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INVENTION
Patent of the Russian Federation RU2078839

LINE OF PROCESSING OF FLOTOCONCENTRATES

The name of the inventor: Panchenko AF; Khmelnitskaya O.D .; Lodejshchikov VV; Mullov V.M.
The name of the patent holder: Joint Stock Company "Irgiredmet"
Address for correspondence:
The effective date of the patent: 1995.03.21

The invention relates to the hydrometallurgy of noble metals, in particular to the line for extracting gold and silver from sulfide flotation concentrates by thiocarbamide technology, including the concentrate grinding module installed during the process and connected by vehicles, the agitation leaching module, the carburizing module and the cleaning and conditioning module Disodium metal solution. The entity line is equipped with a filtration leaching module installed after the grinding module and an electrolysis module of filtration leach solutions placed in front of the carburizing module, wherein the filter leaching module is connected to the grinding module by means of conveying the concentrate, the filter cake transporting means is connected to the agitation leach module and the pipelines Transport of the filtrate and unmethodized solution is connected to the module of electrolysis, the electrolysis module is connected via the transport module to the clearance and conditioning module of the unmetered solution, which is connected to the agitation leaching module by the transport pipeline, and the latter by the pipeline for transport of poor silver-containing solutions with the filtration leaching module.

DESCRIPTION OF THE INVENTION

The invention relates to the hydrometallurgy of noble metals, in particular to the extraction of silver from sulphide flotation concentrates by thiocarbamide technology.

There is a hardware-technological line for extracting gold and silver from the burnt gold and silver containing flotation concentrates of the Salsin mine, in which, along the process, the concentrate grinding module, the agitation leaching module, the silver-silvering solution of thiourea cementation module and the cleaning module And conditioning an unmethodized solution of thiourea with a solution in circulation (1).

In a known line, the original flotation concentrate is ground in a ball mill operating in a closed cycle with hydrocyclones. The resulting pulp is subjected to acid treatment for purification from metal impurities.

Peeled from impurities and dehydrated concentrate is pulverized with a solution of thiourea (thiourea) and subjected to agitation leaching in a cascade of 2 contact vats. Thiocarbamide pulp is dewatered on a band filter. The filter cake is washed off with water and dumped into the dump, and the filter is fed to the deposition of gold and silver by carburizing with aluminum dust in a cascade of 2 cement vats. The cement cake is filtered out on a vacuum filter and fed to refining. The obmetalenny solution of the solvent is purified from the metal-impurities, regenerated and after conditioning by the content of thiourea and acid returns to the leaching cycle.

The line provides processing of flotation concentrates with a gold content of 39 g / t, silver of 100 g / t when 97% silver is extracted into the cement cake - 91%

The drawbacks of the line include a low degree of silver recovery from rich sulfide silver flotation concentrates. This is due to the fact that in the known line when processing rich flotation concentrates containing silver in sulphide form, leaching of silver by agitation is carried out in the same volume of solvent and upon reaching saturation of the solution with silver ceases. At the same time, the need to extract silver into the solution, in turn, leads to an increase in the volume of processing and metal consumption of equipment in leaching cycles, de-silvering of the silver-containing solution, regeneration and conditioning of the disodium metal solution and, as a consequence, to a decrease in processing efficiency.

The object of the invention is to increase the processing efficiency of rich sulfide silver-containing flotation concentrates by increasing the silver recovery and reducing costs.

This technological result is achieved by the fact that the processing line for sulfide silver containing flot concentrates, including the module for grinding the leach concentrate, the carburizing module and the cleaning and conditioning module of the unmethodated solution, installed along the process and connected with each other by means of pipelines, equipped with a filtration module Leaching module installed behind the grinding module and the electrolysis module of the filtration leach solutions placed in front of the carburization module, wherein the filtration leaching module by the concentrate transportation pipeline is connected to the grinding module, the filtration cake transfer line is connected to the agitation leaching module, and the filter transport pipelines and the unmetered solution Is connected to the closed circuit with the electrolysis module, the electrolysis module through the cementation module is connected by a transport pipeline to the unmetered solution cleaning and conditioning module that is connected to the agitation leaching module by the transport pipeline, and the latter by the pipeline for transport of poor silver-containing solutions with the filtration leaching module.

