Conversion method of salt of non-ferrous metal

FIELD: metallurgy.

SUBSTANCE: conversion method of non-ferrous metal salt involves counterflow extraction of metal from solution of its converted salt with the use as cation-exchange extractant in salt form of solution of organophosphorus acid in inert diluter and re-extraction of non-ferrous metal with converting acid so that re-extract containing converted salt of non-ferrous metal is obtained. As non-ferrous metal there used is cobalt or nickel; extraction is performed from solution of converted salt of cobalt or nickel at concentration of cobalt or nickel in solution 65-80 g/l and pH 4-7 with the use as cation-exchange extractant of 20-50% solution of organophosphorus acid in sodium, potassium or ammonia form. Re-extraction is performed with 0.5-2.0 M solution of converting acid. Number of non-ferrous metals to which the proposed method is applied can also include copper and zinc.

EFFECT: increasing conversion degree at minimum content of impurities and enlarging the range of obtained salts of non-ferrous metals.

5 cl, 8 ex

 

The invention relates to hydrometallurgy of non-ferrous metals and can be used to produce metal salts of chloride, sulfate and nitrate solutions formed during the processing of polymetallic raw materials.

Currently, salts of non-ferrous metals are obtained by conversion of the corresponding metal salts, oxides or hydroxides, using mainly their dissolution in acids, with subsequent purification of the resulting salt from impurities. This technology is multi-stage, complex purification from impurities and lack of organization of continuous process. Possible conversion of salts of cobalt from one form to another method of deposition. However, precipitation methods in the production of salts are characterized by a low degree of purity of the salts, the presence of roughing operations and formation of intermediate products that are returned into circulation for processing, which significantly complicates the technology. Significant advantages compared with the above methods has the new technology.

A known method of converting salt non-ferrous metals, in particular cobalt (see Karjakin J.V., Angels NI Pure substance. M.: Chemistry, 1973, s), according to which it is heated to 40-50°C converterhome solution of cobalt chloride add a squirt at the continuous AC is shivani hot solution of sodium carbonate. The precipitate containing the converted cobalt carbonate, washed with plenty of water and dried at 50-60°C. the Method allows to obtain the cobalt carbonate mixed with a basic carbonate salt. The conversion of chloride of cobalt carbonate is 90%.

The main disadvantage of this method is the relatively low degree of conversion of cobalt chloride and the presence of impurities in the target product even after repeated washings. The disadvantages of the method include the limited range of the obtained cobalt salts.

A known method of converting salt nonferrous metal, in particular Nickel (see Karjakin J.V., Angels NI Pure substance. M: Chemistry, 1973, s), according to which in the ammonia solution density of 0.91 g/cm3enter convertible Nickel sulfate, the mixture was kept over night, then add the ammonium chloride with obtaining low-solubility emmakate Nickel chloride, which, after filtration and washing calcined at a temperature of 450°C To produce converted of Nickel chloride. The conversion of sulfate Nickel chloride does not exceed 63%.

The disadvantage of this method is the need to obtain an intermediate product and conducting high-temperature calcination, which complicates the way, leads to losses of the target component and, accordingly, reduce the structure conversion. In addition, the disadvantage of this method is the limited range of the obtained salts of Nickel.

