Method of sulphide stock containing noble metals

FIELD: metallurgy.

SUBSTANCE: invention relates to hydrometallurgy of noble metals. Proposed process comprises grinding of stock to not over 90%-grade minus 10 mcm, pressure leaching at oxygen feed at 100-110°C and partial pressure of oxygen of 1.0-1.5 MPa with production the pulp. Then, pulp is divided into solution and solid residue. Precious metals are extracted from solid residue of pressure leaching by solution containing artificially produced thiosulphate ions by processing of pressure oxidation residue including elementary sulphur by solutions containing sulphite-ion. Note here that concentration of sulphite-ions in solution fed for leaching makes 30-65 g/l. To accelerate dissolution of precious metals leaching is performed at pulp temperature of 20-80°C and medium pH of 5.5-40.5.

EFFECT: lower costs, higher yield.

10 cl, 4 tbl, 2 ex

 

The invention relates to the field of hydrometallurgy of precious metals and can be used to extract gold and silver from mineral raw materials, where they are associated with sulphides and sulphide mineral raw materials containing precious metals and sorption active carbon substance and/or minerals laneside containing copper, arsenic, antimony, etc. or a combination of all these qualities.

The main carriers of gold and silver in hard ores are sulfides: pyrite, arsenopyrite, chalcopyrite, Galena, antimonite and other precious metals - gold and silver are usually present in the concentrates from ores in the form of thin inclusions in sulfides.

A method of refining sulfide concentrates containing precious metals, according to which they are exposed to oxidizing roasting at a temperature of 500÷700°C with subsequent thiosulfate leaching of the calcine. [1]

The disadvantages of this method are the complexity of the hardware design, high capital and operating costs associated with the need for disposal of large quantities of highly toxic kiln gases (including arsenic trioxide, which is limited demand and therefore should be buried). Also we have the loss of precious metals from the tailings leach (5÷10 g/is) due to sintering of the material and the formation of passivating films of low-melting compounds. In addition, noble metals are lost with the arsenic dust bag filters.

There is a method of high-temperature pressure leaching of concentrates containing precious metals and sulfides at temperatures 180-225°C and oxygen pressure of 1.7 to 3.0 MPa, followed by extraction of precious metals sorption cyanidation Chekov or ammonia-sulfite-thiosulfate leaching [2-3].

The disadvantages of this method are the high capital costs due to the large number of technological operations and the high cost of equipment (autoclaves, oxygen plants, etc.), working under high pressure and at high temperatures. In addition, when using very toxic cyanide solutions have significant costs for the disposal of wastewater. The use of ammonia-sulfite-thiosulfate solutions under the application [3] is connected with the necessity of the use of halogenated reagents to achieve acceptable rates of extraction of gold, and is also unfair in connection with the use of ammonia.

A method of refining sulfide gold-bearing materials, including bacterial opening the source material and the subsequent leaching with a solution of oxygen compounds of sulfur, according to the invention, the leaching is carried out with a solution, terrasim ion hydrosulfite (HSO3-)and spend it without access oxidant, for example air [4].

Mass concentration ion hydrosulfite is 10.0-100.0 g/l, and the leaching is carried out at a pH of 3-5.

As a source of ion hydrosulfite use a solution of salts of sulfurous acid or alkali with bubbling sulphurous anhydride or a mixture of sulfur and sulfur anhydrides.

The disadvantages of this method are the need of the leaching of gold in acidic environment, which necessitates the use of acid-resistant materials. In addition, the process of the oxidation process is very long, has high operating costs, and requires careful control of process conditions.

The closest in technical essence and adopted for the prototype is a method of processing sulphide gold-bearing materials [5], including low-temperature pressure oxidation of sulfide raw materials containing precious metals and non-ferrous metals: copper, Nickel and other

In accordance with this method the material is crushed to a particle size of 100% minus 15 μm and is subjected to pressure oxidation at temperatures of 100÷120°C and total pressure of oxygen of 1.0 MPa. While removing color is yellow in the solution is at least 90%. Recovery of gold from Chekov pressure oxidation may cyanidation or other known methods.

This method allows you to process refractory sulfide raw materials containing non-ferrous and noble metals with high rates of extraction. This method allows to reduce the capital cost of the processing of sulfide raw materials through the use of cheaper equipment, and operating costs due to the significant reduction in the consumption of gaseous oxidant (oxygen).

