Method of extraction of nonferrous and noble metals, mainly copper and gold, from sulfur waste

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

 

The invention relates to hydrometallurgy of non-ferrous and precious metals, mainly copper and gold from the pyrite Ogarkov, which is the waste sulfuric acid production, and can be used in heap, cuvette and percolation leaching.

At the present time, neither the domestic nor the foreign practice of gold mining there is no effective technology to extract precious metals from the pyrite slag, a waste sulfuric acid production.

Known for numerous publications, dedicated to the extraction of non-ferrous and precious metals from pyrite Ogarkov.

So, according to I. N. Plaksin. and Zyryanov mathematical SCIENCES. Complex processing of lead-zinc raw materials. M., 1963, ed. Academy of Sciences of the USSR, p.78-79, the most common way of processing pyrite Ogarkov is gloriously roasting with salt and subsequent percolation leaching. To this end, the cinder mixed with sodium chloride and subjected to firing. Kiln gases in contact with water to give a mixture of hydrochloric and sulfuric acid used for leaching polarisavenue cinder, extracting the solution of copper, zinc, sulfate and sodium chloride, recyclable known precipitation and cementation methods.

To extract the remaining gold iron KEK treatment is with chlorine water and produce gold from solution by cementation.

In the same book (s) shows another variant of the preparation of pyrite Ogarkov to percolation leaching with the use of burning in the presence of sulfuric acid, after which conduct water leaching converted to a soluble state of copper, zinc and iron. After solution treatment from these elements neutralization in stage 2 extract gold and silver cyanidation.

The main disadvantages of the proposed methods are increased energy costs associated with conducting firing, the use of toxic chemicals - chlorine and cyanide, the complexity and multi-stage processing pyrite Ogarkov and his increased environmental hazard.

Well-known canadian patent No. 827063 from 11.11.69 "Method of extracting gold from the pyrite Ogarkov, whereby the pyrite cinder glorieuses or sulfatides firing is subjected to air oxidation in the presence of steam and oxidized material is leached with an aqueous solution having an optimal concentration of chlorine. The disadvantages of this method are the increased energy costs and environmental hazard when using chlorine.

In the book Meretukov M.A. metals precious metals. Foreign experience. M.: metallurgy, 1991, p.222-223 described method hydrolytic processing of pyrite Ogarkov, developed at the Barcelona University (Spanish is I), according to which the slurry pyrite Ogarkov introducing chlorine gas at ordinary temperature and pressure, at a pH of 2.5-3.0 precipitated soluble iron lime, from the clarified solution recovered gold and silver on iron scrap, and at pH 9.5 to precipitate the zinc.

In the same book (s) describes the method of leaching pyrite Ogarkov, which are crushed before -0,06 mm, is treated with a solution of sulfuric acid 150 g/l at a temperature of C and remove arsenic, copper, zinc and iron, and the filter cake is treated with thiocarbamide 40 g/l for the dissolution of gold and silver, using as oxidant air. Consumption of thiocarbamide is 6.6 kg/so

In A.S. No. 1486534 the USSR, MKI SW 19/24, 15/10 copper and zinc from pyrite cinder remove water-ammonia solution in the presence of iron pyrites. However, noble metals are not removed.

Known to extract silver and gold from the pyrite Ogarkov acid thiosulfate solution, followed by cementation of precious metals zinc dust: t=70°C, the concentration of thiosulfate ion 10-30 g/l, pH of 1.5-2.0, but how difficult to implement on a large scale due to the decomposition of thiosulfate (Beliavsky M.A. Behavior of gold and silver thiosulfate and sulfide environments with regard to the processing of Ogarkov. Author's abstract on competition of a scientific degree of candidate of technical Sciences. MISA. the., 1988).

Known patent No. 1790230 SU, IPC6SW 7/00 "Method for integrated processing of pyrite Ogarkov, whereby pyrite cinder from roasting iron pyrites Rasulova water and leached with a weak solution of sulphuric acid, while the flow of the pulp is divided into two parts. In the first part of the metered sulfuric acid and leached for 0.5 hour. The solution is separated from the calcine and separated from his non-ferrous metals, and the calcine is treated with hydrochloric acid solutions of thiocarbamide and extracted with this noble metals.

Among the disadvantages of this method include the increased cost of sulfuric acid and thiocarbamide.

