Method of copper extraction form sulphate containing dust of copper production

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

 

The invention relates to a method of recycling pyrometallurgical processes of non-ferrous metallurgy, containing copper, iron and other metals in the oxidized form, and can be used in the processing solfataras dust copper 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. In addition, when pyrometallurgical processing sulfidogenic dusts leads to the formation of sulfuric anhydride, which when in contact with moist air to form sulfuric acid which destroys the flues. Known methods of hydrometallurgical processing of copper dusts production do not provide high extraction of copper with obtaining high-quality commercial products, due to the presence of dusts significant amounts of iron and other impurity elements, and are also characterized by a large volume of material flows.

The method for extracting copper from copper dust production (see M. Amores, Coedo A. G., Alguacil F. J. Extraction of copper from sulphate solutions by MOC 45: Application to Cu separation from leachates of a copper flue dust // Hydrometallurgy, t, issue 1, 1997, s-112), comprising leaching the dust composition, wt.%: Cu 24,5; Fe 14,0; Zn 0,15; Pb 0,08 aqueous solution of sulfuric acid with receiving the receiving solution leaching, containing 0.26 g/l copper and trace amounts of other metals, as well as the extraction of copper extractant Aksenovo type MOS 45 at the time of contact of phases 20 minutes getting the raffinate and extract, from which were reextraction copper with a solution of sulfuric acid 150 g/l with getting sulfate solution, suitable for copper by electroextraction.

The disadvantage of this method is the very low recovery of copper from dust with obtaining poor metals solutions, leading to the formation of large material flows of reagents. The disadvantages of this method include also not a high degree of extraction of copper from the leaching solution and a long-time contact of the phases due to the low rate of extraction of copper selected extractant.

There is also known a method of extracting copper from sulhamstead dust copper production (see Seeger I.I., Gaganov G.P. Glazunov L.A. and other Extraction the extraction of copper from dusts oxygen torch melting // non-ferrous metallurgy. - 1975. No. 3, p.21-23), comprising leaching the dust of cold water for 45 minutes with respect to T:W=1:5 with the transfer of copper and impurity elements in the leaching solution, separating the solution from the insoluble residue by settling solution, liquid extraction of copper extractant Aksenovo type UMG (2-hydroxy-S-alkyl-alkadiene the oxime is the number of carbon atoms in the alkyl radicals of more than five) to obtain the copper-containing extract and obesogenic of raffinate, containing impurity elements, reextraction copper 20% sulfuric acid, the purification of the obtained reextract from the extractant. Of the purified reextract used as the electrolyte and containing 42,3 g/l copper, conduct the two-stage electrolytic deposition to produce cathode copper containing 99.9% of Cu and circulating electrolyte used for reextraction copper.

The disadvantage of this method is that it also does not provide a high recovery of copper by water leaching without heating and inefficient separation of the solution from the insoluble residue by sedimentation. Of dust in the leaching solution is extracted only 45.4% of copper. The disadvantages of the method can also include a low degree of extraction of copper from leaching solutions without performing intermediate neutralization and the necessity of extraction recovery of the entire copper leached from the dust, which requires cleanup of large volumes of fluids from the impurities of the extractant. Application for extraction reagent UMG having low capacity and selectivity, does not provide a deep separation of copper and iron, resulting in a copper electrolyte contains 1.4 g/l of iron, which limits the reusability of the circulating electrolyte at the stage of Stripping, leads to snizheniya current during electrolysis and contributes to lowering the quality of the cathode metal.

The present invention is directed to the achievement of the technical result consists in obtaining high-quality copper cathode from sulfidogenic dusts copper production, while ensuring a high degree of extraction of copper in the product and reducing the volume of material flows.

The technical result is achieved in that in the method of extracting copper from sulhamstead dust copper production, including water leaching dust with copper and impurity elements in the leaching solution, separating the solution from the insoluble residue, liquid extraction of copper oksimnymi extractant to obtain a copper-containing extract and a raffinate containing impurity elements, reextraction copper, purification of the obtained reextract from the extractant and electroextraction copper to produce copper cathodes and circulating electrolyte according to the invention water leaching of lead dust at a temperature of 60-100°and T:W=1:2-4, the leaching solution is cooled to crystallize the main part of copper sulphate and education of the mother liquor containing residual part of copper sulphate is separated from the mother liquor, dissolving in sulfuric acid solution and serves on electroextraction and liquid extraction is carried out from the mother liquor.

The technical result is also achieved by those who, the extraction of copper, lead from dust copper containing not less than 20 wt.% copper in the form of its sulfate.

