Processing method of sulfide copper-nickel concentrate

FIELD: metallurgy.

SUBSTANCE: it is implemented treatment of copper-nickel sulfide concentrate by fluoride and/or ammonium bifluoride at the temperature 165-210°C during 2-3 hours with forming of hard fluorination products and emission of ammonia gas and water vapor. Fluoride and/or ammonium bifluoride are used in amount 1.0-1.2 from stoichiometric with respect to overall content in copper-nickel concentrate of silicates and pyrrhotine. Hard fluorination products exposed to water leaching at the temperature 40-60°C and S:L=1:5-6 during 1-2 hours with transformation to residue nickel sulfide, copper, cobalt, platinum metal and magnetite, and into solution - fluorine-ammonium silicon saline, magnesium, iron, aluminium and calcium. Residue is separated from solution and exposed to magnetic separation with magnetite extraction. Received solution is neutralised by ammonia water till providing of pH 8-10 with regeneration of fluoride and/or ammonium bifluoride and receiving of residue of magnesium, iron, aluminium, calcium and silica hydroxides. In the capacity of ammonia water for solution neutralisation can be used ammonia gas and water vapors from the stage of raw materials fluorination. Formed ammonium fluoride and/or bifluoride are returned to raw materials treatment stage.

EFFECT: energy content reduction and providing of selectivity sulfide crude ore treatment at less number of operations.

5 cl, 1 dwg, 4 ex

 

The invention relates to the hydrometallurgical processing of sulphide ore raw materials, in particular to the processing of sulphide copper-Nickel concentrates containing valuable metals Nickel, copper, cobalt and platinum group metals.

There is a method of processing sulphide ores, mainly gold (see RF Patent №2120487, IPC6SW 11/00, 1998), including preliminary roasting of the ore at 650-750°and handling of fluoride and/or biperiden ammonium when the mass ratio of ore to the fluorinating agent is 1:1.2 to 3.5 and a temperature of 170-190°with the formation of solid products of fluorination and gaseous ammonia and water vapor, heat treatment of products of fluorination at 450-650°With sublimation fluorosilicate preparation and/or hexaferrites ammonium and ammonium fluoride and the formation of gold-bearing non-volatile residue, fluoridation of non-volatile residue in the mass ratio of the balance to the fluoride and/or ammonium bertarido 1:0.3 to 0.4 and temperature of 150-170°C. Then perftorirovannye the residue is subjected to water leaching to produce sediment rough gold associated with leftorium minerals, including zircon, and magnetite, and solution formoney salts of iron and aluminum. The precipitate rough gold is subjected to magnetic separation with separation of magnetite, the solution formoney salts neutralize the ammonia water with the regeneration of fluoride and/or byflorida ammonium and obtaining a precipitate of hydroxides of iron and aluminum. Regenerated fluoride and/or before ammonium return to the stage of ore processing. Gold recovery in the non-magnetic fraction is 97,6%.

The disadvantages of this method are its high energy consumption due to the need to pre-oxidation firing and subsequent thermal processing of products of fluorination, and a significant number of operations to achieve the desired selectivity, which complicates and increases the cost method.

Also known is a method of processing copper-Nickel sulfide concentrate with the extraction of valuable metals (see RF Patent №2057193, IPC6SW 11/00, 11/02, 1996), comprising preparing a mixture of concentrate, containing 19-20 wt.% sulphides of non-ferrous metals and iron, 55-60 g/t platinum group metals, and the flux in the form of carbonatite in the number of 30-32% by weight of the mixture, melting the mixture at 1300-1350°in an inert or low reduction atmosphere with obtaining the slag melt and matte containing Nickel, copper, cobalt, platinum group metals and iron, separating the slag melt and pressure oxidative leaching of the matte with obtaining a solid residue of platinum group metals and a solution containing non-ferrous metals and iron.

The disadvantages of this method are its high energy consumption as a result of operating the heat of the mixture at high the temperatures, limited selectivity, due to the transfer in Stein iron along with precious metals, as well as the necessity of using an inert or reducing atmosphere during the smelting of the charge, which complicates and increases the cost method.

The present invention is directed to the achievement of the technical result consists in reducing the energy intensity of the method of processing of sulphide copper-Nickel concentrate and increase its selectivity.