In a preferred embodiment of the invention, the filtration leaching module is a filter press with horizontal chambers, a leach solution tank and a contact vat for concentrate pulping, connected to the filter press by the solution and pulp conveying pipes respectively, and a rich silver-containing solution storage tank associated with Filter press by pipeline.

In addition, the electrolysis module is made in the form of two electrolyzers with plate and carbon graphite cathodes installed in a cascade and connected in series by a pipeline and a tank of a de-metalized solution.

In this case, the agitation leaching module is, for example, at least one contact vessel and a filter press with horizontal chambers connected to each other by a transport conduit and a poor silver solution collecting tank connected to the filter press by a pipeline. The carburizing module is installed one above the other with the possibility of rearranging at least two cementers, each of which is a container with a compressed stack of alternating layers of metal-cementator and graphitized batting located between the nozzles of the inlet and outlet of the solution.

In this case, the clearance and conditioning module of the unmethodated solution is a lime treatment contact box and a filter press with vertical chambers connected by a transport pipeline and a contact vat for conditioning the solution connected to the filter press by a pipeline.

The conformity of the claimed invention with the requirement of novelty is due to the fact that the totality of its essential characteristics is not identical to the essential features of the prototype.

The conformity of the claimed invention to the requirement of the inventive level is due to the fact that the combination of its distinctive features, allowing leaching of silver from the flotation concentrate by filtration of the solution under pressure through thiourea dental pulp, allows the main part of silver to be extracted into a rich solution, followed by its electrolytic extraction into a cathode deposit, and the remaining in cakes Filtration leaching, some of the silver is extracted in the agitation leaching cycle. At the same time, dezmetallization of a rich silver solution by electrolysis makes it possible to use most of the unmethodized solution in circulation for filtration leaching without cleaning it (solution) from impurities and conditioning by reagents because of the ability of thiourea to regenerate during electrolysis, which helps to reduce costs. The use of a smaller portion of the electrolyzed solution after the pre-extraction of silver by carburizing to alternating layers of cementitious metal and graphitized batting in a cycle of agitational leaching of silver from filtration leaching cakes with feeding the resulting poor silver-silver thiourea solution into the filtration leaching cycle provides the possibility of a non-stop rotation of the thiourea solution in the line And the maximum use of thiourea in circulation, which reduces the cost of processing the concentrate and does not explicitly follow from the prior art.

In addition, two-stage leaching of silver from the initial concentrate and its leaching cakes with the supply of a rich silver-containing solution to precipitation of silver by electrolysis and cementation, and the poor silver-containing solution in the part of the electrolyzed solution for filtration leaching of the concentrate allows, in comparison with the prior art, to increase the extraction of silver from the concentrate In the solution from 91 to 99.9% a and the degree of silver recovery into the cathode and cement sediment, respectively, up to 99.0 and 99.9%.

FIG. 1 schematically shows the general appearance of the line; In Fig. 2 filter press with horizontal chambers.

FIG. 3 Cementator; In Fig. 4 electrolyzer with plate cathodes.

FIG. 5 electrolyser with carbon-graphite cathodes; In Fig. 6 filter press with vertical chambers.

A line for processing sulfide silver containing flotation concentrates by thiocarbamide technology according to the scheme for grinding silver from concentrate, then precipitating it from the thiocarbamide solution by electrolysis and feeding the main part of the electrolysis solution to the filtration leaching, and the remaining part for silver precipitation by cementation and purification of the solution from impurities, agitation leaching of filtration leaching cakes Disinfected electrolysis and a solution free from impurities and then feeding it to the filtration leaching cycle contains the module 1 for grinding the initial concentrate, the concentrate filtration unit 2, the electrolysis module 3, the carburization module 4, the purification module 5 installed along the process and connected to each other by vehicles And concentration of the unmethodized solution, the agitation leaching module 6. [

The grinding unit 1 is intended for refining the concentrate and includes a ball mill 7 connected in a closed grinding cycle to the hydrocyclones 8, 9 of the first and second stage of classification, a thickener 10 and a disk vacuum filter 11 successively connected by transport pipelines.

The module 1 by the pipeline for transporting the products of the grinding of the concentrate is connected to the contact vat of the module 2.