Known also adopted as the prototype of a method of converting salt non-ferrous metals, in particular cobalt (see the Caciques A.G., Dyakov L.V., Omelchuk RV Obtaining salts of cobalt extraction method conversion // Sat. materials international. Symposium on sorption and extraction "ISSE-2008", 29 Sept.-4 Oct. 2008, Vladivostok. - Vladivostok, 2008. - P.189-191), including countercurrent extraction of cobalt from adjusted according to the pH value chloride solution convertible cobalt salts composition, g/l: SB - 112; Ni of 0.01; Fe, Mn, Cu<0,005 cation-exchange extractant. The pH adjustment is produced by the introduction of a 5% aqueous solution of ammonia or sodium hydroxide. As the cation-exchange extractant used Caprylic, di-2-ethylhexylamine or alkylphosphines acid in an inert diluent "Escaid". Reextraction are solutions of 2.0-2.8 M nitric, sulfuric or acetic acid. In the case of extraction Caprylic acid take her 50% solution in salineform. Extraction extraction are 4 stages with O:=1:1 translation extract about 70% of cobalt. Reextraction cobalt from the organic phase carry out the conversion of 2 M acetic acid for 2 steps of obtaining reextract containing acetate Koba is it. Reextraction cobalt from the organic phase can also be nitric acid. In the converted salt of cobalt acetate bulk Nickel content does not exceed 0,008%. The degree of conversion of cobalt chloride in acetate is 70%.

The known method is characterized by a low degree of conversion of cobalt chloride in acetate and the limited range of the obtained cobalt salts. The disadvantages of the method include obtaining cobalt acetate containing a mixture of acetic acid, which reduces the quality of the converted salt.

The present invention is directed to the achievement of the technical result consists in increasing the degree of conversion of salts of cobalt and ensuring a high degree of conversion of salts of Nickel with a minimum content of impurities. The technical result is also in expanding the range of the resulting salts.

The technical result is achieved in that in the method of converting salt nonferrous metal, including countercurrent extraction of non-ferrous metal from a solution of its convertible salt used as the cation-exchange extractant is in salt form solution organophosphorus acid in an inert diluent and reextraction non-ferrous metal converts the acid with getting reextract containing convertional non-ferrous metal, according to the invention, as the non-ferrous metal use cobalt or Nickel, the extraction of lead from solution convertible salt of cobalt or Nickel at a concentration of metal in solution 65-80 g/l and pH 4-7 using as a cation-exchange extractant 20-50% solution of organophosphorus acid in sodium, potassium or ammonium form, and reextraction provide 0.5-2.0 M solution converts acid.

The achievement of the technical result is driven by the fact that as a convertible salt of cobalt or Nickel is used, the chloride, sulfate or nitrate.

The achievement of the technical result also contributes to the fact that as the organophosphorus acid is used di-2-ethylhexylamine or alkylphosphines acid, and extraction was carried out with O:=1-2,5:1 2-4 degrees and a temperature of 20-50°C.

The achievement of the technical result is strengthened by the fact that the conversion uses sulfuric acid, acetic acid, hydrochloric acid, nitric acid, and reextraction cobalt or Nickel is carried out at O:=2-5:1, 3-6 degrees.

The achievement of the technical result is also that as a solution convertible salt of cobalt or Nickel is used, the anolyte formed by the electrodeposition of cobalt or Nickel.

The essential features of the claimed invention, determining the amount of provow the th protection and sufficient to obtain the above-mentioned technical result functions and correlate with the results as follows.

Use as non-ferrous metal cobalt or Nickel due to increasing demand for salts of these metals and the need to increase their purity. The range of non-ferrous metals, applies the inventive method may also include copper and zinc.

The conduct of solvent extraction convertible salt of cobalt or Nickel at a concentration of metal in solution 65-80 g/l provides a high degree of extraction of cobalt or Nickel in the organic phase, which improves the conversion rate. When the concentration of the metal in the solution is less than 65 g/l reduced the degree of conversion, and when more than 80 g/l reduced the stability of the solution and possible crystallization convertible salt of cobalt or Nickel, which hinders the extraction and reduces the degree of conversion.

Carrying out the extraction at pH 4-7 convertible solution of salt of cobalt or Nickel is due to cation exchange mechanism of extraction recovery, since the distribution coefficients largely depend on the equilibrium acidity of the aqueous phase: the higher the pH, the more the distribution coefficient and accordingly the degree of extraction of the metal. Since each non-ferrous metal is extracted organophosphorus acids in a particular field pH, when WPI is icenii cobalt, the preferred pH value, close to the lower limit of the stated interval, and when removing the Nickel to the upper boundary. Regulation of the pH of the solution is an aqueous solution of ammonia or sodium hydroxide.