The technical result is achieved by a method for processing copper-Nickel sulfide concentrate with the extraction of valuable metals, which consists in the processing of concentrate fluoride and/or biperiden ammonium, taken in an amount of 1.0 to 1.2 from stoichiometric with respect to the total content in the copper-Nickel concentrate silicates and pyrrhotite, when heated with the formation of solid products of fluorination and gaseous ammonia and water vapor, water leaching of the solid products of the fluorination with translation sulphides precious metals - Nickel, copper, cobalt and platinum group metals and magnetite precipitates, and formoney salts of iron, aluminum, silicon, magnesium and calcium in the solution, separating the precipitate, its magnetic separation with the separation of magnetite, neutralization of a solution of ammonia water with the regeneration of fluoride and/or byflorida ammonium and received the eat precipitate hydroxides of iron, aluminum, silica and hydroxides of magnesium and calcium and the return of fluoride and/or byflorida ammonium to the stage of processing of the concentrate.

The technical result is also achieved by the fact that the processing of copper-Nickel concentrate fluoride and/or biperiden ammonium carried out at a temperature 165-210°C for 2-3 hours.

The technical result is also achieved by the fact that the leaching of solid products of the fluorination is conducted at a temperature of 40-60°and T:W=1:5-6 1-2 hours.

The technical result is achieved by the fact that the neutralization solution formoney salts of silicon, magnesium, iron, aluminum and calcium are to provide a pH of 8-10.

On the technical achievement of the aims that as ammonia water to neutralize the solution using gaseous ammonia and water vapor from the stage fluorination concentrate.

The essential features of the claimed invention, defining the scope of legal protection and sufficient to obtain the above-mentioned technical result function and correlate with the results as follows.

The introduction of fluoride and/or byflorida ammonium in the amount of 1.0 to 1.2 from stoichiometric with respect to the total content in the copper-Nickel concentrate silicates (Mg2SiO4,(Mg,Fe)2SiO4,Mg2Al4(OH)8Si3O10,(Mg,e) 6(OH)8[Si4O10],Mg3(OH)2[Si4O10],CaMgSi2O6and others) and pyrrhotite (Fe1-xS) due to the need for the most complete fluorination of these minerals with the formation of water-soluble formoney salts of silicon, magnesium, iron, aluminum and calcium. With the introduction of fluoride and/or byflorida ammonium in the amount of less than 1.0 from the stoichiometric not provided the complete fluorination of silicates and pyrrhotite, which leads to decrease in the content in the Deposit of precious metals. When the amount of fluoride and/or byflorida ammonium over 1.2 from stoichiometry will be overrun fluorinating reagent without a noticeable improvement in the selectivity of the process. In addition, there may be in the gas phase HF.

Water leaching products of the fluorination - formoney salts of silicon, magnesium, iron, aluminum and calcium can translate them into a solution and separating the insoluble precipitate sulfides of Nickel, copper, cobalt and platinum group metals, as well as magnetite, which emit magnetic separation.

Neutralization of the resulting solution of ammonia water ensures precipitated silica and hydroxides of magnesium, iron, aluminum and calcium and helps to regenerate the fluoride and/or before ammonium and return to the stage of processing of the concentrate.

Owls is the synergy of the above features is necessary and sufficient to achieve the technical result of the invention, lowering the intensity of a method for processing copper-Nickel sulfide concentrate and increase its selectivity.

In some cases, of the preferred embodiment of the invention the following specific operations and operational parameters.

Processing copper-Nickel concentrate fluoride and/or biperiden ammonia at a temperature of 165-210°within 2-3 hours following reason. Treatment at a temperature of less than 165°does not provide a complete fluorination of silicates and pyrrhotite, which reduces the selectivity of the method. Maintenance treatment at a temperature of more than 210°leads to unnecessary increase in power consumption and losses fluorinating reagent as a result of his selection in the gas phase. It was established experimentally that the time interval of 2-3 hours allows you to perform a complete fluorination of silicates and pyrrhotite.

The leaching of solid products of fluorination at a temperature of 40-60°and T:W=1:5-6 due to the fact that leaching at a temperature below 40°and the ratio of T:W less than 1:5 does not provide a complete translation solution formoney salts, which reduces the selectivity of the method. Leaching at temperatures above 60°leads to increased energy consumption, and the ratio of T:W more than 1:6 is impractical for economic reasons. Experiments have shown that the time interval 1-2 hours allows you provide a full translation into solution formoney salts of silicon, magnesium, iron, aluminum and calcium, and separating the insoluble precipitate sulfides of Nickel, copper, cobalt and platinum group metals, as well as magnetite.

