrowinning operation for recovery of cathode nickel. The chlorine generated at the anode and the spent electrolyte were both returned to the leaching operation thereby closing the process circuit.  
 EXAMPLE 7 Matte of a similar composition to that of Example 6 was leached in the same equipment at similar solids and solution flowrates but at various redox potentials. In  
 redox potentials. Nevertheless the fact remains that about of the nickel in a nickel-copper matte was dissolved according to this invention in a substantially copper-free neutral chloride solution at a concentration of about 250 g/l Ni that was subsequently treated for recovery of nickel by electrowinning without neutralization of acid as is required in most existing leach processes.  
 EXAMPLE 8 While the copper precipitation operation was advantageously conducted at about mv to ensure residual copper in solution was below about 200 mg/l, the effect of redox on residual copper was demonstrated by the results of a series of runs in which the redox was maintained at different values between about 30 and 300 mv. The operating data for the chlorine leach and exchange operations preceding the copper precipitation are reported separately to avoid confusion. Because the conditions of these operations varied considerably, the variation in residual copper at a particular value of precipitation redox could not be definitely ascribed to any one condition.  
 TABLE 9 TABLE 10 EFFECT OF REDOX POTENTIAL ON COPPER PRECIPITATION PRECIPITATION COPPER FROM CHLORIDE SOLUTION Re Pmemlill of Leach 335 T 330 Run Coarse Matte Sulphur Copper in Solution. g/l Matte Feed rate to Cl. Leach 74.5 107.5 kg/hr No g g Initial Final Precipitated Solution feed rate to Cl. Leach 100 260 litres/hr Temperature of Cl Leach l07.5 1 115C Redox Potential of Ni-Cu Exchange 285 310 mv 6 ,2 Temperature of Ni-Cu Exchange 98 l09C i T Q 1,  
  Redox of Matte to Temp. of Residual Cu Precipitation. Precipitation. Precipitation in Solution mv kg/hr C g/ 10 As with the sulphate solutions discussed in Example 30 2L9 73 (mm 5, 1t Isagain clear that much more copper was precipi- 50 73 (I038 tated 1n the presence than 1n the absence of elemental 70 19.0 73 11-053 sulphur. 70 18.2 73 0.013 90 m7 73 M63 The weights of nickel available in the matte as N1 5 l5 and as alloy are tabulated below together with the 150 I73 69 weights of copper precipitated and the nickel equiva- 170 14.3 70 1.9 lent. 190 l 1.3 70 3.7 210 13.1 71 12.7 TABLE 11 240 2.9 70 19.] 290 0,0 624 25 7 Run Nickel in Matte. g Cu Precipitated. g  
 No As Nigsg As Alloy Cu Ni Equivalent II 27.0 3.6 4.8 2.2 1&#39;. 18.3 2.5 26.3 I23 13 30.8 4.2 36.0 16.7 The figures 1n Table 9 appear in graphic form 1n FIG. 25 5 and while there is clearly a spread in copper concentration values at any given redox. the trend to lower As in Example 5. the conclusion drawn from the data copper values at lower redox is striking. Thus while the is that without sulphur the small amount of copper premaximum redox of 290 mv is less than 10 times the cipitated was probably cemented by metallic nickel in minimum value of mv, the maximum residual cop- 30 the matte whereas the amount of metallic nickel availper concentration of 25.7 gpl is nearly 2.000 times able was nowhere near enough to account for all the greater than the minimum value of 0.0l3 gpl. With copper precipitated in the presence of sulphur. Assumsuch sensitivity to redox. the variation in residual coping all the metallic nickel was consumed in Runs 12 and per at a given redox as shown is not surprising. Clearly l3, the proportion of nickel present as Ni S that must the degree of copper precipitation can be controlled have been n m n pr p ating opp r was alcuaccording to the practice of this invention merely by lated as shown below:  
 TABLE 12 Run Cu Precipitated. g Ni Metal therefore Ni Ni therefore Ni No. Cu Ni Equir. Consumed. Reqd Present as NLISQ g as as Consumed.  
  .iS- M 5 &#34;/1 maintaining the redox potential at the value corre- These efficiencies are similar to those in Example 5 sponding to a selected residual copper concentration in for sulphate solutions and support the hypothesis that solution. This is achieved by controlling the feed rate precipitation occurs according to both reactions (3) of matte relative to that of solution and sulphur. As and (4) referred to above.Whether or not precipitation shown in the tabulation above the redox was increased actually occurs according to these reactions. the surfrom less than 50 mv to more than 260 mv by decreasprising fact remains that copper is precipitated under ing the matte feed rate from more than 20 kg/hr to nil the action of Ni S in the presence of elemental suland thereby increasing the residual copper concentraphur, advantageously Ni S- present in nickeliferous tion in solution from less than 0.02 g/l to more than 20 matte. g/l, A I claim:  
  1. In a process for recovering metal from solid particles selected from sulphides and alloys and containing at least two metals selected from nickel, copper and EXAMPLE 9 precious metals. by chlorine leaching the particles as an Tests were performed to illustrate the effect of vari agitated slurry in a cuprous ion-bearing aqueous chloous quantities of coarse matte (as in Example 5) and ride solution, the redox potential of which increases elemental sulphur on the precipitation of dissolved upon feeding chlorine thereto and decreases upon copper in chloride solution resulting from chlorine feeding the particles thereto, the improvement for leaching of nickelifcrous matte. The solution contained leaching at least one metal preferentially with respect 235 g/l nickel and 38.3 g/l copper. Various amounts of to more noble metal in the particles comprising:  
 matte and sulphur were added to one litre quantities of i. controlling the rate of feeding of chlorine relative the solution and the slurries agitated for 2 hours at the to the rate of feeding of particles to the solution boiling point of about 1 10C. Representative operating such that the redox potential of the solution is conand analytical data are reported below: trolled substantially at a selected potential in the range between 250 mv and 550 mv at which at least one metal is leached preferentially with respect to said more noble metal in the particles. and.  
 ii. producing a leach solution containing at least one metal and a leach residue containing said more. noble metal.  
 2. Process according to claim 1 for leaching in continuous mode comprising,  
 i. withdrawing leach solution and leach residue from the agitated slurry as particles. chlorine and solution are fed to the slurry, and  
 ii. controlling the relative feed rates of chlorine and particles such that the redox potential is continuously maintained substantially at the selected potential.  
 3. Process according to claim 1 for leaching in a batch mode comprising.  
 i. controlling the relative feed rates of chlorine and particles such that the redox potential is below the selected potential when feeding of particles is completed. and ii. continuing to feed chlorine until the redox poten- LII tial has risen to the selected potential.  
  4. Process according to claim 2 in which the selected redox potential is within the range 250 mv to 450 mv and nickel is leached preferentially with respect to copper and precious metals in nickeliferous matte.  
  5. Process according to claim 3 in which copper is leached preferentially with respect to precious metals in particles selected from precious metal-bearing mattes and concentrates.  
  6. Process according to claim 1 comprising leaching nickel from substantially copper-free nickel matte and further comprising,  
 iii. separating leach solution from leach residue,  
 iv. precipitating and separating copper from the leach solution. and  
 v. recovering nickelfrom the leach solution.  
  7. Process according to claim 6 comprising dissolving the copper precipitate and returning the dissolved copper for leaching further quantities of copper-free nickel matte