Use as cation-exchange extractant 20-50% solution of organophosphorus acid is in salt form allows, on the one hand, to increase the degree of extraction of cobalt or Nickel, and on the other, to exclude the operation of adjusting the pH equilibrium of the aqueous phase in each stage of extraction that must be made when using organophosphorus acid (H+) form, because in this case there is an exchange of the cation of the metal to hydrogen and is the acidification of the aqueous phase. As the salt forms of organophosphorus acid is preferable to use sodium, potassium or ammonium form, taking into account their availability and the required physico-chemical parameters in relation to the extraction of the conversion.

Using a 20-50% solution of organophosphorus acid due to the capacity of the used extractant and the concentration of the solution convertible salt of cobalt or Nickel. The concentration of the acid is less than 20% leads to a decrease in the degree of extraction of cobalt or Nickel. When the acid concentration of more than 50% significantly deteriorates the hydrodynamics of the extraction process, resulting in the increase the NII duration of phase separation during extraction, as well as the difficult extrakcia cobalt or Nickel, which requires the use of concentrated acids for extraction from the organic phase.

The implementation of the Stripping 0.5-2.0 M solution converts acid due to the completeness of extraction of the target product from the organic phase in the reextract. When using the solution for the conversion of the acid with a concentration of less than 0.5 M is reduced extraction of target product in the reextract and accordingly, the degree of conversion and the concentration of acid is more than 2 M leads to the production of salts contaminated with excess acid.

The combination of the above features is necessary and sufficient to achieve the technical result of the invention to increase the degree of conversion of salts of cobalt and ensuring a high degree of conversion of salts of Nickel with a minimum content of impurities, as well as in expanding the range of the resulting salts.

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

Use as a convertible salt of cobalt or Nickel chloride, sulfate or nitrate due to the fact that during the processing of polymetallic raw materials are mainly formed solutions of these salts, which can be obtained various salts of cobalt and Nickel. This contribute to the t expansion of the range of the resulting salts.

As organophosphorus acid, preferably di-2-ethylhexylamine or alkylphosphines acids that provide full and selective extraction of cobalt or Nickel from a solution of its convertible salt. In addition, these acids have low solubility in water and low degree of hydrolysis. A number of organophosphorus acids, applies the inventive method may also include phosphonic acid.

Conducting extraction with O:=1-2,5:1 2-4 stages provides high recovery of cobalt or Nickel from a solution of its convertible salt at the lowest possible consumption of reagents in the extraction step. The implementation of the extraction O:less than 1:1 provides insufficient high recovery of metal from a solution of its convertible salt, and the ratio of O:over 2.5:1 leads to unnecessary increase in the flow of the extractant. Single-stage conducting the extraction does not provide a sufficiently high extraction of cobalt or Nickel from a solution of its convertible salt. The number of stages more than 4 impractical because of the need to use additional pieces of equipment without significantly increasing the recovery of cobalt or Nickel.

Carrying out the extraction at a temperature of 20-50°C increases the extraction of cobalt or Nickel of his volnogorskoe and improves the hydrodynamics of the extraction process, that is reflected in the decrease in the duration of phase separation during extraction. At temperatures below 20°C decreases the extraction of the metal and increases the duration of phase separation during extraction, and the temperature is above 50°C leads to the loss of solvent due to its evaporation, as well as additional energy for its heating and increases fire risk in the process.

Use as the conversion of the acid sulfuric, acetic, hydrochloric, nitric acids due to the expansion of the range of the resulting salts.

Conducting the Stripping of cobalt or Nickel with O:=2-5:1, 3-6 levels contributes to its deep extraction from the organic phase in the reextract and, consequently, increase the degree of conversion. Holding Stripping O:less than 2:1 results in diluted by salt reextract, which complicates further processing, and O:5:1 does not provide a high extraction of cobalt or Nickel from the organic phase in the reextract. When the number of stages of Stripping less than 3 not achieved a high degree of extraction of the metal in the reextract and the number of step 6 is not desirable because of the small increase in the extraction of the target product as the number of pieces of equipment.

