METHOD FOR PROCESSING COPPER AND NICKEL SULFIDE MATERIALS

Abstract

A method of processing copper and nickel sulfide materials, including oxidizing torrefaction of a material to obtain cinder, leaching the cinder with a cycling solution, separating a leaching residue, and electro-extraction of copper from a leaching solution. The cinder and particulates generated by the torrefaction are separately leached. The particulates are leached in a cycling copper raffinate together with a separated portion of solution from a cinder processing line, the separated portion consisting of a portion of solution provided to the leaching after electro-extraction of copper. Particulates leaching residue is separated. Copper is extracted by solvent extraction from a particulates leaching solution, followed by separate electro-extraction of copper from a circulating re-extract. Then, a portion of the raffinate is separated to be forwarded to a nickel production process.

Claims

1. A method of processing copper and nickel sulfide materials, the method comprising: oxidizing torrefaction of a material to obtain cinder and particulates, leaching the cinder with a cycling solution, separating a leaching residue, electro-extraction of copper from a leaching solution, wherein the cinder and particulates generated by the torrefaction are separately leached, wherein the particulates are leached in a cycling copper raffinate together with a separated portion of solution from a cinder processing line, the separated portion including a portion of solution provided to the leaching after electro-extraction of copper; separating a residue from particulate leaching, extracting copper from a solution from particulate leaching by solvent extraction, followed with a separate electro-extraction of copper from a circulating re-extract, then separating a portion of the raffinate to be sent to a nickel production process.

2. The method of claim 1, wherein a master solution from crystallization of a portion of solution from cinder leaching is used as the separated portion of solution from the cinder processing line.

3. The method of claim 1, wherein copper concentrate from flotation separation of converter matte, or nickel containing copper matte, is used as the material of the copper and nickel sulfide materials to be processed.

4. The method of claim 1, wherein white matte is used as the material of the copper and nickel sulfide materials to be processed.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Simplified schematic process diagrams of sulfide material processing are provided in FIGS. 1 and 2, in which:

[0027] FIG. 1 shows a simplified schematic process diagram of an embodiment of the inventive sulfide material processing; and

[0028] FIG. 2 shows a simplified schematic process diagram of an optimal embodiment of the inventive sulfide material processing.

DETAILED DESCRIPTION

[0029] Implementation of the Inventive Method.

[0030] Implementation of the inventive method for processing copper concentrate from flotation separation of converter matte as the initial material is described. In the same manner, the method may be implemented for nickel containing copper matte, in particular, white matte.

[0031] Copper concentrate from flotation separation of converter matte is torrefied in a fluidized layer (FL) furnace at a boiling material layer temperature of 870°−930° C. until the sulfur residue in the cinder is about 0.1%. After filtering out particulates, torrefaction gases are forwarded into a sulfur acid production process. Torrefaction results in cinder and fine particulates enriched up to 2.0% sulfur. Fine particulates output is 15.5% of cinder output.

[0032] A simplified schematic process diagram of an embodiment of the inventive processing is illustrated in FIG. 1. Two copper production lines are involved in the method: electro-extraction 1 from cinder and electro-extraction 2 from particulates.

[0033] The cinder is leached in a circulating solution of the cinder processing line, i.e., solution after copper electro-extraction 1. Residue from cinder leaching is condensed and forwarded to water flushing and flotation together with residue from particulates leaching. After postfiltration, cinder leaching solution is sent to copper electro-extraction 1. Baths are supplied with electrolyte which is obtained by homogenization of postfiltration filter liquid and electrolyte which is recovered from the baths. Marketable copper is produced in baths with lead-based alloy anodes. Part of acid electrolyte recovered from the baths is mixed with postfiltration filter liquid, part is returned into cinder leaching, and part is separated for particulates leaching.