On the technical achievement of the aims that the leaching solution is cooled to a temperature of not more than 15°C.

On the achievement of the technical result is also aimed that before cooling the leaching solution evaporated to provide the density of 1.30-1,36 g/cm3.

On the achievement of the technical result is also aimed that out of solution leaching allocate 60-85% copper sulphate.

The achievement of the technical result is driven by the fact that electroextraction lead at a concentration of copper in the electrolyte 30-50 g/l and a cathode current density of 200 to 300 a/m2.

The achievement of the technical result also contributes to the fact that as a sulfuric acid solution to dissolve the sulphate use purified or reextract the circulating electrolyte.

The achievement of the technical result is strengthened by the fact that liquid extraction of the residual part of the copper are using as extractant 20-40% solution Acorga in an inert diluent at a:=3-5:1 2-4 degrees and reextraction perform steps 2-4 using as extragent sulfate solution with a concentration of not less than 120 g/l H2SO4.

On achieving technical resulttemplate the before liquid extraction of the mother liquor is neutralized to a pH of 1.0 to 2.5.

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 water leaching of dust at a temperature of 60-100°and T:W=1:2-4 ensures a high degree of extraction of copper from dust and reduce the amount of recyclable solutions, as well as to prevent crystallization of copper sulfate in the leach process. Lowering the temperature below 60°reduces the degree of extraction of copper, as well as to premature formation of crystals of copper sulphate, which is caused by the dependence of the solubility of copper sulphate on temperature. The temperature increase of more than 100°accompanied by excessive energy consumption for heating of the solution and the risk of boiling the solution. The increase in the content of the solid phase relative to the liquid more than 1:2 leads to deterioration of kinetic characteristics and the difficulty of filtering the insoluble residue. A reduction in the content of the solid phase relative to the liquid below 1:4 leads to an unjustified increase material flow.

Cooling of the leaching solution with the crystallization of mostly copper to the Poros allows you to separate the copper from the main part of the impurities, having a higher solubility of sulfate salts as compared with copper sulfate, concentrating the residual of the impurities in the mother solution.

Department of sulfate from the mother liquor and dissolved in sulfuric acid solution allows to obtain a solution with a minimum content of impurities, suitable for use as electrolyte in obtaining a quality copper cathode through electroextraction.

Conducting liquid extraction from the mother liquor obepechivaet more complete extraction of copper from a solution leaching dust while reducing reagent consumption and minimize the volume of solutions to be cleaned from the remnants of the extractant.

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 sulfidogenic dusts copper production, while ensuring a high degree of extraction of copper in the product due to the higher extract it in the leaching solution and reducing the volume of material flows.

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 20 wt.% copper in the form of its sulfate contributes to the high copper recovery and ensure achival the production of standard copper solutions suitable for efficient crystallization of copper sulfate.

Cooling of the leaching solution to a temperature of not more than 15°contributes to a more complete separation of copper as copper sulphate and reduce its residual content in the mother solution. When the cooling temperature of the leaching solution over 15°in the mother solution remains too high concentration of copper, which complicates its subsequent extraction extraction.

Evaporation of the solution before cooling to ensure the density of 1.30-1,36 g/cm3allows the crystallization of copper sulfate to separate from the solution, the major quantity of copper sulphate and separate it from the main part of 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 increase of iron content in the solution supplied to electroextraction and causes a decrease in output current. In addition, evaporation of the solution to the higher density of 1.36 g/cm3leads to premature crystallization of copper sulfate.

The selection of the leaching solution 60-85% copper sulphate allows you to separate the bulk of the copper from when the Yessei and get the product suitable for subsequent preparation of conditioned copper electrolyte. The selection of the solution is less than 60% copper sulphate leads to unnecessary increase in the volume of material flows and the allocation of more than 85% copper sulphate caused by the contamination of its impurities and, consequently, reduces the quality of the copper electrolyte.

Holding electroextraction copper from sulfuric acid solution of copper sulphate at a concentration of copper in solution 30-50 g/l and a cathode current density of 200 to 300 a/m2provided quality saleable copper cathode brands MOOK at high output current. Holding electroextraction from a solution containing less than 30 g/l of copper, and a current density of less than 200 a/m2degrades 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 of copper and a current density of more than 300 a/m2accompanied by dentatoalatum, reducing the quality of cathode copper.

Use as a sulfuric acid solution to dissolve the sulphate purified reextract or circulating electrolyte reduces the volume of material flows.