The filtration leaching unit 2 is designed for intensive leaching of silver from the concentrate grinding products and comprises a leaching solution tank 12, a concentrate separation bag 13 and a filter press 14 with horizontal, stacked filter chambers 15 connected through a leach solution inlet manifold 16 and Pulps with a transport pipeline, respectively, with a capacity of 12 and a contact vat 13, and through a cake and collector outlet manifold 17 with a collecting tank 18 of a rich silver-containing solution.

Module 2 by the filtrate transport pipeline is connected to the electrolysis module 3, and the leaching cake conveying pipeline to the agitation leaching module 6. [

The electrolysis module 3 is designed to disperse the rich silver-containing solution of the leach concentrate leaching, as well as the purification from impurities and the regeneration of the thiourea solution, and is made in the form of two electrolyzers 19, 20 with a developed surface of the electrodes and the collection tank 21 of the unmethodated solution sequentially interconnected by the pipeline. Here, the cell 19 is a housing 22 separated by transverse partitions 23 into chambers 24 in which plate-shaped titanium cathodes 25 and anode chambers 26 are provided, provided with screen anodes 27 and ion-exchange membranes 28 arranged perpendicularly to the cathodes. The end chambers of the electrolyzer are equipped with nipples 29, 30 for introducing a rich silver and for the delivery of an unmethodized solution, respectively. In the lower part of the chambers 24, a branch pipe with a locking device 31 is provided for discharging the cathode deposit.

Electrolyzer 20 consists of a body 32 divided by longitudinal partitions 33 into a working cavity 34 and drain pockets 35 and cathode blocks 36 alternately arranged in the cavity of the casing 36 with a porous cathode 37 of carbon graphite fibers and anode chambers 38 with a screen anode 39 and ion exchange membranes 40. Cathode blocks and anode chambers are provided with fittings for the input and output of catholyte and anolyte (not shown). Module 3 conveys an unmetered solution with the container 12 of the module 2 and the module 4 of carburizing.

The carburizing unit 4 is designed to extract silver from the electrolysis-impregnated filtration leach solutions and is, for example, three cementers 41 arranged one above the other with the possibility of rearrangement, each of which is in the form of a container 42 with a compressed stack 43 of alternating layers of a cementing metal and a graphitized Batting placed between the nozzles of the inlet 44 and the outlet 45 of the solution.

The module 4 conveys the unmetered solution by the piping of the unmetered solution to the lime treatment contact box 48 of the module 5.

The purification and conditioning module 5 is designed to purify an unmetallized solution from metal impurities by liming and reinforce the solution through reagents and is a filter press 46 with vertical chambers 47 connected by a transport conduit at the inlet to a contact vat 48 for precipitation of impurities by liming, and at the outlet Contact term 49 to reinforce the solution-free solution with reagents.

The module 5 is connected to the contact cup 50 of the second stage of leaching of the module 6 by the transport pipeline.

The agitation leaching module 6 is designed to extract silver from the filtration leaching cakes and can be made, for example, in two units, each of which is a contact vat 50, a filter press 51 with horizontal chambers 52 and a silver-silver solution collecting tank 53 sequentially coupled And the filter press 51 'of the first plant is connected by a coke transport pipe to the second tank contact cup 50 "and the silver-silver solution collecting tank 53" by the latter by a transport pipeline is connected to the first installation contact cup 50'.

Module 6 by the pipeline of transportation of the gold-silver solution of the first stage of leaching is connected to the contact vat 13 of the pulp separation of the concentrate of module 1. The vehicles of the line are equipped with pumps, shut-off devices and electric control drive (not shown).

The line works as follows. The initial flotation concentrate containing 13.0 kg / ton of Ag, 19.0 g / t Au, 5.3% Fe, 15.6% S, 14.0% Zn, 10.3% Pb with a mass fraction of the class 0.074 mm 60 % Goes to module 1 in the cycle of closed grinding of the ball mill 7, where it is re-grinded and classified into two stages in hydrocyclones 8, 9 with a discharge of a plum with a mass fraction of the class minus 0.074 mm - 95% in the thickener 10 a of sands per mill.

In the thickener 10, the discharge of the hydrocyclone 9 with a mass fraction of solid 11% is concentrated to a mass fraction of solid in the pulp of -50%

The condensed pulp is fed to dewatering in the vacuum filter 11, and the thickener drains into the hydrocyclone 8. In the vacuum filter 11, the thickened pulp is dewatered to a mass fraction of moisture, in a cake from the solid weight of 25% with the filtrate fed to the thickener 10, and the cake into the contact tank 13 of module 2 as a product for leaching.