[0034] Particulates from torrefaction are leached in a portion of copper extraction raffinate together with a separated portion of electrolyte from copper electro-extraction 1. Residue from particulates leaching is condensed and forwarded to water flushing and flotation together with the residue from cinder leaching. Postfiltration filter liquid from the particulates leaching solution is forwarded to copper extraction by solvent extraction. The extraction is carried out using a modified oxyoxime based extractant (Acorga M5640 produced by Cytec InD, or its equivalent) with 30 vol. % concentration in the form of a solution in a carbohydrate diluter. Raffinate after copper extraction is returned to particulates leaching, and a portion of the raffinate is separated from the copper production process and forwarded into a nickel production process. Copper re-extraction is carried out using the portion of electrolyte which is recovered from the baths of the separate copper electro-extraction 2 line. Re-extraction product is homogenized with the portion of electrolyte recovered from the separate copper electro-extraction 2 line and is supplied to the copper electro-extraction 2 baths. Marketable copper is produced in baths with lead-based alloy anodes. A portion of acid electrolyte recovered from the baths is mixed with the re-extraction product, and another portion is forwarded back to copper re-extraction.

[0035] PM concentrate is extracted using a flotation method from pulp which results from combined flushing of residues from cinder and particulates leaching. Flotation tails are forwarded into a secondary converter matte production process.

[0036] In an optimal embodiment, the claimed method further includes boiling down and crystallization of copper sulfate from a portion of cinder leaching solutions. As such, it is not the separated portion of electrolyte recovered from copper electro-extraction 1 baths but a master solution from copper sulfate crystallization that is sent to particulates leaching.

[0037] A simplified schematic process diagram of an optimal embodiment of the inventive processing of copper concentrate from flotation separation of converter matte is illustrated in FIG. 2. The method also involves two copper production process lines: electro-extraction 1 from cinder and electro-extraction 2 from particulates.

[0038] The cinder is leached in a circulating solution of the cinder processing line, i.e., solution after copper electro-extraction 1. Residue from cinder leaching is condensed and forwarded to water flushing and flotation together with residue from particulates leaching. After postfiltration, the bulk of the cinder leaching solution is sent to copper electro-extraction 1. A portion of leaching solution after postfiltration, which amounts to 3.5%-4%, is sent to vacuum boiling-down and crystallization of copper sulfate, which is performed at room temperature. Crystallization results in a master solution which is sent to particulates leaching, and in copper sulfate crystals to be dissolved, and the solution is combined with the solution which is sent to postfiltration. Baths are supplied with electrolyte which is obtained by homogenization of postfiltration filter liquid and electrolyte which is recovered from the baths. Marketable copper is produced in baths with lead-based alloy anodes. Part of acid electrolyte recovered from the baths is mixed with postfiltration filter liquid, and another part is returned to cinder leaching.

[0039] Particulates from torrefaction are leached in a portion of raffinate from copper extraction together with the master solution from copper sulfate crystallization. Residue from particulates leaching is condensed and forwarded to water flushing and flotation together with the residue from cinder leaching. Postfiltration filter liquid from the particulates leaching solution is forwarded to copper extraction by solvent extraction. The extraction is carried out using a modified oxyoxime based extractant (Acorga M5640 produced by Cytec InD, or its equivalent) with 30 vol. % concentration in the form of a solution in a carbohydrate diluter. Raffinate after copper extraction is returned to particulates leaching, and a portion of the raffinate is separated from the copper production process and forwarded into a nickel production process. Copper re-extraction is carried out using the portion of electrolyte which is recovered from the baths of the separate copper electro-extraction 2 line. Re-extraction product is homogenized with the portion of electrolyte recovered from the separate copper electro-extraction 2 line and is supplied to the copper electro-extraction 2 baths. Marketable copper is produced in baths with lead-based alloy anodes. A portion of acid electrolyte recovered from the baths is mixed with the re-extraction product, and another portion is forwarded back to copper re-extraction.

EXAMPLES

Example 1. Implementation of the Closest Prior Art Method

[0040] Copper concentrate from flotation separation of converter matte, which contains, in %: Cu—70.7; Ni—3.9; Fe—3.9; S—21.0, is torrefied in a fluidized layer (FL) furnace at a fluidized material layer temperature of 870°−930° C. until sulfur residue content in the cinder is 0.1%. After filtering out particulates, torrefaction gases are forwarded into a sulfur acid production process. Torrefaction results in cinder with the following composition, %: Cu—71.3; Ni—3.9; Fe—3.9; and fine particulates enriched up to 2.0% sulfur, with the following composition, %: Cu—68.7; Ni—4.4; Fe—4.4. Fine particulates output is 15.5% of cinder output.