Neutralization of ammonia water solution formoney salts of silicon, magnesium, iron, aluminum and calcium to provide a pH of 8-10 due to the fact that the process at pH below 8 is not possible to achieve complete hydrolysis formoney salts of silicon, magnesium, iron, aluminum and calcium, which leads to contamination of the regenerated fluoride and/or byflorida ammonium. The process at pH above 10 leads to incomplete precipitation of the hydroxides of magnesium, iron, aluminum and calcium and silica.

The use of ammonia for neutralization of a solution of gaseous ammonia and water vapor from the stage fluorination concentrate more cost-efficient and environmentally friendly way.

The above private features of the invention allow the processing of sulphide copper-Nickel concentrate in an optimal manner from the point of view of energy consumption reduction method and increase its selectivity.

On the accompanying drawing is a diagram of the processing of sulphide copper-Nickel concentrate according to the claimed invention.

The method is as follows. Previously conducted flotation beneficiation of sulfide ores from elfennau particle size up - 0.1 mm, ensuring total content of sulphides precious metals 19-20%. Obtained in the process of enrichment of copper-Nickel concentrate 1 process at a temperature of 165-210°C for 2-3 hours a fluoride and/or biperiden ammonium, which take in the amount of 1.0 to 1.2 from stoichiometric with respect to the total content in the copper-Nickel concentrate silicates and pyrrhotite. In these conditions fully ftorida silicate minerals with the formation of solid products of fluorination 2 and release into the gas phase ammonia and water vapor 3. Sulphides of non-ferrous metals - pentlandite (Ni,Fe9S8and chalcopyrite CuFeS2practically do not interact with fluoride and/or biperiden ammonium. Minor fluoridation of pentlandite and chalcopyrite occurs time, incongruently, resulting in the formation of new sulfide phases: the millerite NiS, bornite Cu5FeS4, covellite CuS, enriched with non-ferrous metals. Pyrrhotite also reacts with fluoride and/or biperiden ammonium education hexaferrite ammonium when the degree of opening of the mineral - 80-90%. Then the solid products of the fluorination is subjected to water leaching 4 at a temperature of 40-60°and T:W=1:5-6 1-2 hours. The sulfides of Nickel, copper, cobalt and platinum group metals are almost entirely insoluble in draft 5, and formoney salts credit the Deposit, magnesium, iron, aluminium and calcium into solution 6. The degree of extraction of Nickel, copper, cobalt and platinum group metals in the sediment is thus 98-99%. Because the sediment also contains magnetite, which does not react with fluoride and/or biperiden ammonium, further processing of the sludge includes magnetic separation 7 selection 8 and magnetite sulfide 9 concentrates. Sulphide concentrate 9 sent for further processing in a known manner. A solution of 6 formoney salts of silicon, magnesium, iron, aluminum and calcium is subjected to neutralization with 10 ammonia water, which is injected as a separate reagent, or form by passing through a solution of 6 gaseous ammonia and water vapor 3 emitted from the fluoridation of copper-Nickel concentrate 1. Formed during the neutralization of 10 fluoride and/or before ammonium 11 after regeneration of the solution returns to the beginning of the process to the stage of processing of concentrate to 1, and the obtained residue 12 of the hydroxides of magnesium, iron, aluminum and calcium and silica is subjected to heat treatment (drying and calcining) 13. The resulting product is used to produce building materials.

The nature and advantages of the invention can be illustrated by the following Examples.

Example 1. 1000 g of sulfide max the Nickel concentrate size - 0.1 mm, containing, wt.%: pentlandite 15, chalcopyrite 5, pyrrhotite 19, magnetite 6, 45 serpentine and talc 10, and the platinum group metals in an amount of 5 g/t, process 1892,3 g byflorida ammonium NH4HF2(the stoichiometric amount relative to the total content in the concentrate of silicates and pyrrhotite) at a temperature of 165°C for 3 hours. The resulting solid products of fluorination in the number 2175,4 g is subjected to a water leach at a temperature of 60°and T:W=1:5 for 1 hour. Released by fluoridation gaseous ammonia and water vapor in amounts respectively of 35.4 g and 369,5 g sent for recycling. The sulfides of Nickel, copper, cobalt, platinum group metals and magnetite are almost entirely in the insoluble precipitate, and formoney salts of silicon, magnesium, iron, aluminum and calcium into solution. The sediment in the number 353,3 g is separated from the solution by filtration. The degree of extraction of Nickel, copper, cobalt and platinum group metals in the sediment is 98%. The precipitate is subjected to magnetic separation with separation of 63 g of magnetite and 290,3 g of sulfide concentrates. The sulphide concentrate is sent for further processing by the method of pressure oxidative leaching. The solution formoney salts of silicon, magnesium, iron, aluminum, and cal is tion in the amount of 1.1 l is subjected to neutralization to ensure pH 8 ammonia water, contains 1185 NH4OH. Regenerated after neutralization solution before ammonium in the amount of 1870 return to the stage of processing of the concentrate. The precipitate hydroxides of magnesium, iron, aluminum and calcium and silica in the amount of 926 g is subjected to drying at 110°and calcining at 620°C. the resulting product in the amount of 621 g can be used in the production of construction materials.