The use of anolyte formed by the electrodeposition of cobalt or Nickel, as p is the target convertible salt of cobalt or Nickel will expand the range of convertible initial solutions. Used the anolyte may contain chlorides or sulphates of cobalt and Nickel, or a mixture of these salts.

The above private features of the invention allow a method in the optimal mode from the viewpoint of obtaining high technological parameters of the process.

The essence of the invention and its advantages can be explained by the following examples of specific performance.

Example 1. 1 l of a solution of a convertible cobalt chloride with pH 4, containing 65 g/l and less than 0.1 g/l amounts of impurities Ni, Fe, Mn, Cu, sent for extraction, where in the countercurrent mode solution in contact with the cation exchange organophosphorus extractant - 20% solution of di-2-ethylhexylamine acid in potassium form in an inert diluent "Escaid". Extraction was carried out with a ratio of organic and aqueous phases O:b=1:1 on 4 stages at a temperature of 20°C with translation in the extract 95.6% of cobalt. The extract in the amount of 1 l sent for reextraction, which is carried out by countercurrent 1.5 M solution converts acetic acid with a ratio A:b=2:1 to 6 stages with obtaining 0.5 l of reextract containing cobalt acetate in the total number of impurities, not more than 0.008% of the cobalt content. The degree of conversion of cobalt chloride in acetate is 95.2%. The reextract can be used to obtain a dry salt of cobalt acetate is Zvezdnyi methods. After Stripping the extractant regenerate with translation in potassium form and sent to the first stage of extraction.

Example 2. 1 l of a solution of a convertible cobalt sulfate with pH 4.5, containing 70 g/l and less than 0.1 g/l amounts of impurities Ni, Fe, Mn, Cu, sent for extraction, where in the countercurrent mode solution in contact with the cation exchange organophosphorus extractant - 40% solution alkylphosphines acid (Cyanex-272) in the sodium form in an inert diluent "Escaid". Extraction was carried out with a ratio of organic and aqueous phases O:b=1.5:1 on 2 stages at a temperature of 50°C with translation in the extract 97.3% of cobalt. The extract in the amount of 1.5 liters sent to reextraction, which is carried by the counter 2 M solution converts nitric acid with a ratio A:b=2:1 to 3 steps of obtaining 0,75 l reextract containing cobalt nitrate in the total number of impurities, not more than 0.008% of the cobalt content. The conversion of sulphate of cobalt nitrate to 97.1%. The reextract can be used to obtain a dry salt of cobalt nitrate known methods. After Stripping the extractant regenerate with translation in sodium form and sent to the first stage of extraction.

Example 3. 1 l of a solution of a convertible cobalt nitrate with pH 4, containing 80 g/l and less than 0.1 g/l amounts of impurities Ni, Fe, Mn, Cu, send the to extraction, where in the countercurrent mode solution in contact with the cation exchange organophosphorus extractant - 50% solution of di-2-ethylhexylamine acid in the ammonium form in an inert diluent "Escaid". Extraction was carried out with a ratio of organic and aqueous phases O:b=2:1 on 2 stages at a temperature of 30°C with translation in the extract of 98.2% cobalt. The extract in the amount of 2 liters sent to reextraction, which is carried out by countercurrent 1.5 M solution for the conversion of hydrochloric acid with a ratio A:b=2:1 to 3 steps of obtaining 1 liter of reextract containing cobalt chloride total impurities not exceeding 0.007% from cobalt content. The degree of conversion of nitrate of cobalt chloride 98%. The reextract can be used to obtain a dry salt of cobalt chloride by the known methods. After Stripping the extractant regenerate with translation in ammonium form and sent to the first stage of extraction.