[0041] Particulates and cinder are leached together at a temperature of 70°−80° C. in a circulating solution after copper electro-extraction, with the following composition, g/l: Cu—35; H.sub.2SO.sub.4—120. Leaching residue is condensed and sent to water flushing and flotation. After postfiltration, cinder leaching solution, having the following composition, g/l: Cu—100; H.sub.2SO.sub.4—15, is sent to copper electro-extraction. Baths are supplied with electrolyte which is obtained by homogenization of postfiltration filter liquid and electrolyte which is recovered from the baths. Using current density of 270 A/m.sup.2-300 A/m.sup.2, marketable copper is produced in baths with lead-based alloy anodes. Bath supply solution has the following composition, g/l: Cu—40; Ni—20; H.sub.2SO.sub.4—112. In a bath, the solution has the following composition, g/l: Cu—35; Ni—20; H.sub.2SO.sub.4—120. A part of electrolyte, which is recovered from the baths, is mixed with postfiltration filter liquid, a part is returned into cinder leaching, and a part is separated for recycling. The amount of solution which is separated for recycling is determined by the maximum allowable nickel content in circulating solutions, which is 20 g/l, thus amounting to 1.45 m.sup.3 per ton of marketable copper. As such, iron content in circulating solutions is 2.4 g/l.

[0042] The separated portion of electrolyte recovered from the baths is boiled down by 3 times to reach acid concentration of 360 g/l. Copper sulfate is cooled and crystallized. Copper sulfate is separated from the master solution and forwarded into a cinder leaching line. Sulfur acid is separated from the master solution using solvent extraction. A mixture containing, in vol. %: 30—C7-C9 fraction trialkylamines, and 70—isooctyl alcohol, is used as the extractant. Acid re-extraction is performed using water. Extraction results in a re-extract with the following composition, g/l: Cu—0.4; Ni—2.1; Fe—0.2; H.sub.2SO.sub.4—135, which is returned into cinder leaching, and raffinate with the following composition, g/l: Cu—11.5; Ni—32.5; Fe—3.6; H.sub.2SO.sub.4—157, which is forwarded into a nickel production process. Nickel to copper ratio in the raffinate which is forwarded into a nickel production process is 2.8 t/t.

[0043] PM concentrate is extracted from the pulp from flushed cinder and particulates leaching residues using a flotation method. Flotation tails are forwarded into a secondary converter matte production process.

[0044] Electro-extraction results in marketable copper, M0k grade copper cathodes according to GOST 546-2001. The copper cathodes do not comply with the highest M00k grade due to selenium content which is standardized to be not higher than 0.00020%. Copper cathodes impurity is caused by increased selenium transfer into the solutions from torrefaction particulates which are rich in selenium.

Example 2. Implementation of the Inventive Method

[0045] Copper concentrate from flotation separation of converter matte, which contains, in %: Cu—70.7; Ni—3.9; Fe—3.9; S—21.0, is torrefied in a fluidized layer (FL) furnace at a fluidized material layer temperature of 870°−930° C. until sulfur residue content in the cinder is 0.1%. After filtering out particulates, torrefaction gases are forwarded into a sulfur acid production process. Torrefaction results in cinder with the following composition, %: Cu—71.3; Ni—3.9; Fe—3.9; and fine particulates enriched up to 2.0% sulfur, with the following composition, %: Cu—68.7; Ni—4.4; Fe—4.4. Fine particulates output is 15.5% of cinder output.

[0046] Thus, the initial material and conditions of its torrefaction, as well as amount and quality of cinder and particulates, are the same as in Example 1.