The disadvantage of this method is the formation of granules gray-sulfide phase during pressure oxidation process temperatures above the melting temperature of elemental sulfur (112÷115°C), which reduces the oxidation of sulfides and the extraction of valuable components. In order to avoid this phenomenon when carrying out the process at temperatures higher than specified in the pulp add surface-active substances (surfactants), which prevent contact of the melt with sulfur particles oxidized sulphides. Another disadvantage of this method is the use of expensive and toxic cyanide and increased its consumption during cyanidation Chekov pressure oxidation associated with high (up to 10%) content in the residues form elemental sulfur, which is formed by autoclave oxidation at unizhennyh temperatures. The formation of sulfur occurs by the following reactions:

FeS2+2O2=FeSO4+S0 (1)

4FeAsS+7O2+4H2SO4+2H2O=4FeSO4+4H3AsO4+4S0(2)

Cu2S+O2+2H2SO4=2SuSO4+S+2H2Omtext> (3)

CuFeS2+1.25O2+2.5H2SO4CuSO4+0,5Fe2(SO4)3+2S+2,5H2O(4)

To reduce the amount of cyanide used different methods of sulfur removal from Chekov before cyanidation. For example, hot alkaline or lime handling Chekov at temperatures of 85°C and more. In addition, the use of alkaline cyanide solution causes neobhodimosti operations of washing and neutralization of the acid Chekov AO before leaching, and the need for detoxification solutions containing cyanide and other hazardous for the environment connection. This complicates the technological scheme and is also a disadvantage.

The challenge which seeks the invention is to reduce the cost of processing refractory raw materials containing precious metals and sulfides and improving the extraction of metals. The task is solved by the technical solution, consisting in the reduction of technological operations and the use of less expensive and environmentally friendly solvent.

This technical result is achieved in that in the method for processing sulfide raw materials containing precious metals, including the grinding of the raw material, mixing the raw material with an aqueous solution of sulphuric acid pressure oxidation (AO) of the pulp with oxygen, its separation into a liquid solution and a solid residue, and extraction of non-ferrous and precious metals products from AO. Pressure oxidation is performed on the material with a particle size of not more than 90% minus 10 microns at a temperature of 100÷110°C and a partial pressure of oxygen of 1.0÷1.5 MPa, and the extraction of precious metals are leaching the solid residue AO solutions containing thiosulfate ions, obtained by processing Chekov AO containing elemental CE is the solution, containing a sulfite ion. In this case, the concentration of the sulfite ion in fed to the leaching solution is 30÷65 g/l,

The sulfite ions can be introduced into the solution by adding salts of sulphurous acid and bubbling sulfur dioxide through the alkaline solution.

To obtain the sulfur dioxide is used, the firing Chekov AO and/or cement sludge or sludge from chemical precipitation of gold from the leach solution.

The thiosulfate ions are produced by processing of sulfur-containing Chekov pressure oxidation solution containing sulfite ions(SO32-).

To accelerate the dissolution of noble metals, the process is carried out at a temperature of pulp 20-80°C.

When leaching the pH of the medium is 5.5+10,5.

The essence of the method lies in the fact that the pressure oxidation is performed on the material particle size is not more than 90% minus 10 microns at a temperature of 100÷110°C and a partial pressure of oxygen of 1.0÷1.5 MPa, while base metals into solution JSC, from which they can be allocated to known methods, for example extraction, elemental sulfur formed during AO, remains in the solid residue, and extraction of precious metals are leaching the solid which on balance AO solutions containing a sulfite ion(SO32-).

The solution contains a sulfite ions interact with elementary sulfur with the formation of thiosulfate ions by the reaction:

SO32-+S0S2O32- (5)

The dissolution of precious metals is sulfite and thiosulfate ions according to the reaction:

2(Au/Ag)+4S2O32-+H2O+1/2[O2]2[(Au/Ag)(S2O3)2]3-+2OH-,(6)

2(Au/Ag)+4SO32-+1/2O2+H2O2 [(Au/Ag)(SO3)2]3-+2OH-,(7)

The allocation of precious metals from solution is carried out by known methods, e.g. by cementation or chemical deposition.

As a source of sulfite ion can be used, or a solution of salts of sulfurous acid or alkali with bubbling sulphurous anhydride.

When the bubbling sulfur dioxide through a solution of alkali occur following reaction:

SO2+H2OSO32-+OH- (8)

SO2+OH-SO32-+H+ (9)

Further, the formation of thiosulfate and the dissolution of gold and silver flows in accordance with reactions 5, 6 and 7.