Example 4. 1 l of a solution of a convertible of Nickel chloride with pH 7, containing 80 g/l Ni and less than 0.1 g/l amounts of impurities, Fe, Mn, Cu, sent for extraction, where in the countercurrent mode solution in contact with the cation exchange organophosphorus extractant - 30% solution of alkyl-phosphinic acid (Cyanex-272) in the potassium form in an inert diluent "Escaid". Extraction was carried out with a ratio of organic and aqueous phases S=2:1 on 2 stages at a temperature of 40°C with translation in the extract 92.4 per cent Nickel. The extract in the amount of 2 liters sent to reextraction, which is carried out by countercurrent 1 M solution converts nitric acid with a ratio A:B=5:1 6 speed transmission with receipt of 0.4 l of reextract containing Nickel nitrate total impurities not exceeding 0.005% of Nickel content. The degree of conversion of Nickel chloride to nitrate 92%. The reextract can be used to obtain a dry salt of Nickel nitrate known methods. After Stripping the extractant regenerate with translation in potassium form and sent to the first stage of extraction.

Example 5. 1 l of a solution of a convertible Nickel sulfate with a pH of 6.5 containing 80 g/l Ni and less than 0.1 g/l amounts of impurities, Fe, Mn, Cu, sent for extraction, where in the countercurrent mode solution in contact with the cation exchange organophosphorus extractant - 40% solution of di-2-ethylhexylamine acid in the sodium form in an inert diluent "Escaid". Extraction was carried out with a ratio of organic and aqueous phases O:b=1.5:1 on 3 stages at a temperature of 35°C with translation in the extract 96,2% Nickel. The extract in the amount of 1.5 liters sent to reextraction, which is carried out by countercurrent 1 M solution for the conversion of hydrochloric acid with a ratio A:b=2:1 to 5 levels with obtaining 0,75 l reextract containing Nickel chloride in the total number of impurities that do not exceed the non 0,007% of the Nickel content. The conversion of sulfate Nickel chloride 95,8%. The reextract can be used to obtain a dry salt of Nickel chloride by the known methods. After Stripping the extractant regenerate with translation in sodium form and sent to the first stage of extraction.

Example 6. 1 l of convertible solution of Nickel nitrate with a pH of 6.5 containing 80 g/l Ni and less than 0.1 g/l amounts of impurities, Fe, Mn, Cu, sent for extraction, where in the countercurrent mode solution in contact with the cation exchange organophosphorus extractant - 30% solution of alkyl-phosphinic acid (Cyanex-272) in the ammonium form in an inert diluent "Escaid". Extraction was carried out with a ratio of organic and aqueous phases O:=2,5:1 to 3 steps at a temperature of 35°C with translation in the extract 94,1% Nickel. The extract in the amount of 2.5 liters sent to reextraction, which is carried out by countercurrent 0.5 M solution converts sulfuric acid with a ratio A:b=2:1 to 5 levels with obtaining 1.25 l of reextract containing Nickel sulfate in the total number of impurities, not more than 0.008% of the Nickel content. The degree of conversion of nitrate Nickel sulfate 93,7%. The reextract can be used to obtain a dry salt of Nickel sulfate known methods. After Stripping the extractant regenerate with translation in ammonium form and sent to the first stage extracts is I.

Example 7. 1 l of a solution of a convertible cobalt chloride, which take the anolyte formed by electroextraction cobalt, pH 4, containing 80 g/l and less than 0.2 g/l amounts of impurities Ni, Fe, Mn, Cu, sent for extraction, where in the countercurrent mode solution in contact with the cation exchange organophosphorus extractant - 30% solution of di-2-ethylhexylamine acid in potassium form in an inert diluent "Escaid". Extraction was carried out with a ratio of organic and aqueous phases O:b=2:1 to 3 steps at a temperature of 30°C with translation in the extract 95.2 per cent cobalt. The extract in the amount of 2 liters sent to reextraction, which is carried out by countercurrent 1.5 M solution converts sulfuric acid with a ratio A:b=2:1 to 5 levels with obtaining 1 liter of reextract containing cobalt sulfate in the total number of impurities, not more than 0.008% of the cobalt content. The degree of conversion of the chloride cobalt sulfate 95%. The reextract can be used to obtain a dry salt of sulfate of cobalt known methods. After Stripping the extractant regenerate with translation in potassium form and sent to the first stage of extraction.