[0047] Cinder is leached at a temperature of 70°−80° C. in a circulating solution from cinder processing line, which is the solution from copper electro-extraction 1, with the following composition, g/l: Cu—35; H.sub.2SO.sub.4—120. Residue from cinder leaching is condensed and forwarded to water flushing and flotation together with residue from particulates leaching. After postfiltration, cinder leaching solution, which has following composition, g/l: Cu—100; H.sub.2SO.sub.4—15, is sent to copper electro-extraction 1. Baths are supplied with electrolyte which is obtained by homogenization of postfiltration filter liquid and electrolyte which is recovered from the baths. Marketable copper is produced in baths with lead-based alloy anodes. Bath supply solution has the following composition, g/l: Cu—40; Ni—20.0; H.sub.2SO.sub.4—112. Solution in the bath has the following composition, g/l: Cu—35; Ni—20.0; H.sub.2SO.sub.4—120. A part of acid electrolyte recovered from the baths is mixed with postfiltration filter liquid, a part is returned into cinder leaching, and a part is separated for particulates leaching. The amount of solution separated for particulates leaching was 0.66 m.sup.3 per ton of marketable copper produced in the cinder processing line. It is determined by maximum allowable nickel content in solutions which circulate in the cinder processing line, which is 20 g/l. As such, iron content in circulating solutions is 1.4 g/l.

[0048] Particulates from torrefaction are leached at a temperature of 70°−80° C. in a portion of raffinate from copper extraction, which has the following composition, g/l: Cu—2; Ni—16; H.sub.2SO.sub.4—50, together with the separated portion of electrolyte from the cinder processing line (copper electro-extraction 1). Residue from particulates leaching is condensed and forwarded to water flushing and flotation together with the residue from cinder leaching. Filter liquid from the postfiltration of solution from particulates leaching, which has the following composition, g/l: Cu—32; Ni—16; H.sub.2SO.sub.4—3.5, is sent to copper extraction by solvent extraction. The extraction is performed in three stages using a modified oxyoxime based extractant (Acorga M5640 produced by Cytec InD, or its equivalent) with 30 vol. % concentration in the form of a solution in a carbohydrate diluter. Raffinate after copper extraction is returned to particulates leaching, and a portion of the raffinate is separated from the copper production process and is forwarded into a nickel production process. Copper re-extraction is carried out in two stages using the portion of electrolyte recovered from the baths of separate copper electro-extraction 2. The resulting re-extract, which has the following composition, g/l: Cu—50; Ni—8; Fe—0.5; H.sub.2SO.sub.4—147, is homogenized with a portion of electrolyte recovered from the baths of separate copper electro-extraction 2 and is supplied to the baths of copper electro-extraction 2. Using current density of 270 A/m.sup.2-300 A/m.sup.2, marketable copper is produced in baths with lead-based alloy anodes. Bath supply solution has the following composition, g/l: Cu—40; Ni—8; Fe—0.5; H.sub.2SO.sub.4—162. Part of the electrolyte recovered from the baths, which has the following composition, g/l: Cu—35; Ni—8; Fe—0.5; H.sub.2SO.sub.4—170, is mixed with the re-extract, and another part is returned into copper re-extraction.

[0049] The amount of raffinate to be separated into the nickel production process is determined by consistency of salt content (total sulfates content) in solutions from the particulates processing line. Nickel to copper ratio in the raffinate which is forwarded into the nickel production process is 3.7 t/t.

[0050] PM concentrate is extracted using a flotation method from pulp which results from combined flushing of residues from cinder and particulates leaching. Flotation tails are forwarded into a secondary converter matte production process.

[0051] Electro-extraction results in marketable copper, M00k grade copper cathodes according to GOST 546-2001.

Example 3. Implementation of the Inventive Method

[0052] In an optimal embodiment, the claimed method further includes boiling down and crystallization of copper sulfate from a portion of cinder leaching solutions. In this case, it is not the portion of electrolyte recovered from the copper electro-extraction 1 baths, but a master solution from copper sulfate crystallization that is sent to the particulates leaching.

[0053] The initial material and conditions of its torrefaction, as well as amount and quality of cinder and particulates, are the same as in the Example 1.