The implementation of the extraction of the residual portion of copper using as extractant 20-40% solution Acorga in an inert diluent at a:=3-5:1 2-4 STU is enah provides a high and selective extraction of copper from the mother liquor at the lowest possible flow of reagents in the extraction step. The use of the extractant Acorga provides selective extraction of copper from the mother liquor. The application of this extractant concentration less than 20% does not provide for deep extraction of copper from solution with a concentration of more than 40% affects the hydrodynamics of the extraction process, resulting in increased duration of phase separation during extraction. The implementation of the extraction when On:less than 3:1 does not provide a high copper recovery from the mother liquor, and when a:more than 5:1 leads to an unjustified increase flows of reagents. Single-stage conducting the extraction does not provide the necessary degree of extraction of copper from the mother liquor. The number of stages more than 4 impractical because of the need to use additional pieces of equipment without significantly increasing the degree of extraction of copper.

Holding Stripping 2-4 steps using as extragent sulfate solution with a concentration of not less than 120 g/l H2SO4provides deep copper recovery from the extract and efficient regeneration of the extractant. When the concentration of sulfuric acid of less than 120 g/l and the number of steps of Stripping copper less than 2 not achieved a high degree of Stripping of copper. Conducting the Stripping of copper in more than 4 steps not desirable because of the small increment is and the degree of extraction of copper and increase the number of units.

Neutralization mother liquor before liquid extraction to a pH of 1.0 to 2.5 contributes to increasing the degree of extraction of copper in the extract. Neutralization to a pH of less than 1.0 leads to a decrease in the degree of extraction of copper, and the increase in pH to a value of not more than 2.5 leads to a significant increase in the degree of extraction of copper. In addition, it can cause the formation of the solid phase due to hydrolysis of ferric iron.

The above private features of the invention allow a method in the optimal mode from the viewpoint of obtaining high-quality copper cathode, while ensuring a high degree of extraction of copper in the product and reducing the volume of material flows.

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

Example 1. Dust converting copper matte in the amount of 1 kg, containing, wt.%: Cu 21,8, Fe 2.4 and Ni 0,5 (copper content in the form of sulphate - 80%), leached 2 l of water (T:W=1:2) at a temperature of 100°C for 1 hour with translation copper and impurity elements in the solution. The leaching solution is separated from the insoluble residue by filtration. The degree of extraction in the solution amounted, %: Cu 99,4, Fe 98,9, Ni 95,0. A solution containing, g/l: Cu 108,3, Fe 13,9, Ni 2,0, cooled under stirring for 2 hours to a temperature of 1°with the crystallization of 60% copper sulphate and the image is of the mother liquor. When this occurs the separation of the copper from the main part of the impurity elements. The obtained crystals of copper sulphate is separated from the mother liquor by centrifugation. Copper sulphate containing, wt.%: Cu 24,0, Fe 0,2, Ni of 0.05, dissolved in sulfuric acid solution containing 150 g/l sulfuric acid. The resulting solution is fed to electroextraction, which are at a concentration of copper in the electrolyte 30 g/l and a cathode current density of 300 a/m2by removing the cathode metal 99.5% pure copper. The result is copper cathode mark MOOK with a copper content of 99.99% and circulating the electrolyte, which is directed to the dissolution of copper sulphate or leaching of dust. The current output on electroextraction was 93.5%. The mother liquor composition, g/l: Cu 40, Fe 12,6, Ni 2.1 from pH 0.5 served on liquid extraction, which is carried out by countercurrent using a 40% solution of Acorga 5640 in an inert diluent brand "Escaid" if A:b=3:1 to 2 degrees. The result is the extract containing 12.5 g/l Cu, and a raffinate containing impurity elements and copper in amounts of 2.5 g/l, which is sent for recycling. The degree of extraction of copper in the extract from the mother liquor was 93.8%. Reextraction carried out using as extragent sulfate solution with a concentration of 200 g/l H2SO4if A:b=3:1 to 4 degrees. The contact time of the phases to study the x extraction and re-extraction was 3-5 minutes. The resulting reextract containing 37,2 g/l Cu, after settling purified activated carbon from dissolved extractant and serves on electroextraction.