The closest in technical essence to the proposed method is "a Method for integrated processing of pyrite Ogarkov" (patent No. 1669193 SU, IPC7SW 3/44, 15/00, 19/00), according to which, in solution, the last three stages of leaching water, dispense sulfuric acid to a pH of 1.8-2.0, from the clarified solution allocate cementation on iron scrap blister copper when the value of redox potential (ORP) 0-(-80) mV, separating the precipitate, increase the value of the redox potential of the solution to 600-700 mV and dispense soda to achieve a pH of 6.0, separating the precipitate and subjecting it to heat treatment to obtain iron pigment; from the clarified solution by means of precipitation with soda at pH 7.8 separation of the Ute zinc carbonate, and cinder is treated with hydrochloric acid solutions of thiocarbamide and extracted with this noble metals.

The disadvantages of the prototype should include a multi-stage process, the presence of sludge operations solutions, increased consumption of thiocarbamide and lack of sustainability of the process.

The problem to which the invention is directed, is to develop a method of leaching copper and gold from the pyrite slag, a waste sulfuric acid production.

The technical result of the proposed technical solution is the reduction of specific consumption of chemicals, energy costs and increase the degree of extraction of copper and gold.

The technical result is achieved in that in the method of leaching of non-ferrous and precious metals from pyrite Ogarkov, including the formation of anti-filtration of the base, filling it dump pyrite Ogarkov, the flow in the blade of solutions of sulphuric acid leaching, separation of non-ferrous metals and subsequent processing Ogarkov acidic solution of thiocarbamide the presence of an oxidant formed by the blade pyrite Ogarkov is exposed to atmospheric precipitation in the process of maturation, which leads to the formation of sulfuric acid and ferric ions, gather sour wastedump water and their pH value in the range of 1.5-1.8 used for videla the air traffic management non-ferrous metals, mainly copper, or add in wastedump water acid to these values, providing the pH and Eh of productive solutions in the intervals of 2.0-2.5 and 500-540 mV, respectively, separated from the resulting solution the copper cementation, aeronaut manifold cementation and use them for cooking leach solution, and after reaching the copper concentrations less than 100 mg/l reduce the amount of oxidizer and acid in the leaching solution, give it a thiocarbamide, leached precious metals, mainly gold, with the pH and Eh, defined by the region of stability of gold thiocarbamides complex and the minimum value necessary to keep the gold in the solution, respectively, and found empirically, and recovered gold cementation. As oxidant at thiocarbamide leaching ions are used Fe3+the concentration of thiocarbamide support in the interval 0.2-0.5 g/l, for the deposition of copper and gold is the use of substances, selected from the series: iron scrap, scrap, powder, iron ingots, sponge iron.

For cementation of gold can be used cement residue from the stage of deposition of copper.

The proposed method is as follows. Pyrite cinder sulfuric acid containing soluble forms of the compounds dohwa entogo iron and insoluble ferric oxides and magnetite in an acidic environment, store the prepared anti-filtration substrate and is exposed to atmospheric precipitation. The purpose of this impact is the maximum translation of divalent iron compounds in the ferric oxyhydrate gels due to their oxidation by the oxygen of the air entering the blade together with precipitation and subsequent dissolution of the generated acidic solutions of sulfuric acid and the use of ions of Fe3+for additional dissolution of oxidized copper sulfides contained in the raw material.

The chemical process of oxidation that occurs in the stubs can be described by the following reaction equations:

When infiltration of precipitation through the blade there is an interaction generated sulfuric acid according to reaction (2) with stubs for reactions (3) and hydrolysis of the resulting sulfate Fe3+upon reaching the pH of the solution ≥3.0 precipitation of the hydroxide of Fe3+:

thus formed according to reaction (5) the acid is spent on interaction with soluble oxides blade Ogarkov.

As the studies of the blade formed by the acid and acidification resulting from under negatives the water, containing ions of Fe2+, the oxidation of Fe2+to Fe3+that is accompanied by increasing the value of Eh collect water and intensifies the process of dissolution of copper. Upon reaching the pH of the collected water in the range of 1.5-1.8 they are used for the leaching of non-ferrous metals, mainly copper, thus regulate the process so that the pH value of the obtained production solutions was in the range of 2.0 to 2.5, which allows with minimal cost acid transfer into a solution of oxidized copper compounds:

and when the cementation of copper to reduce the consumption of iron scrap on adverse reactions:

For additional translation in the solution of sulphide of copper compounds in the production solutions it is necessary to maintain the value of Eh in the range of 500-540 mV.