[0054] The cinder is leached at a temperature of 70°−80° C. in a circulating solution from the cinder processing line, which is the solution from copper electro-extraction 1, which has the following composition, g/l: Cu—35; H.sub.2SO.sub.4—120. Residue from cinder leaching is condensed and forwarded to water flushing and flotation together with residue from particulates leaching. After postfiltration, bulk of the cinder leaching solution, which has the following composition, g/l: Cu—100; H.sub.2SO.sub.4—15, is sent to copper electro-extraction 1. A portion of the leaching solution after postfiltration, in the amount of 0.66 m.sup.3 per ton of cathode copper produced in the cinder processing line, is sent to vacuum boiling-down and crystallization of copper sulfate, which is performed at the temperature of 20° C. Crystallization results in a master solution which has the following composition, g/L: Cu—42; Ni—26; Fe—1.8; H.sub.2SO.sub.4—20, which is sent to particulates leaching, and copper sulfate crystals, which are dissolved and combined with the solution which is provided for the postfiltration. Baths are supplied with electrolyte which is obtained by homogenization of postfiltration filter liquid and electrolyte which is recovered from the baths. Using current density of 270 A/m.sup.2-300 A/m.sup.2, marketable copper is produced in baths with lead-based alloy anodes. Bath supply solution has the following composition, g/l: Cu—40; Ni—20.0; H.sub.2SO.sub.4—112. Solution in the bath has the following composition, g/l: Cu—35; Ni—20.0; H.sub.2SO.sub.4—120. A part of electrolyte recovered from the baths is mixed with the leaching solution, and another part is returned for cinder leaching. The amount of solution which is sent for boiling-down is determined by the maximum allowable nickel content in the solutions that circulate in the cinder processing lines, which is 20 g/l. As such, iron content in the circulating solutions was 1.4 g/l.

[0055] Particulates from torrefaction are leached at a temperature of 70°−80° C. in a portion of copper extraction raffinate, which has the following composition, g/l: Cu—2; Ni—18; Fe—2.0; H.sub.2SO.sub.4—50, together with the master solution from copper sulfate crystallization. Residue from particulates leaching is condensed and forwarded to water flushing and flotation together with the residue from cinder leaching. Filter liquid from postfiltration of solution from particulates leaching, which has the following composition, g/l: Cu—32; Ni—18; Fe—2.0; H.sub.2SO.sub.4—3.5, is sent into copper extraction by solvent extraction. The extraction is performed in three stages using a modified oxyoxime based extractant (Acorga M5640 produced by Cytec InD., or its equivalent) in the form of a solution in a carbohydrate diluter, having a 30 vol. % concentration. Raffinate after copper extraction is returned to particulates leaching, and a portion of the raffinate is separated from the copper production process and forwarded into a nickel production process. Copper re-extraction is carried out in two stages using the portion of electrolyte recovered from the baths of separate copper electro-extraction 2. The resulting re-extract, which has the following composition, g/l: Cu—50; Ni—8; Fe—0.5; H.sub.2SO.sub.4—147, is homogenized with a portion of electrolyte recovered from the baths of separate copper electro-extraction 2 and is supplied to the baths of copper electro-extraction 2. Using current density of 270 A/m.sup.2-300 A/m.sup.2, marketable copper is produced in baths with lead-based alloy anodes. Bath supply solution has the following composition, g/l: Cu—40; Ni—8; Fe—0.5; H.sub.2SO.sub.4—162. Part of the electrolyte recovered from the baths, which has the following composition, g/l: Cu—35; Ni—8; Fe—0.5; H.sub.2SO.sub.4—170, is mixed with the re-extract, and another part is returned into copper re-extraction. The marketable copper is produced in baths with lead-based alloy insoluble anodes using a current density of 270 A/m.sup.2-300 A/m.sup.2.

[0056] The amount of raffinate to be separated into the nickel production process is determined by consistency of salt content (total sulfates content) in solutions from the particulates processing line. Nickel to copper ratio in the raffinate which is forwarded into the nickel production process is 9.1 t/t.

[0057] PM concentrate is extracted using a flotation method from pulp which results from combined flushing of residues from cinder and particulates leaching. Flotation tails are forwarded into a secondary converter matte production process.

[0058] Electro-extraction results in marketable copper, M00k grade copper cathodes according to GOST 546-2001.