Example 2. Dust converting copper matte in the amount of 1 kg, containing, wt.%: Cu 31,7, Fe 1.5 and Ni 0,7 (copper content in the form of sulphate - 60%), leached in 4 liters of water (T:W=1:4) at a temperature of 60°C for 1 hour with translation copper and impurity elements in the solution. The leaching solution is separated from the insoluble residue by filtration. The degree of extraction in the solution amounted, %: Cu 95,4, Fe 88,9, Ni 93,0. A solution containing, g/l: Cu 75,6, Fe 3,3, Ni 1,6, evaporated to a density of 1.30 kg/m3and then cooled under stirring for 2 hours to a temperature of 5°with the crystallization of 70% copper sulphate and education of the mother liquor. When this occurs the separation of the copper from the main part of the impurity elements. The obtained crystals of copper sulphate is separated from the mother liquor by filtration. Copper sulphate content, wt.%: Cu 23,6, Fe 0,2, Ni 0,06, dissolved in the circulating electrolyte. The resulting solution containing 120 g/l H2SO4and of 58.8 g/l Cu, served on electroextraction, which are at a concentration of copper in the electrolyte 40 g/l and a cathode current density of 200 a/m2by removing the cathode metal 99.6% of copper. The result is copper cathode mark MOOK with a copper content of 99.99% of the sulfuric acid circulating the electrolyte with a concentration of 120 g/l H 2SO4, 70% of which is directed to the dissolution of copper sulphate. The current output on electroextraction amounted to 91.5 per cent. The mother liquor composition, g/l: 42 Cu, Fe 4,6, Ni 1,7, neutralized with soda solution to a pH of 1.0 and served on liquid extraction, which is carried out by countercurrent using a 20% solution of Acorga 5640 in an inert diluent brand "Escaid" if A:B=5:1 to 2 degrees. The result is the extract containing 8 g/l Cu, and a raffinate containing impurity elements and copper in the amount of 2.0 g/l, which is sent for recycling. The degree of extraction of copper in the extract from the mother liquor was 95%. Reextraction carried out using as extragent the residual sulfuric acid circulating electrolyte when A:B=1:2 on 2 levels. The contact time of the phases on the stages of extraction and re-extraction was 3-5 minutes. The resulting reextract containing 53,6 g/l Cu, after settling purified activated carbon from dissolved extractant and serves on electroextraction copper.

Example 3. Dust from roasting of copper concentrate in the amount of 1 kg, containing, wt.%: Cu 40,1 Fe 3.6 and Ni 2,8 (copper content in the form of sulphate - 20%), leached of 2.8 l of water (T:W=1:3) with the addition of 0.2 l circulating electrolyte at a temperature of 90°C for 1 hour with translation copper and impurity elements in the solution. The leaching solution is separated from nerastvorim the residue by filtration. The degree of extraction in the solution amounted, %: to 72.4 Cu, Fe 68,9, Ni 63,5. A solution containing, g/l: Cu 96,6, Fe 8,3, Ni 5,9, evaporated to a density of 1.36 kg/m3and then cooled under stirring for 2 hours to a temperature of 15°with the crystallization of 85% copper sulphate and education of the mother liquor. When this occurs the separation of the copper from the main part of the impurity elements. The obtained crystals of copper sulphate is separated from the mother liquor by centrifugation. Copper sulphate containing, wt.%: Cu 21,6, Fe 0,5, Ni and 0.08, dissolved in purified reextract. The resulting solution containing 120 g/l of sulfuric acid and 62.2 g/l copper, serves on electroextraction, which are at a concentration of copper in the electrolyte 50 g/l and a cathode current density of 250 a/m2by removing the cathode metal 99.5% pure copper. The result is copper cathode mark MOOK with a copper content of 99.99% and circulating the electrolyte, 10% of which is used as an additive in aqueous leaching dust, and 90% are sent to reextraction copper. The current output on electroextraction made 90.5%. The mother liquor composition, g/l: Cu 45, Fe 14,6, Ni 10,4, neutralized with soda solution to a pH of 2.5 and served on liquid extraction, which is carried out by countercurrent using a 30% solution of Acorga 5640 in an inert diluent brand "Escaid" if A:b=3:1 to 4 degrees. The result is the extract containing 1.6 g/l Cu, and the raffinate containing impurity elements and copper in the amount of 1.0 g/l, which is sent for recycling. The degree of extraction of copper in the extract from the mother liquor was 95%. Reextraction carried out using as extragent the residual sulfuric acid circulating electrolyte when A:B=1:2 on 2 levels. The contact time of the phases on the stages of extraction and re-extraction was 3-5 minutes. The resulting reextract containing 57.6 g/l Cu, after settling purify the activated carbon from the extractant and serves on the dissolution of copper sulphate.

