Processing method of copper manufacturing dust

FIELD: metallurgy.

SUBSTANCE: invention concerns processing method of copper manufacturing dust. Method includes dust leaching at elevated temperature with transferring of copper and iron into solution, separation of solution from insoluble residue, separation of copper and iron. Than it is implemented evaporation of solution, containing basic quantity of copper, blue copperas crystallisation, separation of blue copperas crystals from growth solution and extraction from growth solution of residual quantity of copper. At that solution evaporation is implemented till providing of its density 1.30-1.36 g/cm3. Separation of copper and iron is implemented during the process of blue copperas crystallisation. Received blue copperas crystals are dissolved in sulfuric solution till providing of sulfuric acid concentration 100-250 g/l. Formed solution of blue copperas is exposed to basic electro- extraction with receiving of cathode copper and gate-type electrolyte. Extraction of copper residual quantity from growth solution is implemented by additional electro- extraction. Copper extraction degree from dust into solution at leaching is defined by content of copper in dust in oxidised form and reach 99.4%. Total copper extraction into cathodic metal is 89.4-95.2%.

EFFECT: receiving of qualitative cathode copper of grades MOOK, MOK, M1K, and also copper sponge at outlet by current on basic electro- extraction till 93,3% and at additional - till 74,6%.

10 cl, 4 ex

 

The invention relates to methods for processing recyclable waste pyrometallurgical processes of non-ferrous metallurgy, containing copper in an oxidized form of iron and other metals, and can be used in the processing of copper dust production.

Currently dust most of the copper production process by returning in pyrometallurgical processes, which leads to loss of valuable items and pollution by toxic metals. Known methods of individual processing dust are not universal, as the dust generated during the processing of various types of copper-bearing materials, differ considerably in their chemical and phase composition. For oxidized copper dust production technology sulfide copper-Nickel materials cannot achieve a high degree of extraction of copper in high-quality marketable products. This is due to the presence of dust in a significant (up to 5%) amounts of iron, as well as a wide range of other impurity elements.

A method of refining copper dust production (see Blatov I.A., Khomchenko O.A., Maksimov V.I., Caciques A.G. Getting activator for flotation of dusts copper-Nickel production. // Non-ferrous metals. 1997. No. 6. - P.16-20), comprising leaching the dust with water, filtering the slurry separating insoluble OS is Atka from a solution of copper sulphate, crystallization of copper sulfate with obtaining technical copper sulphate and the mother liquor and purification of the mother liquor from the iron for use in copper production.

The disadvantage of this method is that formed as the end product of copper sulphate is largely contaminated with impurities of non-ferrous metals and iron, therefore its use is restricted for use as activator flotation of sulfide copper-Nickel ores. The method does not provide a high degree of extraction of copper in commercial products and do not include further processing of copper sulphate to obtain high-quality cathode copper.

Also known is a method of processing copper dust production (see Bogacheva L.M., Ismatov HR Hydrometallurgical processing of copper-containing materials. // Tashkent: Publishing house "FAN" of the Uzbek SSR. 1989. - Pp.92-109, 29, b), comprising leaching the dust with water or sulfuric acid solution at 90-98°and T:W=1:2,2-4 for 2 hours to obtain solutions containing 40,0-96,3 g/l of copper and to 58.5 g/l iron, separating the leaching solution from the insoluble residue, the cleaning solution from the iron by the precipitation of ammonium hydroxide or potassium (jarosite process), evaporation of the pure solution, crystallization of copper sulfate, otdeleniye solution, neutralization of the solution and additional extraction of copper from him precipitation method of producing crude copper-containing product.

The disadvantage of this method is that it also does not provide a high recovery of copper in high-quality commercial products, because after crystallization and separation of copper sulphate subsequent to extract copper from the mother liquor is carried out with obtaining a copper-containing product is low quality. In addition, the presence of allocations of iron in the sediment, which sbresny product, leads to additional copper losses and increase the flow of the reactants.

The present invention is directed to the achievement of the technical result consists in obtaining high-quality copper cathode from copper dust production while providing high output current and high degree of extraction of copper in commercial products.