TABLE-US-00001 TABLE Ni/Cu Direct Boiling- ratio in copper down rate Market- solutions extraction (amount of Iron able forwarded into evaporated content copper to nickel market- water), m.sup.3 in quality, production able per ton of electro- GOST Example process, product, marketable lyte, 546- No. t/t % copper g/l 2001 1 (closest 2.8 96.7 0.98 2.4 M0k  prior art) 2 3.7 97.65 N/A 1.4 and M00k (inventive 0.5 on method) edges 3 9.1 97.9 0.12 1.4 and M00k (inventive 0.5 on method) edges

[0059] Distinct quantitative characteristics of processing of copper concentrate from flotation separation of converter matte are compared in the Table. It is apparent that, given the same quantitative characteristics of torrefaction and leaching of the same initial material, the claimed method increases the nickel to copper ratio in the solutions which are forwarded into the nickel production process, which explains the increased direct extraction of copper into marketable products. In the claimed method, the iron content in electrolytes from copper electro-extraction baths is reduced, which increases the copper yield to current ratio. The claimed method also reduces the boiling-down ratio, or completely obviates the need for boiling-down. Besides, according to the inventive method, highest grade copper is produced from initial material that is contaminated with impurities.

Example 4. Implementation of the Inventive Method

[0060] Processing of low-iron copper-nickel matte (white matte) produced by smelting in a Vanyukov furnace (VF) and subsequent conversion.

[0061] White matte, which has the following composition, %: Cu—72.5; Ni—3.7; Fe—4.0; S—19.3, is torrefied in a fluidized layer (FL) furnace at a temperature of 850°−880° C. in the boiling material layer until the residual sulfur content in the cinder is about 0.1%. After filtering out particulates, torrefaction gases are forwarded into a sulfur acid production process. Torrefaction results in cinder, which has the following composition, %: Cu—72.0; Ni—3.6; Fe—4.0, and fine particulates, which have the following composition, %: Cu—70; Ni—3.6; Fe—3.9, and are sulfur rich up to 2.0%. Fine particulates output is 11.4% of cinder output.

[0062] The cinder is leached at a temperature of 70°−80° C. in a circulating solution from the cinder processing line, which is the solution from copper electro-extraction 1, which has the following composition, g/l: Cu—35; H.sub.2SO.sub.4—120. Residue from cinder leaching is condensed and forwarded to water flushing and flotation together with residue from particulates leaching. After postfiltration, bulk of the cinder leaching solution, which has the following composition, g/l: Cu—100; H.sub.2SO.sub.4—15, is sent to copper electro-extraction 1. After postfiltration, a portion of leaching solution in the amount of 0.5 m.sup.3 per ton of cathode copper produced in the cinder processing line is sent to vacuum boiling-down and copper sulfate crystallization, which is performed at the temperature of 20° C. Crystallization results in a master solution, which has the following composition, g/l: Cu—42; Ni—26; Fe—2.4; H.sub.2SO.sub.4—21, which is sent to particulates leaching, and copper sulfate crystals, which are dissolved and combined with the solution that is provided to the postfiltration. Baths are supplied with electrolyte which is obtained by homogenization of postfiltration filter liquid and electrolyte which is recovered from the baths. Using current density of 270 A/m.sup.2-300 A/m.sup.2, marketable copper is produced in baths with lead-based alloy anodes. Bath supply solution has the following composition, g/l: Cu—40; Ni—20.0; H.sub.2SO.sub.4—112. Solution in the bath has the following composition, g/l: Cu—35; Ni—20.0; H.sub.2SO.sub.4—120. A part of electrolyte recovered from the baths is mixed with the leaching solution, and another part is returned for cinder leaching. The amount of solution which is sent for boiling-down is determined by the maximum allowable nickel content in the solutions that circulate in the cinder processing lines, which is 20 g/l. As such, iron content in the circulating solutions was 1.8 g/l.