From the analysis above examples show that the proposed method can be obtained from sulhamstead dust copper production of high quality copper cathode mark MOOK with access to commercial products up to 98% of the copper contained in the dust, at high (90,5-93,5%) output current. Using the proposed method of concentrated copper solutions and selective extractant reduces the volume of material flows and deep separation of copper from impurity elements. The proposed method can be implemented using commercially available reagents and standard equipment.

1. The method of extracting copper from sulhamstead dust copper production, including water leaching dust with copper and impurity elements is found in the leaching solution, the separation of the solution from the insoluble residue, liquid extraction of copper oksimnymi extractant to obtain a copper-containing extract and a raffinate containing impurity elements, reextraction copper, purification of the obtained reextract from the extractant and electroextraction copper to produce copper cathodes and circulating electrolyte, characterized in that the water leaching of lead dust at a temperature of 60-100°and T:W=1:2-4, the leaching solution is cooled to the crystallization of the main part of copper sulphate and education of the mother liquor containing residual part of copper sulphate is separated from the mother liquor, dissolving in sulfuric acid solution and served on electroextraction and liquid extraction is carried out from the mother liquor.

2. The method according to claim 1, characterized in that the extraction of copper, lead from dust copper containing not less than 20 wt.% copper in the form of its sulfate.

3. The method according to claim 1, wherein the leaching solution is cooled to a temperature of not more than 15°C.

4. The method according to claim 1, wherein prior to cooling the leaching solution evaporated to provide the density of 1.30-1,36 g/cm3.

5. The method according to claim 1, characterized in that the leaching solution allocate 60-85% copper sulphate.

6. The method according to claim 1, characterized in that electroextraction lead at the end of the ation of copper in the electrolyte 30-50 g/l and a cathode current density of 200 to 300 a/m 2.

7. The method according to claim 1, characterized in that as a sulfuric acid solution to dissolve the sulphate use purified or reextract the circulating electrolyte.

8. The method according to claim 1, characterized in that the liquid extraction of the residual part of the copper are using as extractant 20-40%solution Acorga in an inert diluent at a:=3-5:1 2-4 degrees and reextraction perform steps 2-4 using as extragent sulfate solution with a concentration of not less than 120 g/l H2SO4.

9. The method according to claim 1, characterized in that before the liquid extraction of the mother liquor is neutralized to a pH of 1.0 to 2.5.



 

Same patents:

FIELD: metallurgy.

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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

FIELD: metallurgy.

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1 dwg, 1 tbl, 1 ex

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1 tbl

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FIELD: non-ferrous metallurgy; re-working of lead-containing wastes.

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7 tbl, 1 ex

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FIELD: metallurgy of non-ferrous metals.

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5 cl, 1 tbl, 1 ex

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%.

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10 cl, 4 ex

FIELD: chemistry.

SUBSTANCE: invention can be used for production of high-purity silicon dioxide within integrated processing of magnesium-chrome crude ore that is mixed serpentinite, chromite, pyroxene and other minerals. Method of integrated processing of magnesium-chrome crude ore includes as follows. Crude ore is decomposed by solution of mineral acids. Produced suspension is filtered, and insoluble residue is processed. Filtrate neutralisation is accompanied with sedimentation of contained metal hydroxides with washing and drying of produced end-products. Processing of insoluble residue includes annealing at temperature 350-600°C, following dissolution in caustic soda to residual alkalinity 40-60 g/l NaOH, filtering of prepared suspension, washing of residue that is chrome ore concentrate and sedimentation of silicon dioxide from produced filtrate with solution of hydrochloric acid to residual acidity 2-15 g/l HCl.

EFFECT: higher separation integrity of silica component with simultaneous integrated extraction of other components of crude ore that provides extended application of base mixtures.

6 tbl, 2 ex

FIELD: metallurgy.

SUBSTANCE: invention concerns industrial sanitation and environmental protection field, at usage in manufacturing and in domestic conditions of metallic mercury, its containing devices and facilities, and also of amalgams, and is intended for neutralisation of mercury at its ingress both on surfaces of different materials and into volumes (material, brick, concrete and so forth). Neutralisation technique of metallic mercury by immobilisation includes its oxidation by means of treatment by water solution of hydrogen peroxide. At that additionally to oxidation it is implemented mercury deposition by means of simultaneous or successive treatment by water solution of reagent, transferring metallic mercury into insoluble or sparingly soluble in water compound of natural or anthropogenic composition. In the capacity of reagent there are used water-soluble compounds of alkaline or alkaline-earth metals for instance, sulphates, phosphates or carbonates.

EFFECT: effectiveness increase of process at excluding of mercury - organic compounds formation.

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: 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

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