The technical result is achieved in that in the method of processing copper dust production, including dust leaching at elevated temperature with the transfer of copper and iron in solution, separating the solution from the insoluble residue, the separation of copper and iron), evaporation of the solution containing the major amount of copper, the crystallization of copper sulfate, separating crystals of copper sulfate from the mother liquor and removing from matchevaluator ostalnogo amounts of copper, according to the invention, evaporation of the solution is carried out to ensure its density of 1.30-1,36 g/cm3separation of copper and iron is carried out in the process of crystallization of copper sulfate, the resulting crystals of copper sulphate are dissolved in sulfuric acid solution to provide a concentration of sulfuric acid 100-250 g/l, the resulting copper sulfate solution is subjected to the main electroextraction to produce cathode copper and electrolyte compartment, and removing residual copper from the mother liquor perform additional electroextraction.

The technical result is also achieved by the fact that processing is subjected to dust copper production, containing at least 15 wt.% copper in the oxidized form.

The technical result is achieved by the fact that the dust leaching is carried out at a temperature of 70-95°and With respect to T:W=1:2-5.

On the technical achievement of the aims that the leaching of dust carry water or condensate formed during the process of evaporation, or sulfuric acid solution, or spent electrolyte copper production.

On the achievement of the technical result is also aimed that the ratio of copper and iron in the copper sulfate is at least 35:1.

On the achievement of the technical result is also aimed that as a sulfuric acid solution for rest the rhenium crystals of copper sulphate using spent electrolyte copper production.

The achievement of the technical result is driven by the fact that the main electroextraction lead at a concentration of copper in solution 30-50 g/l

The achievement of the technical result also contributes to the fact that additional electroextraction carried out at an initial concentration of copper in a solution of 45 g/l and less.

The achievement of the technical result is strengthened by the fact that basic and additional electroextraction carried out at a cathode current density of 200 to 300 a/m2.

On the achievement of the technical result is also aimed that 10-50% off electrolyte main electroextraction served on more electroextraction.

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.

Evaporation of the solution to ensure its density of 1.30-1,36 g/cm3allows the crystallization of copper sulfate to separate the main amount of copper from iron. Evaporation to density below 1.30 g/cm3accompanied by the reduction of sulphate and evaporation to the higher density of 1.36 g/cm3increases the degree of co-precipitation of iron, followed by dissolution of crystals of copper sulfate in sulfuric acid solution leads to the appreciation is the iron content in the solution, supplied to electroextraction, and causes a significant reduction of the current output. In addition, evaporation of the solution to the higher density of 1.36 g/cm3leads to premature crystallization of copper sulfate, which is undesirable.

Dissolution of crystals of copper sulphate in sulphuric solution allows to obtain an electrolyte with a given conductivity, from which copper can be efficiently allocated through electroextraction. Dissolution of crystals of copper sulfate in sulfuric acid solution with a sulfuric acid concentration of 100-250 g/l, due to the fact that when the concentration of the acid is less than 100 g/l significantly reduced the conductivity of the solution, thereby increasing the power consumption to obtain high-quality copper, and increasing the concentration of sulfuric acid of more than 250 g/l leads to corrosion of equipment, excessive consumption of sulfuric acid and the formation of more toxic aerosols.

The main electroextraction electrolyte allows to effectively isolate the copper from the receiving compartment of the electrolyte and high quality copper cathode (brand M00K and M0K), which is a more popular product on the market of non-ferrous metals compared with copper sulphate.

Removing residual copper from the mother liquor an additional electroextraction allows basmajian the solution to a residual copper concentration 5 g/l to produce commodity copper cathode brands M0K and M1K and copper sponge, which can be used to obtain copper. All this helps to improve the extraction of copper from the dust.

The combination of the above features is necessary and sufficient to achieve the technical result of the invention to obtain high-quality copper cathode from copper dust production while providing high output current and high degree of extraction of copper.