[0063] Particulates from torrefaction are leached at a temperature of 70°−80° C. in a portion of raffinate from copper extraction, which has the following composition, g/l: Cu—2; Ni—15; Fe—1.5; H.sub.2SO.sub.4—50, together with the master solution from copper sulfate crystallization. Residue from particulates leaching is condensed and forwarded to water flushing and flotation together with the residue from cinder leaching. Filter liquid from the postfiltration of solution from particulates leaching, which has the following composition, g/l: Cu—32; Ni—15; Fe—1.5; H.sub.2SO.sub.4—3.7, is sent to copper extraction by solvent extraction. The extraction is performed in three stages using a modified oxyoxime based extractant (Acorga M5640 produced by Cytec InD., or its equivalent) in the form of a solution in a carbohydrate diluter, having a 30 vol. % concentration. Raffinate after copper extraction is returned to particulates leaching, and a portion of the raffinate is separated from the copper production process and forwarded into a nickel production process. Copper re-extraction is carried out in two stages using the portion of electrolyte recovered from the baths of separate copper electro-extraction 2. The resulting re-extract, which has the following composition, g/l: Cu—50; Ni—10; Fe—1.0; H.sub.2SO.sub.4—147, is homogenized with a portion of electrolyte recovered from the baths of separate copper electro-extraction 2 and is supplied to the baths of copper electro-extraction 2. Using current density of 270 A/m.sup.2-300 A/m.sup.2, marketable copper is produced in baths with lead-based alloy anodes. Bath supply solution has the following composition, g/l: Cu—40; Ni—10; Fe—1.0; H.sub.2SO.sub.4—162. Part of the electrolyte recovered from the baths, which has the following composition, g/l: Cu—35; Ni—10; Fe—1.0; H.sub.2SO.sub.4—170, is mixed with the re-extract, and another part is returned into copper re-extraction. The marketable copper is produced in baths with lead-based alloy insoluble anodes using a current density of 270 A/m.sup.2-300 A/m.sup.2.

[0064] The amount of raffinate to be separated into the nickel production process is determined by consistency of salt content (total sulfates content) in solutions from the particulates processing line. Nickel to copper ratio in the raffinate which is forwarded into the nickel production process is 7.5 t/t.

[0065] PM concentrate is extracted using a flotation method from pulp which results from combined flushing of residues from cinder and particulates leaching. Flotation tails are forwarded into a secondary converter matte production process.

[0066] Electro-extraction results in marketable copper, M00k grade copper cathodes according to GOST 546-2001. Direct extraction of copper was 97.4%.

Example 5. Implementation of the Inventive Method

[0067] Processing of copper-nickel matte produced by smelting in a Vanyukov furnace (VF).

[0068] Copper matte, which has the following composition, %: Cu—58.5; Ni—3.04; Fe—14.2; S—23.2, is torrefied in a fluidized layer (FL) furnace at a temperature of 840°−870° C. in the boiling material layer until the residual sulfur content in the cinder is about 0.5%. After filtering out particulates, torrefaction gases are forwarded into a sulfur acid production process. Torrefaction results in cinder, which has the following composition, %: Cu—60.2; Ni—3.1; Fe—14.6; and fine particulates enriched up to 3.0% sulfur, which have the following composition, %: Cu—61.1; Ni—3.2; Fe—14.9. Fine particulates output is 10.9% of cinder output.

[0069] The cinder is leached at a temperature of 70°−80° C. in a circulating solution from the cinder processing line, which is the solution from copper electro-extraction 1, which has the following composition, g/l: Cu—35; H.sub.2SO.sub.4—110. Iron is precipitated from leaching pulp until its residual content is 2.0 g/l by excess cinder while aerating the pulp with oxygen at pH 2.0-2.5. Combined residue from cinder leaching and cleaning out iron is condensed and forwarded to water flushing and flotation together with residue from particulates leaching. After postfiltration, bulk of the cinder leaching solution, which has the following composition, g/l: Cu—97; H.sub.2SO.sub.4—0, is sent to copper electro-extraction 1. After postfiltration, a portion of filter fluid (in the amount of 0.8 M.sup.3 per ton of cathode copper produced in the cinder processing line) is sent to vacuum boiling-down and copper sulfate crystallization, which is performed at the temperature of 20° C. Crystallization results in a master solution, which has the following composition, g/l: Cu—40; Ni—2.8; Fe—4.0; H.sub.2SO.sub.4—0, which is sent to particulates leaching, and copper sulfate crystals, which are dissolved and combined with the solution that is provided to the postfiltration. Baths are supplied with electrolyte which is obtained by homogenization of postfiltration filter liquid and electrolyte which is recovered from the baths. Using current density of 270 A/m.sup.2-300 A/m.sup.2, marketable copper is produced in baths with lead-based alloy anodes. Bath supply solution has the following composition, g/l: Cu—40; Ni—15.0; H.sub.2SO.sub.4—102. Solution in the bath has the following composition, g/l: Cu—35; Ni—15.0; H.sub.2SO.sub.4—110. A part of electrolyte recovered from the baths is mixed with the leaching solution, and another part is returned for cinder leaching. The amount of solution sent to boiling-down was 0.8 M.sup.3 per ton of marketable copper produced in the cinder processing line. It is determined by the amount of solutions which are generated during the combined flushing of cinder and particulates leaching residues. In this case nickel content in solutions that circulated in the cinder processing line was 15 g/l.