Example 2. 1000 g of sulfide copper-Nickel concentrate particle size is 0.1 mm, containing, wt.%: pentlandite 16, chalcopyrite 4, pyrrhotite 17, magnetite 9, olivine 32, 4 serpentine, talc 4 and diopside 2, and the platinum group metals in the amount of 5.2 g/t handle 1558,6 g byflorida ammonium NH4HF2(1,1 of the stoichiometric amount relative to the total content in the concentrate of silicates and pyrrhotite) at a temperature of 210°C for 2 hours. The resulting solid products of fluorination in the number 1856,7 g is subjected to a water leach at a temperature of 40°and T:W=1:6 for 2 hours. Released by fluoridation gaseous ammonia and water vapor in the amount of respectively 22.9 grams and 238 g sent for recycling. The sulfides of Nickel, copper, cobalt, platinum group metals and magnetite are almost entirely in the insoluble precipitate, and formoney salts of silicon, magnesium, iron, aluminium the Oia and calcium into solution. The sediment in the number 362,6 g is separated from the solution by filtration. The degree of extraction of Nickel, copper, cobalt and platinum group metals in the sediment is 99%. The precipitate is subjected to magnetic separation with separation of 98 g of magnetite and 264,6 g of sulfide concentrates. The sulphide concentrate is sent for further processing by the method of pressure oxidative leaching. The solution formoney salts of silicon, magnesium, iron, aluminum and calcium in the amount of 1.12 l is subjected to neutralization to ensure pH 10 ammonia water containing 780 g NH4OH. Regenerated after neutralization solution before ammonium in the number of 1550 g return to the stage of processing of the concentrate. The precipitate hydroxides of magnesium, iron, aluminum and calcium and silica in the amount of 783 g is subjected to drying at 120°and calcining at 650°C. the resulting product number 552 can be used in the production of construction materials.

Example 3. 1000 g of sulfide copper-Nickel concentrate particle size is 0.1 mm, containing, wt.%: pentlandite 14, chalcopyrite 5, pyrrhotite 15, magnetite 7, olivine 35, 8 serpentine, chlorite 7, talc 7 and diopside 2, and the platinum group metals in the amount of 4.9 g/t handle 2378 g of ammonium fluoride NH4F (1,2 of the stoichiometric amount relative to the total of the in content in the concentrate of silicates and pyrrhotite) at a temperature of 200° C for 2.5 hours. The resulting solid products of fluorination in the number 2185,7 g is subjected to a water leach at a temperature of 50°and T:W=1:5.5 V for 1.5 hours. Released by fluoridation gaseous ammonia and water vapor in the amount of respectively 564 g and 321,7 g is directed to the operation of neutralization. The sulfides of Nickel, copper, cobalt, platinum group metals and magnetite are almost entirely in the insoluble precipitate, and formoney salts of silicon, magnesium, iron, aluminum and calcium into solution. The resulting residue 338 g is separated from the solution by filtration. The degree of extraction of Nickel, copper, cobalt and platinum group metals in the sediment is to 98.6%. The precipitate is subjected to magnetic separation with separation of 74 g of magnetite and 264 g of sulfide concentrates. The sulphide concentrate is sent for further processing by the method of pressure oxidative leaching. The solution formoney salts of silicon, magnesium, iron, aluminum and calcium in the amount of 1.15 l is subjected to neutralization to ensure pH 10 ammonia water containing 1098 g NH4OH, which use released by fluoridation gaseous ammonia and water vapor. Regenerated after neutralization of the solution of ammonium fluoride in the number 2330 g return to the stage of ebrabarceloneta. The precipitate hydroxides of magnesium, iron, aluminum and calcium and silica in the amount of 979 g is subjected to drying at 130°and calcining at 600°C. the resulting product number 679 g can be used in the production of construction materials.