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

The content in the dust is not less than 15 wt.% copper in the oxidized form contributes to its high extraction of dust and allows you to get conditioned copper-containing solutions, suitable for efficient crystallization of copper sulfate.

The leaching at a temperature of 70-95°and With respect to T:W=1:2-5 ensures a high degree of extraction of copper from dust, and to prevent crystallization of copper sulphate leaching. Lowering the temperature below 70°To reduce the degree of extraction of copper and the formation of crystals of copper sulphate, which is caused by the dependence of the solubility of copper sulphate on temperature. The temperature rise of more than 95°accompanied With unnecessary power consumption for heating of the solution. The increase in the content of the solid phase of the reference to liquid more than 1:2 leads to deterioration of the kinetic characteristics of the process, the formation of saturated copper solution and crystallization of copper sulphate leaching. A reduction in the content of the solid phase relative to the liquid below 1:5 does not allow you to get conditioned for the copper content of the solution, which leads to increased consumption during the subsequent evaporation of the solution upon receipt of vitriol.

The leaching water translates into a solution of copper contained in the dust in the sulfate form. Leaching of dust using the condensate formed during the process of evaporation, contributes to the economy of industrial water and electricity needed to heat it. The leaching of dust using a sulfuric acid solution translates into a solution of copper contained in the dust in sulfate and oxide forms. Leaching using spent electrolyte copper production formed at various stages of electrolytic copper recovery, contributes to the economy of commodity sulfuric acid and reduces the amount of acid drainage enterprises.

The ratio of copper and iron in the crystals of copper sulphate is at least 35:1 due to the fact that the dissolution of crystals of sulphate in sulphuric solution should be obtained from the solution corresponding to the requirements on the level of impurities in the electrolyte supplied to the electro is straccia, which ultimately provided quality copper at high current output.

Use as a sulfuric acid solution to dissolve the crystals of copper sulphate spent electrolyte copper production contributes to the economy of commodity sulfuric acid and allows you to limit the amount of acidic waste company.

Conducting basic electroextraction copper from sulfuric acid solution of copper sulphate at a concentration of copper in solution 30-50 g/l provided quality saleable copper cathode grades M00K and M0K at high output current. Holding electroextraction from a solution containing less than 30 g/l copper, degrades the quality of the cathode metal above marks and reduces the current output, and the conduct of electroextraction from a solution containing more than 50 g/l copper, accompanied by dentatoalatum, which reduces the grade of copper.

Additional electroextraction when the initial concentration of copper in a solution of 45 g/l and less allows you to produce copper cathode or cathode metal in the form of copper sponge, which is then used to produce copper. The upper limit of the initial concentration of copper in a solution of 45 g/l due to its content in the mother solution. In addition, more electroextraction when the concentration of copper in solution 15-45 g/l allows recip is th commodity copper cathode brands M0K, M1K. Holding electroextraction at copper concentrations of less than 15 g/l provides deep obezbedjivanje solution in order to reduce the losses in the copper production to produce cathode sponges, which can then be sent to the pyrometallurgical process to produce copper at the current technology. It is desirable that the lower limit of the concentration of copper in solution when additional electroextraction was limited by the amount of 5 g/l as the concentration of copper is less than 5 g/l, the formation on the cathode highly toxic arsenic hydrogen.

Conducting primary and secondary electroextraction at a cathode current density in the range 200 to 300 a/m2allows the production of cathode copper in the optimal mode from the point of view of economic and technological parameters of the process. The decrease in cathodic current density of 200 a/m2on the main and additional electroextraction any of the above limits the concentration of copper in solution makes the process uneconomical, as it increases the time capacity of the cathode metal and the increase in cathodic current density of more than 300 a/m2leads to deterioration of the grade of metal (the formation of dendrites, loose cathode metal and the like) due to the fact that the capacity of copper is too fast.

Submission 10-50% off electroly is and the main electroextraction additional electroextraction contributes to increasing the degree of extraction of copper from dust due to a deep abuseive electrolyte, obtained by dissolving copper sulphate.

The above private features of the invention allow a method in the optimal mode from the viewpoint of obtaining high-quality copper cathode from copper dust production while providing high output current and high degree of extraction of copper.