[0070] Particulates from torrefaction are leached at a temperature of 70°−80° C. in a portion of raffinate from copper extraction, which has the following composition, g/l: Cu—2; Ni—27; Fe—9.7; H.sub.2SO.sub.4—50, together with the master solution from copper sulfate crystallization. Residue from particulates leaching is condensed and forwarded to water flushing and flotation together with the residue from cinder leaching. Filter liquid from postfiltration of solution from particulates leaching, which has the following composition, g/l: Cu—35.8; Ni—27; Fe—9.7; H.sub.2SO.sub.4—3.5, is sent into copper extraction by solvent extraction. The extraction is performed in three stages using a modified oxyoxime based extractant (Acorga M5640 produced by Cytec InD., or its equivalent) in the form of a solution in a carbohydrate diluter, having a 30 vol. % concentration. Raffinate after copper extraction is returned to particulates leaching, and a portion of the raffinate is separated from the copper production process and forwarded into a nickel production process. Copper re-extraction is carried out in two stages using the portion of electrolyte recovered from the baths of separate copper electro-extraction 2. The resulting re-extract, which has the following composition, g/l: Cu—45.5; Ni—10; Fe—1.0; H.sub.2SO.sub.4—154, is homogenized with a portion of electrolyte recovered from the baths of separate copper electro-extraction 2 and is supplied to the baths of copper electro-extraction 2. Using current density of 270 A/m.sup.2-300 A/m.sup.2, marketable copper is produced in baths with lead-based alloy anodes. Bath supply solution has the following composition, g/l: Cu—40; Ni—10; Fe—1.0; H.sub.2SO.sub.4—162. Part of the electrolyte recovered from the baths, which has the following composition, g/l: Cu—35; Ni—10; Fe—1.0; H.sub.2SO.sub.4—170, is mixed with the re-extract, and another part is returned into copper re-extraction. The marketable copper is produced in baths with lead-based alloy insoluble anodes using a current density of 270 A/m.sup.2-300 A/m.sup.2.

[0071] The amount of raffinate to be separated into the nickel production process is determined by consistency of salt content (total sulfates content) in solutions from the particulates processing line. Nickel to copper ratio in the raffinate which is forwarded into the nickel production process was 13.5 t/t.

[0072] PM concentrate is extracted using a flotation method from pulp which results from combined flushing of residues from cinder and particulates leaching. Flotation tails are forwarded into a secondary converter matte production process.

[0073] Electro-extraction results in marketable copper, M00k grade copper cathodes according to GOST 546-2001. Direct extraction of copper was 94.0%.

[0074] Lower extraction is explained by high iron content in the initial material. In the course of cinder and particulates leaching, a portion of copper remains in the leaching residue in the form of dissolution-resistant ferrites which are generated during torrefaction. At the same time, much iron is transferred into the solution, which iron is again precipitated by means of the cinder. As such, an additional amount of cinder copper remains in the insoluble residue.

[0075] Thus, the claimed method for processing copper and nickel sulfide materials enables an improvement of performance characteristics of copper and nickel sulfide materials processing, an increase in direct extraction of copper into a marketable product, reduced losses of copper and other valuable components, and a reduced incomplete processing of non-ferrous and precious metals by reducing process cycles.