Example 4. 1000 g of sulfide copper-Nickel concentrate particle size is 0.1 mm composition as in Example 1, process 2174,5 g of a mixture of fluoride NH4F and byflorida ammonium NH4HF2taken in the ratio of 1.3:1 (stoichiometric amount relative to the total content in the concentrate of silicates and pyrrhotite), at a temperature of 170°C for 3 hours. The resulting solid products of fluorination in the number 2191,9 g is subjected to a water leach at a temperature of 55°and T:W=1:5.5 V for 1.5 hours. Released by fluoridation gaseous ammonia and water vapor in the amount of respectively USD 329.8 g and 375,4 g is directed to the operation of neutralization. The sulfides of Nickel, copper, cobalt, platinum group metals and magnetite are almost entirely in the insoluble precipitate, and formoney salts of silicon, magnesium, iron, aluminum and calcium into solution. The sediment in the number 341,2 g is separated from the solution by filtration. The degree of extraction of Nickel, copper, cobalt and platinum group metals in the sediment is 98,1%. The precipitate was subjected to the Ute magnetic separation with separation of 62.5 g of magnetite and 278,7 g of sulfide concentrates. The sulphide concentrate is sent for further processing by the method of pressure oxidative leaching. The solution formoney salts of silicon, magnesium, iron, aluminum and calcium in the amount of 1.2 l is subjected to neutralization to ensure pH 9 ammonia water containing 1212 NH4OH, which use released by fluoridation gaseous ammonia and water vapor. Regenerated after neutralization of the solution mixture of fluoride and byflorida ammonium in the number 2170 g return to the stage of processing of the concentrate. The precipitate hydroxides of magnesium, iron, aluminum and calcium and silica in the amount of 955 subjected to drying at 120°and calcining at 630°C. the resulting product number 643 g can be used in the production of construction materials.

From the analysis above Examples show that the proposed method compared with the prototype to reduce energy intensity and increase the selectivity of processing of sulphide copper-Nickel concentrate. The method enables the extraction of Nickel, copper, cobalt and platinum group metals in the range of 98-99%. The proposed method is relatively simple and can be implemented using commercially available reagents and standard equipment.

1. A method of processing copper-Nickel sulfide concentrate is rata with the extraction of valuable metals, involved in the processing of concentrate fluoride and/or biperiden ammonium, taken in an amount of 1.0 to 1.2 from stoichiometric with respect to the total content in the copper-Nickel concentrate silicates and pyrrhotite, when heated with the formation of solid products of fluorination and gaseous ammonia and water vapor, water leaching of the solid products of the fluorination with translation sulphides precious metals - Nickel, copper, cobalt and platinum group metals and magnetite precipitates, and formoney salts of iron, aluminum, silicon, magnesium and calcium in the solution, separating the precipitate, its magnetic separation with the separation of magnetite, neutralization solution of ammonia water with the regeneration of fluoride and/or byflorida ammonium and obtaining a precipitate of the hydroxides of iron, aluminum, silica and hydroxides of magnesium and calcium and the return of fluoride and/or byflorida ammonium to the stage of processing of the concentrate.

2. The method according to claim 1, in which the processing of sulphide copper-Nickel concentrate fluoride and/or biperiden ammonium carried out at a temperature 165-210°C for 2-3 hours

3. The method according to claim 1, wherein the leaching of the solid products of the fluorination is conducted at a temperature of 40-60°and T:W=1:5-6 1-2 hours

4. The method according to claim 1, in which the neutralization solution formoney salts of silicon, magnesium, iron, aluminum and calcium outdo provide a pH of 8-10.

5. The method according to claim 1 or 4, in which the ammonia water to neutralize the solution using gaseous ammonia and water vapor from the stage fluorination of raw materials.



 

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4 cl, 3 dwg, 1 tbl, 11 ex

FIELD: metallurgy.