This is achieved by the fact that the mother solution after cementation of copper, having a pH of 2.4-2.8 and containing Fe2+2-4 g/l, is subjected to aeration, which leads to the oxidation of Fe2+in Fe3+and increase the Eh values to values 600-650 mV, which is sufficient for oxidation of sulfide copper compounds by the reaction:

Maintaining the value of Eh in the final solution in the range of 500-540 mV, provide for extraction of the honey is at the level of 86-88%. In the absence of the effects of rainfall on the blade pyrite cinder resulting from the extraction of copper does not exceed 80%.

In addition, when values of Eh in the final solution is not more than 540 mV also reduces the consumption of iron scrap and reduced reverse the dissolution of the formed cement copper:

If wastedump waters do not reach pH values in the range of 1.6-1.8, they additionally acidified to these values and is directed to the irrigation of the blade and the leaching of copper.

Solutions after aeration is used to prepare leach solution.

Obtained by leaching Ogarkov production solutions containing, g/l: Cu2+0.6-1.2; Fe3+0.5-1.0, sent for cementation of copper metal scrap:

Reaction (12) is accompanied by an increase in the content of iron ions to 2-4 g/l

Dedicated copper catch in the cascade of tanks and mortars cementation aeronaut and is directed to the preparation of leach solutions.

When reaching the copper concentrations in the final solutions of less than 100 mg/l reduce the amount of acid and oxidant in the leaching solution, give it a thiocarbamide in the amount of 0.2-0.5 g/l and is sent to the leaching of gold:

This and the interval of concentrations of thiocarbamide selected because which, as demonstrated by laboratory studies, when the concentration of thiocarbamide less than 0.2 g/l extraction and dissolution rate of gold is sharply reduced, and when its concentration is more than 0.5 g/l increases the unproductive consumption of thiocarbamide in connection with the formation of thiocarbamide complexes, passed into a solution of metals and additional oxidation of its salts of Fe3+.

Restriction on the content of copper in the solutions entering the leaching of gold, less than 100 mg/l due to the fact that when thiocarbamide the process of dissolution of noble metals, copper at a concentration in solution of more than 100 mg/l forms with thiocarbamide insoluble complex Cu[CS(NH2)2]3SO4that leads to loss of thiocarbamide and reduce the degree of extraction of gold from Ogarkov. In addition, elevated concentrations of copper in solution contribute to the destruction of thiocarbamide and the formation of gelatinous compounds able to reduce the extraction of gold and degrade the filtration properties of the blade up to a full stop filter.

The decrease in the concentration of acid contributes to the loss of part of Fe3+in the sediment to the minimum sufficient to leach the gold level, which reduces the consumption and loss of gold on the grouting operation.

When necessary, the pH of the solution is determined by the area of the mouth is echeveste thiocarbamides complex, and the Eh value - minimum value necessary to keep the gold in solution.

In turn, specific optimum values of pH and Eh in the leaching of gold set empirically depending on the phase composition of Ogarkov and determined by thermal oxidation firing the source of sulfide-bearing raw materials.

So, depending on the firing temperature of sulfide-bearing raw materials, such as pyrite, in an oxidizing atmosphere, you may receive the following reaction products:

As can be seen from the above reactions, depending on the temperature of the oxidative roasting of the reaction products can be salts and oxides of divalent iron oxides ferric Fe2O3and the mixed oxides of basicity of Fe3O4that requires different values of pH and Eh of the solution during the leaching of gold.

The final stage of the leaching of gold is removed from production solutions by cementation, which is carried out with the use of the substances chosen from the series: iron scrap, scrap, powder, iron ingots, sponge iron or cement sludge from the stage OS the statement of copper.

The use of a separate scheme of extraction of non-ferrous and precious metals from waste dumps pyrite Ogarkov on the place of storage allows you to extract up to 88% copper and up to 71% of gold.

The inventive method is illustrated by the following examples.

The feasibility of processing pyrite Ogarkov precipitation during maturation illustrates the example 1.

Example 1

Stockpiled pyrite and pyrite cinder cinder current storing, containing, %: copper 0.1; zinc 0,4; iron oxide (III) 49,4; silicon oxide 8,4; total sulfur 3,2; gold 1.4 g/g, was loaded into percolator respectively, and pass through them in infiltration mode aerated water, simulating precipitation, up to the value W:T=1 at a steady speed of water flow 2 l/h m2. Defined process parameters and their values are given in table 1.