Sulfur dioxide can be obtained by burning part of the material obtained with AO or when the cement kiln sludge or sludge obtained in the destruction of sulfur-containing compounds during the chemical deposition of gold from thiosulfate solution.

The physico-chemical nature of the leaching of precious metals by the present method is the simultaneous processes of formation of a reagent-solvent from the products obtained in the processing of mineral raw materials (reactions 1-5, 8-9) and dissolution of precious metals using this reagent (reaction 6-7).

In the present method parameters sulfite leaching depending the chemical composition of the processed solid residue autoclave opened. The solution fed to the leaching contains 30÷65 g/l of a sulfite ion(SO32-). Formed by the reaction of 5 thiosulfate ion is the main solvent of noble metals, while the sulfite ion is used primarily to obtain the thiosulfate-ion(S2O32-).

Gold directly poorly soluble sulfur-ion, but forms a strong enough connection[Au(SO3)2]3-.

In the present method the AO process is performed on the material particle size is not more than 90% minus 10 microns at temperatures (100÷110°C) below the melting temperature of elemental sulfur (112÷115°C) and oxygen partial pressure of 10÷15 MPa.

In the present method sulfite solutions in contact with sulfur-containing cakes AO with the formation of thiosulfate ions by the reaction of 1.

In the present method, the concentration of the sulfite ion is 30÷65 g/l thus osenia W:T=5÷10:1, the leaching process is carried out at a temperature of 20÷80°C, with access of air oxygen.

In the present method the pH of the medium is 5.5÷10,5.

Analysis of the proposed method with the prototype shows that the inventive method differs from the known process AO at temperatures not higher than 110°C.

The inventive method differs from the known process AO on the material having a particle size of not more than 90% minus 10 microns.

The inventive method differs from known without using a surfactant in the AO process.

The inventive method differs from the known lack of need for prior removal of sulfur from Chekov AO before the leaching of precious metals.

The inventive method differs from the known process of leaching of precious metals from Chekov AO using nationsthe solvent obtained in the processing of mineral raw materials by the present method.

The inventive method differs from the known lack of need for acid washing Chekov and neutralize them before cyanidation processing of mineral raw materials by a known method.

The inventive method differs from known more than a simple technological scheme of processing of mineral raw materials by the present method.

Each otlicials the discernment is essential because of the absence of any of them does not allow to achieve the specified technical result.

The inventive method of processing sulphide raw materials containing precious metals provides lower capital and operating costs for processing of concentrates through the use of reagents, obtained on the spot, and also by reducing the number of operations of processing of raw materials, and meets higher environmental requirements for processes of extraction of gold and silver due to the use of chemicals with less harmful hazard class not requiring the use of special operations neutralization.

Examples of using the proposed method

Example 1. Flotation concentrate containing, wt.%: pyrite 27,7; tennantite 16,8; chalcopyrite 1,5; quartz 30,4; pyrophyllite 18,5; gold 54.6 g/t; silver of 92.1 g/t, were crushed to a particle size 90% minus 20, 15, 10 and 5 μm were subjected to AO at a temperature of 107±2°C and a pressure of 0,5,1,0 and 1.5 MPa.

AO flotation concentrate was carried out in a laboratory autoclave with a displacement of 2 DM3. The autoclave was an airtight tank is made of stainless steel with a titanium liner, equipped with impeller agitator. The autoclave is equipped with an electric heater that has a sensor for measuring temperature, voltage regulator circuit heating, ammeter, timer display, busstop is striated (smooth) speed control mixer with display showing, manometer for measuring the pressure inside the autoclave. The gas phase is produced by using a needle valve. Oxygen is supplied via a gearbox from a container.

The experimental results are shown in table 1

for 93.4
ValueIndicators
The oxidation of sulfides, %Extraction of metals from products AO %
CuZnAuAg
The particle size of material*, µm2077,174,360,840,123,1
1584,579,171,574,634,2
10to 89.993,287,597,361,4
594,392,6of 98.263,4
The oxygen pressure**, MPa0,5to 85.2to 89.580,145,233,2
1,0to 89.5for 93.488,687,141,1
1,5br93.194,7.90,499,062,4
2,093,394,890,4the 98.963,1
* - General conditions Po2=1.5 MPa, the contents of the specified size class 90 %, temperature 105°C.
** - General conditions the particle size of 90% minus 10 microns, the temperature of 105°C

From table 1 it is evident that to achieve the technical result of the AO process should be carried out on the material particle size is not the more minus 10 microns and at a pressure of oxygen of 1.0÷1.5 MPa. Increasing the particle size of the material above the specified limit leads to reduction process. At the same time lowering the pressure below 1.0 MPa also leads to reduction of the process, and increase more than 1.5 MPa is not advisable as it does not has a significant positive effect on process performance and requires additional investment.