In Module 2, the products of the grinding of the concentrate are pulverized in the contact cup 13 to a mass fraction of the solid in the pulp of 33% leach solution with a concentration of thiocarbamide 40-50 g / l, sulfuric acid 50/60 g / l for 30 min.

Thiocarbamide pulp from the vat 13 is fed into the filter press 14 and, through the manifold 16, fills the filter chambers 15 into which a leaching solution with a concentration of thiocarbamide 40-45 g / l, sulfuric acid 50 G / l. Upon completion of filtration of the leach solution through the pulp, the solution is wrung from the cake (sediment) by a waterproof diaphragm (not shown) and through the collector 17 enters the collecting tank 18. Then, after depressurization, the cake (sediment) is removed from the chambers 15 through the reservoir 17 and transported to the first Setting the agitation leach to the contact vat 50 'of the module 6.

The content of silver and gold in the filtration cake was 1.2 kg / ton and 2.9 g / t, respectively. The extraction of silver into a solution of 91% gold 85%

After completion of the filtration leaching, a rich silver-containing thiourea solution containing 1.0 g / l silver and 1.5 mg / l gold from the collecting tank 18 is transported to an unscarf metal module 3.

In module 3, the rich silver-containing thiocarbamide solution is supplied first to the cell 19, where it sequentially passes through the chambers 24, washing the plate-like cathodes 25 and the anode chambers 26 in a continuous flow, is unmassed at the cathodes 25, and the de-metalized is withdrawn from the housing 22.

Electrolytic deposition of silver and gold on plate cathodes is conducted on the "depletion" of the solution to achieve a residual silver concentration of 20 mg / l, gold -0.2 mg / l. In this case, the separation of the cathode and anode space by the ion exchange membrane 28 prevents the oxidation of thiourea on the anode.

The cathode deposit from the cathode plates is showered into the lower part of the chambers 24, from which it is periodically discharged and fed to refining.

The recovery into the cathode metal was: silver 99.0% gold 92.0% Degree of regeneration of thiourea 80%

The solution immersed in the electrolyser 19 is additionally passed through an electrolysis cell 20 where the pressure solution is fed to the cathode blocks 36, filtered from the bottom up through the carbon graphite cathode 37, on the fibers of which gold and silver are extracted, and the depersonalized liquid is drained into the pockets 35 and then transported to the tank- Collection 21. Saturated with noble metals cathode blocks are extracted from the cell, released from the cathode deposit, which is fed to refining.

The residual concentration of silver in the solution was 5 mg / l, gold - 0.08 kg / l.

The thiourea solution in the module 3 that is immobilized in the module 3 is fed from the collecting tank 21 to the filtration leach cycle in the container 12 of the module 2, where it is corrected for the content of thiourea and sulfuric acid.

The other part of the solution by switching the valve is sent to the extraction of gold and silver by carburizing to module 4.

In module 4, a poor silver-silver solution of thiourea is sequentially passed through packets 43 alternating with a layer of cemented metal (iron shavings) and graphitized batting cementers 41 of the first, second and third stages of carburization until the concentration of silver in the solution at the outlet of the cementator of the third stage is not more than 0.1 Mg / l.

If the concentration of silver in the unmethodated solution exceeds 0.1 mg / l, the cementator from the first stage of carburization containing up to 90% of precious metals is disconnected from the module, in its place the cementator is moved from the second stage containing up to 35% of noble metals. The cementator with the third stage of carburization containing up to 5% of gold and silver is installed on the vacant space, and the cementant 41 with a freshly charged layer of cement-cement and graphitized batting is placed on the third stage.

The extraction of silver from the solution was 99.9%. Saturated with noble metals, charvatin is processed together with cathodic sediments.

The mortar immobilized by carburization from the module 4 is fed to the module 5 for cleaning from the impurity metals.

In module 5, a thiourea solution with a concentration of 0.15 g / l zinc, 0.15 g / l iron, 0.25 g / l copper, 35.0 g / l thiourea and 5.0 g / l sulfuric acid is first fed to Contact tank 48 where it is neutralized with lime to pH 8 and then passed through a filter press 46 where it is cleaned of the precipitated metal impurities and then fed into a contact vat 49 to reinforce the solution with sulfuric acid.