As can be seen from table 1, all the pH and Eh of the solution obtained by leaching stockpiled pyrite Ogarkov precipitation, preferably by comparison with leaching from slag, a waste of the current storage.

The feasibility of maintaining a pH in the range 2.0 to 2.5 in solutions flowing out of the blade, is illustrated in example 2.

Example 2

Stockpiled pyrite cinder composition of example 1 under similar conditions was treated with arrowanas water with the addition of sulfuric acid in quantities providing pH 1,5; 2,0; 2,5; 3,0 output from percolator. Indicators analyzed and the results of the determinations are given in table 2

Table 2
The results of leaching stockpiled pyrite Ogarkov solutions of different acidity
The analyzed indicatorsIndicators at the output of percolator at values of pH
1,52,02,53,0
Eh, mV525516500380
copper:
zinc:
The consumption of sulfuric acid, kg/t2015,114.4V12,3

As you can see from the data is x 2, lower pH values of the solution at the outlet of percolator correspond to elevated concentrations of copper and zinc and their degree of extraction with higher consumption of acid.

Optimal pH values at the exit of percolator, allowing to obtain approximately the same extraction of copper and zinc compared with the interval of pH values of 1.5, is an interval of 2.0-2.5. In the claimed range of pH values the consumption of sulfuric acid 25% lower than in the range of pH values+1.5. Similar results were obtained when using as the leach solution is collected sour wastedump water when their pH value in the range of 1.5-1.8.

The feasibility of maintaining the values of Eh values in the production fluids flowing out of the blade, more than 500 mV illustrates an example 3.

Example 3

Stockpiled pyrite cinder composition of example 1 was treated with aerated water containing sulfuric acid so that at the exit of percolator the Eh value was 300, 400, 500, 600 mV, respectively. Indicators analyzed and the results of the determinations are given in table 3.

Table 3
The dependence of the degree of extraction of non-ferrous metals from stockpiled pyrite Ogarkov acidic solutions with the ranks Eh
The analyzed indicatorsIndicators at the output of percolator when values of Eh of the solution, mV
300400500550600
pH2,02,02,02,02,0
copper
zinc
Acid consumption kg/tthe 15.615,315,114,914,7

As can be seen from table 3, the increase of the values of Eh in the solutions coming out of percolator, promotes increased recovery of both copper and zinc. For copper, this dependence is more significant. When the value is s Eh more than 500 mV, the degree of extraction of copper increased slightly, i.e. the optimal interval Eh is 500-550 MB.

The dependence of the filtration properties of the blade stockpiled pyrite cinder resulting from the residual concentration of copper in the solutions at thiocarbamide gold leaching illustrates an example 4.

Example 4

Stockpiled pyrite cinder composition of example 1 was videlacele in percolator to a residual concentration of copper in a solution of 10.0 mg/l and treated sour thiocarbamide solutions containing 25, 50, 100, 150 mg/l Cu2+accordingly, in the presence of Fe3+. The value of W:T leaching of gold 3.0. The analyzed parameters and results of the determinations are presented in table 4.

Table 4
The dependence of the filtration properties of stockpiled pyrite cinder resulting from the concentration of copper in the leach solutions at thiocarbamide leach
The analyzed indicatorsLeaching thiocarbamide solution containing Cu2+mg/l
2550100150
Specific pickup pls, l/m2B5,05,0a 4.92,0
The content of Cu2+in solutions at the output of p is rolator, mg/l32,058,095,0100,0

As can be seen from table 4, the increase in the concentration of copper in the leach solutions over 100 mg/l reduces the specific pickup feed pls 2.5 times with a simultaneous decrease in the concentration of copper in solution, due to the advent of gelatinous products of the decomposition of thiourea, characterized by high viscosity and reduces the filtration rate of the solution, and the formation of insoluble compounds of copper with thiocarbamide.

The feasibility of maintaining the concentration of thiocarbamide in the range of 0.2-0.5 g/l illustrates an example 5.

Example 5

Stockpiled pyrite cinder composition of example 1 was treated in percolator to a residual content of copper 10.0 mg/l and videlacele gold sour thiocarbamide solutions in the presence of Fe3+.

The concentration of thiocarbamide 0,1; 02; 0,5; 0,6; 1,0 g/l, respectively, the Value of W:T=3.