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

Example 1. Dust converting copper matte in the amount of 10 kg, containing, wt.%: Cu 18.1 and 1,6 Fe (content of copper in the oxidized form 18,0%), leached 20 l of water (T:W=1:2) at a temperature of 70°C for 1 hour with the transfer of copper and iron in solution. The solution is separated from the insoluble residue by filtration. The degree of extraction in the solution amounted, %: Cu - 99,4, Fe - 98,9. A solution containing, g/l: Cu 90,0, Fe 8,2, evaporated to a density of 1.30 g/cm3and cooled within 6 hours to a temperature of 5°with the crystallization of copper sulfate. When this occurs the separation of the copper from the main part of iron. The obtained crystals of copper sulphate is separated from the mother liquor by centrifugation. Copper sulphate containing, wt.%: Cu 24,0, Fe 0,4 (ratio of Cu:Fe=60:l), dissolved in sulfuric acid solution to provide a concentration of sulfuric acid 100 g/l, resulting in a solution that serves the main electroextraction. the main electroextraction lead from the solution, containing 50 g/l of copper at a cathode current density of 300 a/m2. The result of cathode copper brand M00K with copper content of 99.99% and iron 0,0009% and isolating the electrolyte. The current output on the main electroextraction amounted to 93.3%. The mother liquor after separation of the crystals of copper sulphate acidified to the concentration of H2SO4100 g/l and serves on additional electroextraction. Additional electroextraction lead from a solution containing 45 g/l Cu and 5.6 g/l Fe at a cathode current density of 300 a/m2. You get a copper cathode mark M0K with a copper content of 99.97% and iron 0,001%, and copper sponge. The current output for additional electroextraction have to 74.6%. The concentration of copper in solution after additional electroextraction - 6 g/l Total extract copper from the solution in the cathode metal in the primary and secondary electroextraction amounted to 95.2 per cent.

Example 2. Dust converting copper matte in the amount of 10 kg, containing, wt.%: Cu 23.5 and Fe 2,4 (the content of copper in the oxidized form 22,9%), leached 30 litres of condensate formed in the process of evaporation (T:W=1:3) at a temperature of 80°C for 1 hour with the transfer of copper and iron in solution. The solution is separated from the insoluble residue by filtration. The degree of extraction in the solution amounted, %: Cu - 97,4, Fe - 98,6. A solution containing, g/l: Cu 76,3, Fe 7,9, upari is up to the density of 1.36 g/cm 3and cooled within 6 hours to a temperature of 5°with the crystallization of copper sulfate. When this occurs the separation of the copper from the main part of iron. The obtained crystals of copper sulphate is separated from the mother liquor by centrifugation. Copper sulphate containing, wt.%: Cu 24,5, Fe 0,7 (ratio of Cu:Fe=35:1), dissolved in sulfuric acid solution to provide a concentration of sulfuric acid 250 g/l, resulting in a solution that serves the main electroextraction. The main electroextraction lead from a solution containing 30 g/l of copper at a cathode current density of 250 a/m2. The result of cathode copper brand M0K with a copper content of 99.98% and iron 0,0008% and shut electrolight current on the main electroextraction was 92.6%. The mother liquor after separation of the crystals of copper sulphate serves on additional electroextraction together with 50% of the volume of electrolyte compartment of the main electroextraction. Additional electroextraction lead from a solution containing 20 g/l Cu and 6.3 g/l Fe at a cathode current density of 250 a/m2. You get a copper cathode mark M1K with a copper content of 99.96% and iron 0,002%, and copper sponge. The current output for additional electroextraction made up 72.1%. The concentration of copper in solution after additional electroextraction - 5 g/l Total izvlecheny the copper from the solution in the cathode metal in the primary and secondary electroextraction amounted to 89.4 per cent.