Example 8. 1 l of a solution convertible sulfate-chloride Nickel salts, which take the anolyte formed during electrolysis Nickel, pH 6, containing 80 g/l Ni and less ,2 g/l amounts of impurities, Fe, Mn, Cu, sent for extraction, where in the countercurrent mode solution in contact with the cation exchange organophosphorus extractant - 30% solution alkylphosphines acid (Cyanex-272) in the sodium form in an inert diluent "Escaid". Extraction was carried out with a ratio of organic and aqueous phases O:B=2,5:1 in 4 stages at a temperature of 30°C with translation in the extract 93,2% Nickel. The extract in the amount of 2.5 liters sent to reextraction, which is carried out by countercurrent 1 M solution converts sulfuric acid with a ratio A:b=3:1 to 6 stages with getting 0,83 l reextract containing Nickel sulfate in the total number of impurities, not more than 0.008% of the Nickel content. The conversion of sulfate-chloride salt of Nickel sulfate 93%. The reextract can be used to obtain a dry salt of Nickel sulfate known methods. After Stripping the extractant regenerate with translation in sodium form and sent to the first stage of extraction.

As can be seen from the data presented in the examples, the use of the proposed method to provide a degree of conversion of salts of cobalt 95-98%, Nickel 92,0 is 95.8%, while ensuring the content of the impurities is not more than 0,008%. Compared with the prototype of the conversion of salts of cobalt is increased by 25-28%. The proposed method is relatively simple, can be implemented with COI is whether the standard equipment and provides expansion of the range of the obtained salts of non-ferrous metals. The range of non-ferrous metals, applies the inventive method may also include copper and zinc.

1. A method of converting salt nonferrous metal, including countercurrent extraction of non-ferrous metal from a solution of its convertible salt used as the cation-exchange extractant is in salt form solution organophosphorus acid in an inert diluent and reextraction non-ferrous metal converts the acid with getting reextract containing the converted salt nonferrous metal, characterized in that as non-ferrous metal use cobalt or Nickel, the extraction of lead from solution convertible salt of cobalt or Nickel at a concentration of cobalt or Nickel in solution 65-80 g/l and pH 4-7 using as a cation-exchange extractant 20-50% solution of organophosphorus acid in sodium, potassium or ammonium the form and reextraction provide 0.5-2.0 M solution converts acid.

2. The method according to claim 1, characterized in that as a convertible salt of cobalt or Nickel is used, the chloride, sulfate or nitrate.

3. The method according to claim 1, characterized in that as the organophosphorus acid is used di-2-ethylhexylamine or alkylphosphines acid and extraction is carried out at a:=1-2,5:1 2-4 degrees and a temperature of 20-50°C.

4. The method according to claim 1, characterized those who, as the conversion uses sulfuric acid, acetic acid, hydrochloric acid, nitric acid, and reextraction cobalt or Nickel is carried out at a:=2-5:1, 3-6 degrees.

5. The method according to claim 1, characterized in that as a solution convertible salt of cobalt or Nickel is used, the anolyte formed by the electrodeposition of cobalt or Nickel.



 

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FIELD: metallurgy.

SUBSTANCE: procedure for processing final tailings of galvanic production consists in crumbling, leaching, separation of solution from sedimentation and in extracting heavy non-ferrous metals from produced solution. Also, final tailings are crumbled with mechanic-chemical activation by wet crumbling in form of pulp suspension at pH≤3 and ratio s (solid): l (liquid) = 1:(0.4-1) and temperature 60-90°C.