To determine the parameters of extracting precious metals from Chekov AO flotation concentrate was oxidized in an autoclave under the following conditions: particle size 90% minus 10 microns, the temperature of 107±2°C, oxygen pressure of 1.5 MPa.

The obtained residues form Ao contained 6,5÷8,5% sulfur in the elemental state, 69÷80 g/t Au and 127÷143 g/t Ag.

The obtained cake was processed in accordance with the method of the prototype, and in accordance with the claimed method. The results obtained are presented in tables 2 and 3.

Table 2
The results of the experiments on leaching of gold from Chekov AO prototype
KEKThe output of the cake, %The content in the cake, g/tInitial content analysis, g/tWPI is Uchenie, %The consumption of reagents by technology, kg/t
AuAgAuAgAuAgNaOHNaCNCaO
JSC1426,48675,0127,987,94,5-143,0350
SCHO*1025,813891,515693,59,8500871,5
* - KEK JSC after removal of sulfur alkaline processing

Table 2 shows that during the process Chekov AO in the method prototype have an excessively high consumption of reagents (Flow are presented only for the operation of the leaching of precious metals). In addition to t the th, the extraction of silver was less than 10%. This demonstrates the inappropriateness of the use of the method of the prototype with respect to this mineral raw materials due to the high capital costs of reagents.

Leaching of precious metals from Chekov AO, by the present method, solutions containing sulfite ion, conducted by dissolving sodium sulfite, and bubbling through a solution of caustic soda of sulphurous anhydride. The concentration of sodium sulfite was 50÷100 g/l (at a concentration of less than 50 g/l, the extraction of gold is reduced, and in concentrations above 100 g/l does not increase), temperature 25÷80°C (the lower limit is limited to normal conditions, and when exceeding the upper limit of the rate of destruction of the thiosulfate ion increases dramatically, resulting in lower gold recovery). pH was 5.5÷40,5. At a lower pH value, you need to use acid-resistant equipment, the upper limit is due to the physical properties of sulfite solutions. Output Chekov leaching was 85÷87%.

Table 3
The results of the experiments on leaching of gold from Chekov JSC sulfite solutions
Na2SO3/sub> , g/lW:TpHt °Cτ, hThe content in cakes*, g/tExtraction into solution, %
AuAgAuAg
5:19,825-308015,386,2to 78.338,1
9,970-80213,878,480,445,2
5010:19,525-30805,854,392,257,6
the 9.770-80 26,551,3to 92.158,2
15:19,525-30804,552,2of 92.754,3
9,870-8025,150,6br93.155,9
5:19,825-308012,675,380,145,3
9,670-80216,370,176,950,1
7510:19,525-30802,3 66,9for 95.357,6
9,870-8021,868,297,6to 58.1
15:19,825-30800,960,198,660,6
9,970-8020,759,399,064,8
5:19,625-308010,973,9to 85.246,2
9,970-8028,769,9and 88.8 50,3
10010:110,025-30800,560,8of 99.165,1
9,870-8021,568,897,662,3
15:110,525-30800,660,199,466,2
the 9.770-8020,859,898,364,9
SO2+NaOH (10 g/l)5:15,525,4of 89.170,810:16,04,275,194,156,0
15:15,870-8022,1and 88.898,3to 49.9
SO2+NaOH (20 g/l)5:18,112,473,176,256,5
10:17,61,078,699,252,3
15:18,30,770,6of 99.157,9
* contents are given without taking into account the output of the solid residue leaching.
** - the ratio of NaOH=1,1÷1,5:2

Example 2. Ismalic the config particle size up to 98% minus 10 microns flotation concentrate, containing pyrite 32,6; arsenopyrite 17,2; quartz 12,8; micaceous-gidrologiya (sericite, hydrosilicate, illite) 20,1; organic sorption--active carbon of 0.6; gold and 22.6 g/t; were subjected to AO at a temperature of 107±2°C and a pressure of 1.5 MPa.