SUBSTANCE: invention refers to hydrometallurgy, particularly to method of leaching of base metals out of oxidised ores, for example, out of laterite ore, at extraction of nickel and/or cobalt by heap leaching. The method consists in (a) dividing ore to small and large fractions, (b) leaching of large fraction of ore in a leaching solution with a corresponding leaching agent for leaching out metals contained therein, and (c) using small fractions of ore or part of it for neutralisation or partial neutralisation of the leaching agent contained in a saturated leaching solution obtained at stage (b) to transfer certain amount or total amount of saturated leaching solution for further purifying or refining. Then a base metal, for example, nickel and/or cobalt is extracted out of the solution.

EFFECT: reduction of operational costs and increased efficiency of extracting metals from ore.

10 cl, 1 dwg

FIELD: metallurgy.

SUBSTANCE: invention concerns metallurgy field. Particularly it concerns receiving technique of nickel and can be used at treatment of efficient solutions of sulfuric acid leaching of nickel. Treatment technique of sulfuric acid nickel-bearing solutions includes its rectification from ferric iron by solution neutralisation till pH=5 and extraction from it nickel. At that neutralisation till achieving pH=4 is implemented by alkali metal hydrate, and further neutralization from pH=4 till pH= 5 - by aqua ammonia.

EFFECT: increasing of nickel extraction from efficient solution of sulfuric acid leaching at its purification from ferric iron.

2 tbl, 2 ex

FIELD: metallurgy.

SUBSTANCE: invention concerns metallurgy field. Particularly it concerns nickel recovery methods from oxidised nickel ore. Method includes grinding of nickel ore, its mixing to sulphur addition and chlorides of alkaline or alkali-earth metal, mixture burning at presence of water steam with further cooling. After cooling it is implemented sulfuric acid leaching of burnt mixture and further treatment of productive solution. At that before burning mixture of grinned ore with admixtures is subjected to graining and drying, and after burning granulated mixture is cooled on air with further keeping on air.

EFFECT: increasing of filtration speed of burnt ore after sulfuric acid leaching, decreasing of ferrous iron content in productive solution, simplification of process instrument appearance and reduction of expenditures for method implementation.

2 tbl, 2 ex

FIELD: metallurgy.

SUBSTANCE: invention concerns metallurgy field. Particularly it concerns nickel and cobalt recovery. Method of nickel and cobalt recovery from nickel- and cobalt-containing laterite ores includes burning of source ore in deoxidising atmosphere in rotary calciner for selective reduction of nickel and cobalt, at that before burning reducer either is not added at all or is added in quantity less than 2.5% mass to the source ore and then it is implemented leaching of reduced ore by means of ammonium carbonate aerated ammoniac solution for nickel and cobalt extraction into leach solution. Then leach solution is separated from ore rejects and nickel and cobalt are extracted by means of liquid extraction by organic reagent, deposition or ion exchange.

EFFECT: increasing of radiant efficiency sufficient degree of nickel and cobalt extraction.

18 cl, 4 ex, 5 tbl

FIELD: metallurgy.

SUBSTANCE: invention refers to hydro metallurgy of non ferrous metals and can be used at development of practices for hydro metallurgical processing of solutions containing zinc together with nickel and/or copper and/or cobalt. The method includes introducing a sulphur containing reagent into the solution and heating it at a temperature of 130-170°C. At that thiosulfate as a sulphur containing reagent is used at a consumption rate of 110-130% from stoicometric required for sedimentation of nickel, cobalt and copper; this reagent is introduced into initial solution containing nickel and zinc and at least one of metals like cobalt, copper and iron. The suggested method allows extraction out of solution of nickel, copper and cobalt in form a heading with low degree of a zinc codeposition.

EFFECT: processing without seeding agent and reduction of process time.

4 cl, 6 tbl, 6 ex

FIELD: metallurgy of non-ferrous metals.

SUBSTANCE: invention pertains to the metallurgical industry, predominantly to the metallurgy of nickel and cobalt. It concerns procurement methods of liquid metals with reprocessing of an oxygenized, metal-containing natural raw material and technogenic materials. This method works in the follow manner: the melted slag of a fusion mixture, consisting of initial material, flux agent, liquid and firm slag, carbon-containing material and oxygen in an oxygen-containing forced draught, is introduced into an oxygenized area of the twin-chambered furnace. The fusion mixture must be provided in appropriate quantities that would guarantee complete burning of carbon and the highest heat emission. Thereafter a fusion of slag is performed, resulting in the liquid slag formed. The product is then introduced into the recreation area along with the carbon-containing material, oxygenated draught and additional fluxes in such quantities as deemed sufficient to, firstly, restore oxides of obtained metals in the metal phase and, secondly, to indemnify for the lost thermal expenses. The relations between expenses of an oxygenated material per ton of the obtained material in the oxidative and restorative areas must be maintained within the 0.3-2.5 range, and a specific oxygen consumption rate in these areas should be preserved within the range of 0.7-3.0. Periodically, prior to an emission of the metal component of the fused products in the slag siphon, it is heated with an electric arc at the border between the sintered and metal baths until the 1350 - 1500°C range of temperatures is finally reached. Before emitting of the metal component, the molten mass must be kept still for some 10 to 15 minutes while electricity has to be switched off on electrodes. The technical result of this process increases extraction of metals and is a significant improvement of division between the sintered and metal baths.