Example 3. Dust reverberatory smelting of copper concentrate in an amount of 10 kg, containing, wt.%: Cu 42,5 and Fe 3,0 (content of copper in the oxidized form 25,0%), leached 40 l sulfuric acid solution containing 100 g/l H2SO4, (T:W=1:4) at a temperature of 95°C for 1 hour with the transfer of copper and iron in solution. The solution is separated from the insoluble residue by filtration. The degree of extraction in the solution amounted, %: Cu - 58,8, Fe - 62,5. A solution containing, g/l: Cu 62,5, Fe 4,7, evaporated to a density of 1.32 g/cm3and cooled within 6 hours to a temperature of 5°with the crystallization of copper sulfate. When this occurs the separation of the copper from the main part of iron. The obtained crystals of copper sulphate is separated from the mother liquor by centrifugation. Copper sulphate containing, wt.%: Cu 19,1, Fe 0,4 (ratio of Cu:Fe=48:l), dissolved in spent electrolyte copper production to ensure the concentration of sulfuric acid 200 g/l, resulting in a solution that serves the main electroextraction. The main electroextraction lead from a solution containing 40 g/l of copper, at a cathode current density of 200 a/m2. The result of cathode copper brand M00K with copper content of 99.99% and iron 0,001% and isolating the electrolyte. The current output on the main electroextraction amounted to 91.2%. The mother liquor after separation of the crystals IU the aqueous sulphate serves on additional electroextraction together with 10% of the volume of electrolyte compartment of the main electroextraction. Additional electroextraction lead from a solution containing 30 g/l Cu and 5.9 g/l Fe at a cathode current density of 200 a/m2. You get a copper cathode mark M0K with a copper content of 99.98% and iron 0,0009%, and copper sponge. The current output for additional electroextraction amounted to 71.5%. The concentration of copper in solution after additional electroextraction - 5 g/l Total extract copper from the solution in the cathode metal in the primary and secondary electroextraction amounted to 94.8%.

Example 4. Dust reverberatory smelting of copper concentrate in an amount of 10 kg, containing, wt.%: Cu of 29.4 and Fe 2,4 (the content of copper in the oxidized form to 15.0%), leached 50 l (T:W=1:5) the spent electrolyte copper production composition, g/l: H2SO4130, 32 Cu, Ni 16,8, 0,9 Fe, at a temperature of 90°C for 1 hour with the transfer of copper and iron in solution. The solution is separated from the insoluble residue by filtration. The degree of extraction in the solution amounted, %: Cu - 50,0, Fe - 55,8. A solution containing, g/l: Cu 53,4, Fe 5,7, evaporated to a density of 1.34 g/cm3and cooled within 6 hours to a temperature of 5°with the crystallization of copper sulfate. When this occurs the separation of the copper from the main part of iron. The obtained crystals of copper sulphate is separated from the mother liquor by centrifugation.

Copper sulphate containing, wt.%: Cu 22,5, Fe 0,5 (aspect] is the solution of Cu:Fe=46:l), dissolve in sulfuric acid solution to provide a concentration of sulfuric acid 180 g/l, resulting in a solution that serves the main electroextraction. The main electroextraction lead from a solution containing 35 g/l copper, at a cathode current density of 230 a/m2. The result of cathode copper brand M0K with a copper content of 99.97% and iron 0,001% and isolating the electrolyte. The current output on the main electroextraction amounted to 91.6%. The mother liquor after separation of the crystals of copper sulphate serves on additional electroextraction together with 30% of the volume of electrolyte compartment of the main electroextraction. Additional electroextraction lead from a solution containing 20 g/l Cu and 7.8 g/l Fe at a cathode current density of 230 a/m you get a copper cathode mark M1K with copper content of 99.95% and iron 0,001%, and copper sponge. The current output for additional electroextraction amounted to 71.0 per cent. The concentration of copper in solution after additional electroextraction - 6 g/l Total extract copper from the solution in the cathode metal in the $ 94.2%.