EFFECT: reduced harmful environmental impact and power expenditures due to elimination of thermal treatment stage at processing final tailings; raised efficiency of extraction of heavy metal compounds.

3 tbl, 1 ex

FIELD: metallurgy.

SUBSTANCE: there are used soluble and insoluble anodes connected to separate sources of current for control over soluble anode dissolution during process of electrolysis and concentration of ions of metal in solution by means of correcting ratio of anode strengths of current of soluble and insoluble anodes at constant value of cathode density of current. Also, constant value of cathode density of current is achieved by constant area of cathode and sum of current strength on the soluble and insoluble anodes.

EFFECT: avoiding labour-intense operation of correction of electrolyte due to equalising cathode and anode current outputs at production of powders of metal.

8 dwg, 3 ex

FIELD: metallurgy.

SUBSTANCE: procedure consists in leaching at atmospheric or raised pressure, in production of effluent and in utilisation of ion-exchanging resins for absorption and extraction of nickel and cobalt. Before extraction of nickel and cobalt effluent in form of solution or pulp is treated with cation or chelate resin possessing selectivity relative to extraction of iron, aluminium and copper for their removal; it also increases pH of solution.

EFFECT: elimination of neutralisation stage of solution, efficient purification of effluent, prevention of nickel losses and avoiding division of solid and fluid phase of formed pulp at laterite ore leaching.

6 cl, 2 dwg

FIELD: metallurgy.

SUBSTANCE: procedure consists in leaching with chloride solution at supply of chlorine, in purification of solution from copper and in production of copper sulphide cake, in extracting concentrate of precious metals and in electro-extraction of nickel from solution. Prior to leaching matte is separated to a sulphide and metallised fractions. The sulphide fraction is subjected to leaching with chloride solution with supply of chlorine. The metallised fraction produced at separation of matte is added into pulp produced at leaching thus performing purification of solution from copper and its withdrawal to copper sulphide cake. Upon purification of solution from copper solution is purified from iron, zinc and cobalt. Copper sulphide cake is roasted and produced cinder is leached. Solution is directed to electro-extraction of copper, while concentrate of precious metals and chamber product are extracted from residue by flotation.

EFFECT: reduced material and operational expenditures and losses of non-ferrous and precious metals.

2 cl, 12 ex, 2 dwg

FIELD: metallurgy.

SUBSTANCE: procedure consists in processing wastes with sulphuric acid at raised temperature, in supplying hydrogen peroxide, in introducing rhenium, nickel and cobalt into leaching solution and in concentrating tungsten, niobium and tantalum in insoluble residue. Further, solution is separated from insoluble residue; extraction of rhenium from solution is leached with secondary aliphatic alcohol. Extract is washed and rhenium is re-extracted with leaching solution upon extraction. Hydrogen peroxide is supplied after main part of nickel and cobalt have passed into solution at maintaining redox potential in interval of 0.50-0.75 V relative to a saturated chlorine-silver electrode, while extraction of rhenium, extract washing and rhenium re-extraction are carried out on 2-5 steps.

EFFECT: increased extraction of rhenium at reduced consumption of oxidant, increased safety of procedure due to separated in time operations followed with release of hydrogen and oxygen.

6 cl, 4 ex

FIELD: metallurgy, in particular complex metal recovery from oxidized ore.

SUBSTANCE: claimed method includes granulation with sulfuric acid. Obtained granules are sulfated at 250-4500C for 1-2 h in one or two steps. Then leaching of nickel and other metal sulfates are carried out followed by metal recovery using known methods. Invention is useful in reprocessing of oxidized nickel-cobalt ores, as well as laterite ores containing nickel, cobalt, and copper, and iron-manganese nickel-containing nodules.

EFFECT: high yield nickel recovery; inexpensive and usable equipment.

3 cl, 3 tbl, 4 ex

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