The solution with a concentration of thiocarbamide 40 g / l, sulfuric acid 5 g / l of module 5, conditioned to the reagent content, enters the contact vat 50 of the second agitation leaching unit of the module.

In module 6, the filtration leaching cakes of the concentrate from the module 2 enter the contact tank 50 'of the first leaching plant where they are pulverized to a mass fraction of 20% solid in the slurry with a silver-containing thiourea solution from the second leaching plant. The resulting pulp is agitated for 6 hours and then transported to a filter press 51 '. In the filter press 51 ', the leached thiocarbamide pulp fills the filtration chambers 52', where the leaching solution is squeezed from the cake, and then fed to the collecting tank 53 'and then transported to the concentrate pulp in the contact vessel 13 of the module 2. Silver recovery to the solution from the concentrate 97% of gold 89.5% Keki of the first agitation leaching plant, containing silver 2 g / t, gold 3.3 g / t, are fed to the second leaching plant in a contact tank 50 ", where they are pulped to a mass fraction of solid in the pulp of 25% Thiourea solution from module 5.

The resultant pulp is agitated for 4 hours and then fed to a filter press 51 ", where the leach solution is pressed from the cake and fed to the collecting tank 53, from where it is transported to the contact vat 50 'for the dislocation of the filtration leaching cakes.

The extraction of silver into the solution from the concentrate amounted to 98.0% of gold - 93.2 The content of metals in the quark: silver 260.0 g / t, gold 1.3 g / t.

Keki of the second stage of agitation leaching is washed in the filter press 51 "from thiourea with water, the filtrate after evaporation is fed to the collecting tank 53", and the cakes are discharged from the filter press 51 "and dumped into the heap.

Thus, the proposed line when processing rich sulfide silver-containing flotation concentrates allows to increase the degree of silver recovery in the leaching solution and commercial product and, in addition, due to the non-stop circulation of the thiourea solution during the processing, allows processing with a smaller volume of the solution. This in turn allows to reduce the costs of processing the initial concentrate, as well as the volumes and metal consumption of the equipment and, as a consequence, improve the processing efficiency.

CLAIM

1. A line for processing flot concentrates containing silver predominantly in the form of sulphides, including the module for grinding the concentrate, the agitation leaching module, the grouting module and the module for cleaning and conditioning the unmethodated solution, which are installed along the process and connected by means of vehicles having pipelines, Characterized in that it is provided with a filtration leach module installed after the grinding module and an electrolysis module for filtration leach solutions placed in front of the carburizing module, wherein the concentrate leachate leaching module is connected to the grinding module, the filter cake transporting means is connected to the agitation leaching module, and the pipelines Of the filtrate vehicles and of the unmetered solution is connected to a closed circuit with the electrolysis module, the electrolysis module is connected via a pipeline to the module for cleaning and conditioning the unmethodated solution, which is connected to the agitation leaching module by the pipeline and the latter by a pipeline of poor silver-containing solutions with a filtration leaching module.

2. A line according to claim 1, characterized in that the filtration leaching module is in the form of a filter press with horizontal chambers, a leach solution supply tank and a contact pan for ripulosing the concentrate, connected to the filter press, respectively, by the solution and pulp piping, and the collector tank A rich silver-containing solution, a pipeline connected to the filter press.

3. A line according to claim 1, characterized in that the electrolysis module is made in the form of two electrolyzers with plate and carbon graphite cathodes installed in a cascade and connected to each other by a pipeline and a tank of a disinfected solution.

4. A line according to claim 1, characterized in that the cementation module is arranged one above the other with the possibility of rearranging at least two cementers, each of which is a container with a compressed stack of alternating layers of cement metal and a graphitized batting located between the nozzles Input and output of the solution.

5. A line according to claim 1, characterized in that the cleaning and conditioning module of the unmethodated solution is made in the form of a lime treatment contact cup and a filter press with vertical frames connected to each other by a pipeline and a contact solution conditioning vessel connected to the filter press by a conduit .

6. A line according to claim 1, characterized in that the agitation leaching module is at least one contact vessel and a filter press with horizontal chambers connected to each other by a conduit and a collecting tank of a poor silver-containing solution connected to the filter press by a conduit .

print version
Date of publication 14.03.2007gg

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