From the analysis above examples show that the proposed method can obtain high-quality cathode copper grades M00K, M0K, M1K, and copper sponge from dust copper production during the current output on the main electroextraction is about to 93.3% and more - to 74,6%. The degree of extraction of copper from dust in the solution during leaching is determined by the content of copper in the dust in the oxidized form and reaches 99.4 per cent. The total recovery of copper from leaching solution in the cathode metal is 89,4-95.2 per cent. The proposed method does not require the use of expensive reagents, it is relatively simple and can be implemented using standard equipment.

1. A method of processing copper dust production, including dust leaching at elevated temperature with the transfer of copper and iron in solution, separating the solution from the insoluble residue, the separation of copper and iron), evaporation of the solution containing the major amount of copper, the crystallization of copper sulfate, separating crystals of copper sulfate from the mother liquor and the extraction of the mother liquor residual amounts of copper, characterized in that the evaporation of the solution is carried out to ensure its density of 1.30-1,36 g/cm, the separation of copper and iron is carried out in the process of crystallization of copper sulfate, the resulting crystals of copper sulphate are dissolved in sulfuric acid solution to provide a concentration of sulfuric acid 100-250 g/l, the resulting copper sulfate solution is subjected to the main electroextraction to produce cathode copper and electrolyte compartment, and removing the residual amount of mediis mother liquor perform additional electroextraction.

2. The method according to claim 1, characterized in that the processing is subjected to dust copper production, containing at least 15 wt.% copper in the oxidized form.

3. The method according to claim 1, characterized in that the leaching of lead dust at a temperature of 70-95°and With respect to T:W=1:2-5.

4. The method according to any one of claims 1 to 3, characterized in that the leaching of dust carry water or condensate formed during the process of evaporation,

or sulfuric acid solution, or spent electrolyte copper production.

5. The method according to claim 1, characterized in that the ratio of copper and iron in the crystals of copper sulphate is at least 35:1.

6. The method according to claim 1, characterized in that as a sulfuric acid solution to dissolve the crystals of copper sulphate using spent electrolyte copper production.

7. The method according to claim 1, characterized in that the main electroextraction lead at a concentration of copper in solution 30-50 g/l

8. The method according to claim 1, characterized in that the additional electroextraction carried out at an initial concentration of copper in a solution of 45 g/l and less.

9. The method according to claim 7 or 8, characterized in that the basic and additional electroextraction carried out at a cathode current density of 200 to 300 a/m2.

10. The method according to claim 7, characterized in that 10-50% off electrolyte main electroextraction serves on electroe is straccia.



 

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5 cl, 5 ex

FIELD: metallurgy.

SUBSTANCE: method includes leaching of material with water solution of chemical reagent and successive treatment of produced pulp for extraction of germanium and zinc. At that leaching is carried out with mechanical, grinding and disintegrating effect, using as solution chemical reagent of solution, containing oxidant at amount from 1.8 to 2.5 kg per 1 kg of germanium contained in source material and hydroxide of alkali metal at amount maintaining medium pH from 12 to 14 at ratio of solid and liquid phases 1:(3-8). Germanium is sorption settled out of produced pulp by means of transmission of pulp through ion exchanging resin; alkali at amount facilitating 13.5-14 pH of medium and water at amount facilitating ratio of solid and liquid phases 1:(5-8) are added to pulp. Product received after sorption sedimentation of germanium is treated in autoclave at temperature of 120-250°C and pressure of 6-40 atm. Then liquid phase is separated out of which zinc is extracted while germanium is eluated out of ion exchanging resin. Germanium is extracted out of produced eluate.

EFFECT: increased degree of germanium and zinc extraction.

4 cl, 2 ex

FIELD: metallurgy.