The obtained residues form AO consisted of 9.9÷13.8% sulfur in the elemental state and 32.3÷35,7 g/t AU.

On the cake AO conducted leaching of precious metals with solutions containing sulfite ion. The sulfite ion was introduced into the solution by dissolution of sodium sulfite, and bubbling through a solution of caustic soda of sulphurous anhydride. Temperature leaching in all experiments was 75÷80°C for a duration of 0.5 hours. The output of the solid residue after leaching was 80÷85%. The results of the experiments are presented in table 4.

Table 4
The results of experiments on the extraction of gold from Chekov AO sulfite solutions
Na2SO3, g/lW:TpHThe concentration of Au in solution, mg/lThe content of Au in cakes*, g/tExtraction of Au in solution, %
505:19,5 7,13,592,3
10:110,24,33,791,9
SO2+NaOH (7 g/l)**5:15,66,84,590,9
SO2+NaOH (10 g/l)**6,87,23,4br93.1
* contents are given without taking into account the output of the solid residue leaching.
* * - the ratio of NaOH=1,1÷1,5:2

The results presented in tables 3 and 4 show that the extraction of gold and silver does not practically depend on how the suspension was saturated with the sulfite-ion: the introduction of sodium sulfite or the introduction of caustic soda by bubbling sulfur dioxide, but depends on its concentration, G:T and properties of the processed material.

The optimum concentration of the sulfite ion depends on the individual composition of the processed material and SOS which defaults to 30÷65 g/L. The conditions and process parameters AO resistant material and sulfite leaching of precious metals from Chekov AO also selected experimentally for each resistant material.

The optimal pH of a solution is a value of from 5.5 to 9.5.

The positive effect of the proposed method in comparison with the prototype is to reduce capital and operating costs for processing hard materials, as well as in the facilitation of the technological scheme of processing.

The list of references

1. Beliavsky M.A. Behavior of gold and silver thiosulfate and sulfite media in relation to the problem of hydrometallurgical processing of pyrite Ogarkov: abstract. - M: ISIS, 1988.

2. Patent 5071477 USA, MCI C22B 3/44. Process for recovery of gold from refractory ores / K.G.Thomas, H.J.Pieterse, R.E.Brewer, K.S.Fraser; American Barrick Resources Corp.of Toronto. No. 518125; Appl. 03.05.90; Publ. 10.12.91, NCI 75/744.

3. Patent 2447166 EN, IPC C22B 11/00. Method for processing sulfide raw materials containing precious metals / Ashurkov, Mai, Aphrodite; Irkutsk research Institute of noble and rare metals and diamonds. No. 2010124712/02; Appl. 16.06.2010; Publ. 10.04.2012.

4. Patent 2031157 EN, IPC C22B 3/04, C22B 11/00. Method for processing gold-bearing sulfide materials / Sub, Veemente, Lpositive; Irkutsk state scientific research is Yelsk Institute of rare and nonferrous metals. No. 5014080/02; Appl. 04.07.91; Publ. 20.03.95.

5. Patent 5232491 A US, MKI C22B 11/08. Activation of a mineral species / Ian J.Corrans, John E.Angove; Dominion Mining Limited. No. 902992; Appl. 23.06.92; Publ. 03.08.1993, NCI 75/743 prototype.

1. Method for processing sulfide raw materials containing precious metals, including grinding of raw materials, low-temperature pressure oxidation with oxygen from obtaining pulp, its division into the solution and the solid residue and the extraction of precious metals from the products obtained, characterized in that the extraction of precious metals are leaching from the solid residue by solutions containing thiosulfate ions, obtained by processing the solid pressure oxidation residue containing elemental sulfur, solutions containing sulfite ion.

2. The method according to claim 1, characterized in that the particle size of the material to be applied to pressure oxidation is not more than 90% of the class minus 10 microns.

3. The method according to claim 1, wherein the pressure oxidation is carried out at a temperature of 100÷110°C.

4. The method according to claim 1, characterized in that the partial pressure of oxygen in the autoclave oxidation is 1.0÷1.5 MPa.

5. The method according to claim 1, characterized in that the pressure oxidation residue contains elemental sulfur.

6. The method according to claim 1, characterized in that the concentration of the sulfite ion in fed to the leaching RA the creation is 30÷65 g/l

7. The method according to claim 1, wherein the sulfite ions is introduced into the solution by adding salts of sulfurous acid or by bubbling sulfur dioxide through the alkaline solution.