Indicators analyzed and the results of the determinations are given in table 5

Table 5
The degree of extraction of gold and specific consumption of thiocarbamide concentration of thiocarbamide in the leaching solution
Analiziruyushchei The concentration of thiocarbamide in the leaching solution, g/l
0,10,20,50,61,0
Leachate solution: Eh 390 mV; pH of 2.7
The degree of extraction of gold, %14,265,770,471,071,1
Specific consumption of thiocarbamide, kg/g of gold1,510,651,521,823,02

As can be seen from table 5, the optimal concentration range of thiocarbamide leaching Ogarkov is in the range of 0.2-0.5 g/l, specific consumption is 0.65-1.52 kg/g of gold. Further increase in the concentration of thiocarbamide, almost without increasing the degree of extraction of gold, leads to its significant expense.

The potential for leaching of gold from pyrite Ogarkov after extraction of copper and zinc illustrates example 6.

Example 6

Stockpiled pyrite cinder and cinder current storage after extraction of copper and zinc was treated with acidic thiocarbamide solutions in the presence of oxidant-Fe2(SO4)3and without it. The concentration of thiocarbamide - 0,56 is/l, the value of W:T=3. The analyzed parameters and results of the determinations are presented in table 6.

328,5
Table 6
The results of the leaching of gold from pyrite Ogarkov
Leaching solutionWith Au, ug/lExtract, %
Pyrite cinder current storage
Leachate solution:
the thiocarbamide - 0.5 g/l;
pH 2.0 to 2.5;303,365,4
Eh 520 mV;
Fe2(SO4)3- 3.0 g/l
Leachate solution:
the thiocarbamide - 0.5 g/l:
pH 2.0 to 2.5;12,22,6
Eh 310 MB
Stockpiled pyrite cinder
Leachate solution:
the thiocarbamide - 0.5 g/l;
pH 2.0 to 2.5;? 7.04 baby mortality
Eh 520 mV;
Fe2(SO4)3- 3.0 g/l
Leachate solution:
the thiocarbamide - 0.5 g/l:
pH 2.0-2.5;105,722,6
Eh 180 mV

As can be seen from table 6, the presence of an oxidant - Fe3+promotes the leaching of gold from pyrite Ogarkov. The absence of Fe3+significantly reduces the concentration of gold in solution, and the extraction of gold from stale Ogarkov significantly higher than that of the Ogarkov current storage that is associated with the conversion of compounds of Fe3+in Fe3+in the storage process and the effects of rainfall on the dumps pyrite Ogarkov.

Thus, the above examples clearly show the advantages of the proposed solution and the possibility of its practical implementation.

1. The method of extraction of non-ferrous and precious metals, mainly copper and gold from the pyrite Ogarkov, including the leaching of non-ferrous metals, separation of non-ferrous metals from solution and subsequent leaching of precious metals from slag, a waste acid is astorm of thiocarbamide in the presence of an oxidant, characterized in that before the leaching of non-ferrous metals construct anti-filtration base form therein a blade pyrite Ogarkov, gather formed under the influence of precipitation in the process of maturation of the blade acidic solutions containing sulfuric acid and ferric ions, and the pH value in the range of 1.5-1.8 use them for leaching of non-ferrous metals or add in wastedump water acid to the same pH values, providing the pH and Eh of productive solutions in the intervals of 2.0-2.5 and 500-540 mV, respectively, precipitated from the resulting production of solutions of copper cementation, aeronaut manifold grouting and after reaching the concentration of copper in the final solutions of less than 100 mg/l reduce the amount of oxidizer and acid in the leaching solution, give it a thiocarbamide, leached precious metals, mainly gold, with the pH and Eh, defined by the region of stability of gold thiocarbamides complex and the minimum value necessary to keep the gold in solution, respectively, and recovered gold cementation.

2. The method according to claim 1, characterized in that as the oxidant used ferric ions.

3. The method according to claim 1, characterized in that the concentration of thiocarbamide support in the interval 0.2-0.5 g/is.

4. The method according to claim 1, characterized in that for the cementation of gold used cement residue from the stage of deposition of copper.



 

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10 cl, 2 ex

FIELD: metallurgy.