SUBSTANCE: invention refers to extraction and concentration of thorium out of process waste of loparit concentrates treatment - spent melt of saline sprinkler filter (SSF) of loparit concentrate chlorination process. The method includes preparation of suspension by means of discharge of spent melt of saline sprinkler filter (SSF) into water, incorporation of high molecular flocculant, of holding, filtering, separation of sediment, obtaining of chloride solution, and of treatment with steel scrap and metal magnesium. Prior to obtaining chloride solution the source suspension is heated to 60-90°C and treated with solution of sodium hydroxide to pH 1.5-2.0 and to 0.1-0.3% solution of high molecular flocculant at amount of 3-5% from the source volume of suspension; then suspension is held for 2-4 hrs. Chloride solution is received by means of filtration of spent suspension obtaining sediment of rare metals; chloride solution is then treated with steel scrap and metal magnesium; at that the solution is successively treated first with the steel scrap at amount of 3-5 mass fractions of iron per 1 fraction of iron ions (III) in chloride solution at 80-100°C for 1-3 hrs till achieving the value of pH in a pulp equal to 3.0-3.5. Then the pulp is separated from the non-reacted portion of the steel scrap and is treated with metal magnesium to pH 3.5-4.5, and further with 0.1-0.3% solution of high molecular flocculant taken at amount of 5-20% from the volume of chloride solution. Thus produced pulp is held without mixing for 1-4 hrs and filtered producing thorium containing sediment; the said sediment is washed at filter first with solution containing 1-5 g/dcm3 of sodium sulphite, then with water. Washed out sediment is repulped in solution of sodium hydroxide with concentration of 50-150g/dcm3 at a ratio of "Ж:Т"=3-5 at 60-90°C for 2-3 hrs, after what the pulp is filtered with separation of alkaline filtrate. Thorium containing sediment at the filter is washed with water, pressed at the filter and dried; the alkaline filtrate and process water are merged and mixed, then heated to 80-90°C, and treated with solution of sodium hydroxide to pH 11-13 with production of hydroxide pulp. Hydroxide pulp is filtered and then radioactive sediment is produced at the filter; it is washed out with water and transferred to a special wastes depositary, while filtrate is mixed with 10-20 volumes of shop flush water, heated to 80-90°C and again treated with solution of sodium hydroxide to pH 11-13. Obtained pulp is held and filtered thus producing sediment of rare metals and deactivated chloride solution which is discharged to drainage. Sediment of rare metals is unloaded from the filter, merged with sediment of rare metals extracted from the source suspension, dried, washed out and then transferred for preparation of charge for its further chlorination together with the loparit concentrate.

EFFECT: upgraded efficiency of thorium extraction and simultaneously solving problem of neutralisation and utilisation of process waste.

1 dwg, 1 ex

FIELD: metallurgy.

SUBSTANCE: invention refers to non-ferrous metallurgy and can be used for extraction of vanadium out of ashes which is waste produced by burning of sulphuric vanadium containing black oil in heat engines of heat and hydropower stations. The method consists in the following: source ashes are mixed with sodium carbonate and water at a weight ratio of 100:(10-60):(30-50), then produced mixture is held at temperature of 100-150°C, preferably 115-120°C, during 2 hours. Vanadium is leached out of produced self-diffusing cake with water at temperature of 95-100° and a ratio of liquid: solid = (1.5-3):1.

EFFECT: avoiding of generating harmful gas exhausts at extraction of vanadium and implementation of available equipment.

1 tbl, 2 ex

FIELD: blasting.

SUBSTANCE: method for pile loosening by blasting in heap leaching (HP) of ores is used to intensify the HP process due to performing drilling-and-blasting works. The method for pile loosening by blasting in heap leaching of ores, whereby a pad is formed by protective drainage 14 and damp-proof layers 15 made of polymeric film, consists in drilling boreholes 2, placing low-density explosive charges into the boreholes 2 and blasting of said charges. The boreholes 2 are drilled to the depth of the protective and drainage layer 14, charges 9 and 12 are distributedly disposed in the boreholes 2. Pieces 13 and 11 of an expanded material, e.g., foamed polystyrene, are placed respectively in the lower part of the borehole and between the charges. The charges are blasted with time delaying beginning from the top charge 9 to the bottom one 12.

EFFECT: increase in the efficiency of ore loosening; prevention of damage of the anti-seepage polymeric film membrane and of penetration of the toxic solution into ground waters.

1 dwg

FIELD: metallurgy.