8. The method according to claim 7, characterized in that to obtain the sulfur dioxide is used, the firing part of the balance of pressure oxidation and/or cement sludge or sludge from chemical precipitation of gold from the leach solution.

9. The method according to claim 1, characterized in that, to accelerate the dissolution of precious metals leaching is carried out at a temperature of slurry 20÷80°C.

10. The method according to claim 1, characterized in that the pH of the environment by leaching is 5.5÷10,5.



 

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EFFECT: maximum application of live steam heat, optimised thermal and hydrodynamic conditions, lower costs.

4 cl, 2 dwg, 3 ex

FIELD: mining.

SUBSTANCE: method to produce metals from storages of stale wastes of polymetal ore dressing consists in trench opening of the storage, detection of layers containing easily dissolved forms of non-ferrous metals and layers containing noble metals, bulk extraction of stale wastes from the storage, fraction separation of stale wastes into a finer sulfide fraction dressed with noble metals and coarser fraction dressed with non-ferrous metals, and their separate leaching.

EFFECT: complete processing of storages of stale dressing wastes, release of areas occupied by them, complex usage of mineral materials and high environmental and economic effect.

3 cl, 1 dwg

FIELD: chemistry.

SUBSTANCE: method of separating platinum (II, IV) and rhodium (III) from nickel (II) in chloride solutions includes sorption of platinum (II, IV) and rhodium (III) and further desorption of the said metals. Sorption is carried out from freshly prepared and mature solutions in dynamic conditions by passing the solution through a layer of strongly basic anionite Purolite A 500 or weakly basic complex-forming anionite Purolite S 985, containing polyamine functional groups. Complete transfer of platinum (II, IV) and rhodium (III) into anionite takes place, with nickel (II) remaining in a discharged solution.

EFFECT: reduction of the process time, separation of platinum metals from accompanying metals, in particular from nickel, an increased degree of metal extraction, reduction of labour consumption of the separation process.

2 dwg, 2 tbl, 6 ex

Device for leaching // 2526350

FIELD: chemistry.

SUBSTANCE: device contains a conical reactor with a lid, a lower branch pipe of the input and an upper branch pipe of the output of a reaction mixture. It includes a unit of forced circulation consisting of a pump and connecting tubes. The unit of forced circulation includes internal and external contours. The internal contour is made in the form of a tube, which is placed vertically inside the reactor, with the tube facing a branch pipe of the input with the lower end, and in the upper part the tube is made in the form of an arch, placed in the horizontal plane and adjoining the internal wall of the reactor. The branch pipe of the input is equipped with a nozzle, which forms an ejection system with the lower end of an internal contour, and the branch pipe of the output of the reaction mixture is placed in the middle of the reactor lid and is made with a possibility of immersion into the reaction mixture.

EFFECT: intensification of leaching of metals and their compounds.

1 dwg, 1 tbl

FIELD: metallurgy.

SUBSTANCE: proposed method comprises melting of initial stock with flux containing 3-15 wt % of dewatered borax, 0.5-3 wt % of calcium oxide and 0.4-3 wt % of quartz sand relative to the sum of weight of impurities in initial product. Melt heated to 1100-1200°C is bubbled by oxygen-bearing gas to termination of impurities oxidation. Then, oxidised melt is poured at 1200-1250°C into heated lined mould arranged at centrifuge rotor. Mould with melt is spinned at the rate creating the gravity factor Kg=50-500. Note here that used mould allows melt cooling rate not exceeding 10°C/min. Mould spinning is terminated after melt crystallisation termination to obtain casting with temperature lower that solidus temperature.

EFFECT: higher purity and good geometry of final product.

2 cl, 2 tbl

FIELD: mining.

SUBSTANCE: invention relates to concentration of minerals and can be used for extraction of fine gold from argillaceous sediments. This method comprises preparation of suspension of argillaceous sediments, trapping of fine gold from said suspension by introduction of vegetable material-based sorbent premixed to 0.3 mm grain size in suspension and mixing. Then, sorbent is flushed through 0.3 mm mesh screen, dried and subjected to assay fusion. Note here that suspension is prepared at S:L ratio of 1:25. Sorbent is added to suspension activated in mixer to homogeneous state for 3-5 minutes and, then, mixed for 30-40 seconds. After sorption, loose flakes bearing gold are flushed.