SUBSTANCE: method includes oxidising roasting, copper cinder leaching in circulating electrolyte, compartment of leaching residual, electroextraction of copper from leaching solution. At that leaching residual in the form of thickened underflow is effected to foam separation with concentrate extraction of precious metals, and chambered product, containing in preference nonferrous materials. Chambered product is reprocessed for secondary nis matte. Electrolyte part after copper electroextraction is separated and effected to evaporation till concentration of sulfuric acid 250-300 g/l, copper vitriol is extracted from it by crystallisation, and sulfuric acid by extraction and it is returned to leaching of copper cinder. Raffinate after acid extraction, containing nickel in preference, is directed to nickel manufacturing. Concentrate of precious metals is directed to refining.

EFFECT: reduction of expenditure of energy and material cost and increasing of receiving materials extraction.

1 dwg, 1 tbl, 1 ex

FIELD: metallurgy.

SUBSTANCE: group of inventions concerns composition and method for metal extraction from solution. Composition contains one or more orthohydroxiarilaldoximes and one or more orthohydroxiarilketoximes, and also one or more equilibrium modifier in quantity providing modification extent of presented orthohydroxiarilaldoximes from preliminary 0.2 till 0.61. Equilibrium modifiers correspond alkylphenols, alcohols, esters, alkyl oxides and polyether, carbonate, ketones, nitriles, amides, carbamates, sulfoxides, or amine salts and quaternary ammonium compound. At that one or more equilibrium modifier are chosen from group 2,2,4-trimethyl-1,3-pentanediolmonoisobutyrate, 2,2,4- trimethyl-1,3-pentanedioldibenzoate, dibutyladipate, dipenthyladipate, dyhexyladipate, isobutylheptylketone, nonanon, 2,6,8-trimethyl -4-nonanon, diundecylketone, 5,8-diethyldodecane-6,7-dion, tridecanol and nonyl phenol.

EFFECT: increasing of metals extraction ratio.

11 cl

FIELD: metallurgy.

SUBSTANCE: invention concerns copper hydrometallurgy by extraction method from sulfuric solutions by organic extractants, and elecro extraction. Particularly from solutions of ore leaching by means of dense, subterranean and vat method and also from concentrates, dumps, sledges, slugs etc. Method for copper extraction from sulfuric solutions, containing copper ions and ions of ferrous iron includes treatment of solution by oxidant containing active oxygen forms, and copper extraction by 2-3 stages by blending of treated copper-bearing solution with solution of organic cation-exchange extractant. After extraction it is implemented mixture separation by sedimentation with receiving copper-bearing extract and raffinate. Copper re-extraction from extract is implemented by 1-2 stages of extract blending with solution of sulfuric acid or treated electrolyte with further separation of mixture by sedimentation with receiving re-extract and extractant solution. From re-extract it is implemented re-extraction of copper with receiving of cathode copper and spent electrolyte.

EFFECT: reduction of extractant consumption, increasing of copper extraction selectivity, increasing of cathode copper quality.

8 cl, 2 ex

FIELD: metallurgy.

SUBSTANCE: invention concerns copper hydrometallurgy. Particularly it concerns method for copper extraction received, for instance, ore leaching by means of dense, subterranean and vat method and also from concentrates, dumps, sledges, slugs etc. Method for copper extraction from sulfuric solutions includes extraction at blending of sulfuric solutions with solution of cation-exchange organic selective extractant and further separation of mixture by means of sedimentation with receiving of copper-bearing extract and extraction raffinate. Copper re-extraction from extract is implemented by means of blending extract with solution of sulfuric acid cwith further separation with receiving of copper-bearing extract extractant solution. Then it is implemented cleaning of re-extract by flotation with further filtration or coalescing and electro extraction of copper from clean re-extract with receiving of cathode copper and spent electrolyte. Spent electrolyte is used for copper re-extraction.

EFFECT: decreasing of sulfuric acid consumption, increasing of copper extraction, decreasing of copper losses with spent solutions, improving of cathode copper.

11 cl, 2 ex

FIELD: metallurgy.

SUBSTANCE: invention concerns hydrometallurgical manufacturing and can be used at bioleaching of sulphide products, containing various nonferrous and precious metals. Method of sulphide-bearing ore treatment includes ore leaching stacked on the watertight basis, located at slope, in heap has a form of rustum of pyramid. Leaching is implemented by means of sulfuric acid solution at concentration 2-10 g/l, containing ions of ferric iron by concentration 1-20 g/l, iron-oxidizing bacteria with microelements and sulphur-oxidizing bacteria. After collection of flowing out solution it is implemented iron regeneration in collected solution in separate instrument by immobilized on neutral bearer bacteria with aeration by air. Metals extraction is implemented from leaching solution.