EFFECT: improvement of the metal extraction when the raw materials, containing non-ferrous metals and iron, are reprocessed.

1 ex

FIELD: non-ferrous metallurgy; methods of extraction of nickel by reduction, cooling and subsequent processing of ore, by hydrometallurgical method, for example.

SUBSTANCE: reduced ore at cooling is loosened by inert gas and is cooled by indirect method with the aid of cooling medium.

EFFECT: enhanced efficiency of extraction of nickel due to more efficient cooling.

10 cl, 1 dwg, 1 ex

FIELD: nonferrous metallurgy.

SUBSTANCE: invention relates to processing nickel-containing intermediate products, namely ferriferous cakes obtained in hydrometallurgical nickel production process. Method comprises repulping of cakes with acid solution containing alkaline metal salts at elevated temperature and maintaining pH of pulp between 1.2 and 1.6. Repulping is effected in reactor provided with mechanical stirring means at specific stirring power in first stage 500-1000 W/m3 and in second stage 5-100 W/m3.

EFFECT: enhanced removal of nickel and improved filterability of products.

8 cl, 5 tbl

FIELD: nonferrous hydrometallurgy; other industries; methods of reprocessing of materials containing nickel in its protoxide form.

SUBSTANCE: invention is pertaining to the hydrometallurgy of non-ferrous metals and may be used at development of the production processes of refining of the converter mattes and reprocessing of other material containing nickel in its protoxide form. The method includes dissolution of these products in solutions of inorganic acids at potential of no less than 1.2 V of the hydrogen electrode, for what they introduce into the initial mash the oxidant, which if necessary is used in the course of production process for maintaining of the necessary value of the redox potential. The method allows to leach the persistent mineral forms containing nickel protoxide in the atmospheric conditions with production of solutions, containing less than 10 g/dm3 of the free acid at the variable concentration of nickel. The technical result of the invention is the increased extraction of the nickel into the solution at simplification of the production method.

EFFECT: invention ensures the increased extraction of the nickel into the solution at simplification of the production method.

2 cl, 3 tbl, 4 ex

FIELD: nickel and cobalt metallurgy, in particular, processing of return converter slag of nickel-cobalt production.

SUBSTANCE: method involves providing mixed charging into shaft furnace of burden containing agglomerate, coke, mixture of lime with pyrites, return converter slag; smelting for producing of nickel material and waste slag; introducing return converter slag into burden in the form of mixture with pyrites used in the ratio of (9-14):1.

EFFECT: increased extent of extracting nickel and cobalt in matte.

2 ex

FIELD: metallurgy.

SUBSTANCE: invention concerns methods of residue utilisation. Particularly it concerns method of copper extraction from sulphate containing dust of copper production. Method includes water leaching of dust with copper and impurity elements conversion into leaching solution, separation of solution from insoluble residue, liquid solvent extraction of copper by oximne extractant with receiving of copper-bearing extract and raffinate, containing impurity elements. After extraction it is implemented copper re-extraction, cleaning of received re-extract from extragent and electro-extraction of copper with receiving of commercial copper and reversible electrolyte. At that water leaching of dust is implemented at temperature 60-100°C and H:L=1:2-4. Leaching solution is cooled with crystallisation of copper main part in the form of vitriol and forming of mother solution, containing residual part of copper. Vitriol is separated from mother solution, dissolved in sulphuric solution and fed to electro-extraction, and liquid solvent extraction is implemented from mother solution.

EFFECT: receiving of qualitative cathode copper of grade MOOK with yield into commercial product up to 98% of copper at high (90,5-93,5%) yield by stream, and also in reduction of material flow volume and deep separation of copper from impurity elements.

9 cl, 3 ex

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