EFFECT: higher yield, environmental safety.

3 ex

FIELD: chemistry.

SUBSTANCE: method includes oxidising roasting, percolation leaching of the roasted product with aqueous solution of an oxidising agent or mixtures of oxidising agents to obtain a rhenium-containing solution and an insoluble residue, sorption of rhenium from the rhenium-containing solution in a separate apparatus, drying the insoluble residue, mixing with fluxing agents and fusion on a metal collector. Percolation leaching is carried out at redox potential values of 900-1100 mV and temperature of 50-90°C, with simultaneous sorption of rhenium, followed by desorption and separation of rhenium compounds or rhenium metal from the strippant. The fluxing agents used to fuse the insoluble residue are fluorspar, sodium carbonate and sodium nitrate. Fusion is carried out at temperature of 1200-1800°C on a metal collector in several steps, while discharging the formed slag after each step and fusing the next portion of the mixture on the collector from the previous fusion with separation of the alloy of platinum metals with the collector.

EFFECT: high degree of extraction of rhenium, low reactant consumption, labour input, faster processing of the material, considerable reduction of the volume of solutions which require recycling.

8 cl, 1 dwg, 1 ex

FIELD: chemistry.

SUBSTANCE: method includes passing the solution through polymer fibre for sorption of silver ions. After passing the solution, silver ions contained in the fibre are reduced to a metal state with 0.02 M aqueous solution of a mixture of ascorbic acid with glucose in ratio of 1:9. Silver metal is then extracted by burning the silver-containing fibre in an air atmosphere at temperature of 450-500°C, followed by washing the formed silver reguli.

EFFECT: recovering silver ions from industrial waste water, improved method of extracting silver from process solutions used when producing textile materials with antimicrobial properties.

2 ex

FIELD: metallurgy.

SUBSTANCE: invention relates to hydrometallurgy of noble metals and can be used for silver extraction from alkaline cyanide solutions by cementation. Proposed method comprises cementation by aluminium as 0.1-2.0 mm thick chips. Cementation is carried out at specific solution feed rate of 1-4 m3/m2·h at concentration of sodium hydroxide of 1.0-10.0 g/l.

EFFECT: higher yield and quality.

3 tbl, 3 ex

FIELD: metallurgy.

SUBSTANCE: electronic waste is crushed on a hammer crusher; crushed copper is added, and then, it is fused in presence of flux during 45-60 minutes at the temperature of 1320-1350°C with air blowdown at its flow rate of 3-4.5 l/h and the obtained slag containing at least 2.6 wt % of precious metals is separated from slag.

EFFECT: effective electronic waste processing with increase of content of precious metals in an alloy.

1 ex

FIELD: metallurgy.

SUBSTANCE: invention relates to hydrometallurgy and can be used for processing of concentrates, industrial products and solid wastes containing metals. Proposed process comprises leaching of cake 3 n, by HCl solution at 70°C and L:S ratio of 2. Note here that leaching is performed in the presence of table salt of concentration making at least 120-140 g/dm3.

EFFECT: intensified leaching, higher yield.

4 tbl, 2 ex

FIELD: metallurgy.

SUBSTANCE: method to process an alloy of ligature gold, containing not more than 13% of silver and at least 85% of gold, includes electrolysis with soluble anodes from initial alloy with usage of hydrochloric acid solution of aurichlorohydric acid (HAuCl4) with excessive acidity by HCl 70-150 g/l as electrolyte. Electrolysis is carried out with deposition of pure gold on cathodes. At the same time into the initial electrolyte prior to start of the electrolysis process they introduce nitric acid to its concentration in electrolyte 70÷100 g/l. Then nitric acid is added in process of electrolysis into electrolyte in a dosing manner.

EFFECT: performance of gold refining per one stage with production of target product with high content of gold with reduced duration of process and lower energy and labour inputs.

3 cl

FIELD: noble metal hydrometallurgy.

SUBSTANCE: invention relates to method for acid leaching of platinum method from secondary raw materials, in particular from ceramic support coated with platinum metal film. Target metals are leached with mixture of hydrochloric acid and alkali hypochlorite at mass ratio of OCl-/HCL = 0.22-0.25 and redox potential of 1350-1420 mV.

EFFECT: decreased leaching temperature, reduced cost, improved platinum metal yield.

2 ex

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