EFFECT: increasing of metals extraction ratio, decreasing of treatment time.

4 cl, 2 ex

FIELD: metallurgy.

SUBSTANCE: method includes mixing of source concentrate with calcium oxide CaO and calcium peroxide CaO2 and burning in two stages. At the first stage burning is carried out at temperature of 350-500°C within 30-40 minutes, at the second stage - at temperature of 500-800°C during 30-60 minutes. After burning there is performed leaching of non-ferrous metals out of cinder. Consumption of calcium oxide CaO is 50-100% from stoichometric required for binding sulphur into gypsum while consumption of calcium peroxide CaO2 is 1-10% from concentrate weight.

EFFECT: increased extraction of non-ferrous metals and reduced duration of cinder leaching.

2 cl, 2 tbl, 2 ex

FIELD: metallurgy.

SUBSTANCE: before leaching ore is broken and ground to size of 60-70% not more, than 3.0 mm. Leaching of ore is carried out in vats at mixing within 60-120 min with solution of sulphuric acid of primary concentration 10-40 g/l and solid phase contents 50-70%. While leaching during the first 40 minutes concentration of sulphuric acid is maintained within limits of not less, than 10 g/l. After completion of leaching solid and liquid phases are separated and copper is extracted out of leaching liquid phase.

EFFECT: increased extraction of copper out of ore and leaching kinetics and reduction of sulphuric acid consumption and duration of leaching.

6 cl, 6 tbl, 5 ex

FIELD: metallurgy.

SUBSTANCE: method includes breaking and grinding of ore to size of not more, than 0.074 mm, and collective flotation of sulphide and oxidised copper minerals into collective flotation concentrate. After dehydration of concentrate there is performed leaching and mixing with participation of oxygen containing ecologically harmless oxidant at contents of solid phase of 10-50% in water solution of sulphuric acid of 10-80 g/dcm3 concentration at temperature 20-70°C and at presence of trivalent iron ions of 2.0-15.0 g/dcm3 concentration. Cake of leaching is dehydrated and washed, after what liquid phase of leaching is merged with cake washing water. Further merged solution is clarified and copper is extracted out of merged solution thus producing cathode copper.

EFFECT: increased extraction of copper and depth of ore processing; producing commercial output in form of cathode copper and increased ecological compatibility.

11 cl, 2 ex

FIELD: metallurgy.

SUBSTANCE: method includes dry breaking and grinding of ore to size of not more, than 1.0-4.0 mm, ore leaching and mixing, when contents of solid phase is 50-70% with solution of sulphuric acid of 10.0 to 40 g/dcm3 within 0.5-2.0 hrs. After leaching generated cake is dehydrated, washed, subject to neutralisation and crushed to size of 60-95% class - 0.074 mm. Flotation of copper minerals with production of flotation concentrate is carried out. Solution after leaching of ore and cake wash water are merged and freed from solid suspension; then cathode copper is extracted out of them.

EFFECT: reduced consumption of sulphuric acid and water for process; increased extraction of copper out of ore and upgraded quality of consumer products.

8 cl, 2 ex

FIELD: metallurgy.

SUBSTANCE: method of vat bacterial leaching consists in leaching of crumbled, sulphide containing product in water solution of sulphuric acid at value of pH 1.5-2.0 and temperature 10-40°C. Leaching is carried out at presence of ions of trivalent iron of concentration 5-20 g/l, iron oxidizing bacteria of concentration 105 kl/ml and microelements aerated with gas mixture of air and ozone. Contents of ozone in gas mixture are at amount of up to 0.01 vol %. Leaching solution is divided into solid and liquid phase.

EFFECT: upgraded degree of metal extraction out of sulphide containing product and accelerated rate of leaching.

3 cl, 2 ex

FIELD: metallurgy, mining.

SUBSTANCE: method for gold extraction from cyanic pulp includes gold sorption by means of pulp directing to ion-exchange resin by backflow in cascade of appliances. At that sorption is implemented at the control of concentration of gold in pulp liquid phase of each appliance. At reduction of gold concentration till 0.9 mg/l it is implemented extraction of resin from appliance and its regeneration by solution of caustic soda and/or sodium chloride brine.

EFFECT: increasing of resin sorptive capacity and extraction increasing of solute gold.

2 cl, 2 tbl, 1 ex

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