SUBSTANCE: said utility invention relates to the field of noble metal metallurgy, in particular, to methods of recovery of osmium from non-ferrous metallurgy platinum-containing electrolytic slime processing products, namely, cakes containing selenium and non-ferrous metals. The cake is subjected to preliminary caustic treatment with caustic soda solution with a concentration of 180-220 g/dm3, and the residual matter resulting from the separation is heated at a temperature of 100 to 130°C. The heated residual matter is subjected to treatment with sulphuric acid and secondary caustic treatment. The osmium concentrate resulting from the caustic treatment is sent for the distillation of the osmium tetraoxide, with its recovery using ammonia solution and subsequent preparation of osmium salt.

EFFECT: increase in efficiency and maximum simplification of osmium recovery process.

4 cl, 3 dwg, 1 tbl, 11 ex

FIELD: hydrometallurgy and mining industry; ecological methods of extraction of metals.

SUBSTANCE: proposed method of extraction of metals from solid metal-containing materials or ores includes treatment or underground leaching-out with solution of reagent obtained by electrolysis treatment of solution containing halogenide-anion and separation of metal from this solution. Electrolysis treatment is carried out under condition of positive mass transfer on revolving electrode or on electrode moving at acceleration of no less than 0.1 m/s. After electrolysis treatment, water-soluble polymer used as surfactant is introduced into reagent solution in the amount of no less than 0.01%.

EFFECT: enhanced efficiency and ecological safety due to reduced power requirements, intensification of process, avoidance of toxic emissions and use of safe chemicals.

7 cl, 2 dwg, 6 ex

FIELD: hydrometallurgy of extraction of non-ferrous, rare-earth and noble metals from rebellious raw materials containing natural carbon or other rebellious compounds.

SUBSTANCE: proposed method includes treatment of rebellious carbon-containing mineral raw material by oxygen-containing oxidant followed by extraction of noble metal compounds from liquid phase. Treatment of carbon-containing mineral raw material by oxygen-containing oxidant is carried out in presence of reductants possessing donor-acceptor properties which are expressed in the fact that at first stage of chemical reactions, reductants give off their electrons to oxygen-containing oxidant, forming stronger oxidant as compared with first one in form of short-lived radicals and intermediate products of oxidation of donor-acceptor reductants which are also used as oxidants.

EFFECT: increased extraction of non-ferrous, rare-earth and noble metals; low cost of process.

3 ex

FIELD: non-ferrous metallurgy; pressure hydrometallurgy and processing of oxidized silicate nickel ores enriched with magnesium.

SUBSTANCE: proposed method includes sulfidizing stage and oxidizing stage with the use of elemental sulfur at the sulfidizing stage in form of aqueous suspension and oxygen at the oxidizing stage. At the sulfidizing stage, use is made of solution of sulfates with bivalent cation and surfactant which facilitates hydrophilization of elemental sulfur; surfactant is fed to suspension at grinding the sulfur which makes it possible to perform both stages of pressure leaching at temperature below 200°C and total pressure in autoclave below 2.0 Mpa, thus ensuring high extraction of nickel into solution up to 93-97%.

EFFECT: considerable reduction of pressure leaching temperature and total pressure in autoclave at high extraction of nickel into solution.

2 cl, 4 ex

FIELD: metallurgy.

SUBSTANCE: invention concerns hydrometallurgy of nonferrous and noble metals, mainly extraction of copper and gold from sulfur wastes which are wastes from sulfuric acid manufacturing, and can be used at dense, cuvet and percolation leaching. Method includes piling of sulfur wastes to antifilter basis, influence upon it of precipitations during its storage, collection of underspoil acid water, its additional if necessary acidation by sulfuric acid and copper leaching at values of pH and Eh of productional solutions 2.0-2.5 and 500-540 mV respectively. After reduction of copper concentration less than 100 mg/l there are reduced content of oxidant and acid in leaching solution, thiocarbamide is introduced in it, noble metals are leached, and mainly it is gold. Extracted in solution copper and gold are isolated by cementation.

EFFECT: reduction of reagent unit discharge, expenditures of energy and increasing of copper and gold extraction ratio.

4 cl, 6 tbl, 6 ex

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