RU2568223C2 - Extraction method of metals, mainly nickel and cobalt, from oxidised ores - Google Patents

Abstract

FIELD: metallurgy.

SUBSTANCE: metal extraction method involves ore leaching by continuous multistage counter flow heap leaching. At each intermediate stage there supplied is a leaching solution prepared using a mother solution obtained at the next leaching stage of the previous heap. At the last stage there supplied is an initial leaching solution. The mother solution obtained at the first stage is supplied for processing as a productive solution. Leaching is performed with the number of stages, which provides for the reduction of acidity of mother solutions obtained at the first stages to the level required for the first processing stage of productive solutions, or in addition, these mother solutions are subject to neutralisation by their filtration on a heap of another rock. Processing of the productive solutions is performed stage-by-stage using ion-exchange sorbents at several stages so that an eluate is obtained at each stage, which is saturated with the metal corresponding to this stage and depleted with other metals.

EFFECT: improving complete extraction of nickel and cobalt from low-quality ore and/or from small deposits at low material and energy consumptions.

63 cl, 14 dwg, 9 tbl

Description

The present invention relates to hydrometallurgy, in particular to the hydrometallurgical extraction of nickel, cobalt and other metals from oxidized ores. The present invention is a method for the extraction of Nickel, cobalt and other metals from oxidized ores, which apply the technology of leaching of ores by leaching solutions prepared using an acid belonging to the group comprising hydrochloric acid, sulfuric acid, nitric acid and acids formed by the vital activity of bacteria, to obtain productive leaching solutions, as well as the technology of processing productive leaching solutions using the ion-exchange process in.

Oxidized ores, for example ores called laterites, are known to contain limonite (a ferruginous type of ore) and saprolite (a magnesian type of ore), are the largest potential sources of nickel (Ni) and cobalt (Co) in the world.

These ores cannot be subjected to magnetic separation or foam flotation, in contrast to ferronickel sulfide ores, which can easily be concentrated to a sufficiently high nickel level using well-known methods such as foam flotation and matte smelting. Unsuitable for enrichment by conventional methods leads to the uneconomical development of oxidized nickel ores.

One of the processes for the extraction of nickel and cobalt from oxidized ores is the well-known Moa Bay process, which involves acid leaching at elevated temperatures and pressures, at which iron oxide and aluminum oxysulfate are largely insoluble (Reznik I.D., Ermakov G.P. ., Schneerson, Ya.M. Nickel. M.: Science and Technology LLC, 2001. Vol. 2: Oxidized Nickel Ores). A brief description of the Moa Bay process is given in the "prior art" section of the patent specification US 4097575 (C01G 53/10; publ. 1978.06.27). In the Moa Bay process, laterite ore with a fineness of minus 20 mesh (95 percent of the material passes through a 325 mesh American Standard sieve) is converted to pulp with a solids content of approximately 45 percent, and nickel and cobalt are selectively leached with sufficient sulfuric acid (H ₂ SO ₄ ) at elevated temperatures and pressures (e.g., at 230 ° C ÷ 250 ° C and an overpressure of 405 lb / ⁱⁿ² to 580 lb / ⁱⁿ² (28.5 kg / cm ² to 40.8 kg / cm ²⁾ in order to dissolve about 95 percent of both nickel and cobalt in 60 minutes ÷ 90 minutes. To relieve pressure, the leached pulp is washed with counterflow decanting and the washed pulp is dumped, and then the leach solution, which has a fairly low pH value (for example, between 0 and 0.5), is neutralized by coral sludge to a pH of about 2.4 in series of four tanks with a total residence time of approximately 20 minutes, and the liquid product thus treated (containing approximately 5.65 g / l of nickel, 0.8 g / l of iron and 2.3 g / l of aluminum) after separation of solid and liquid fractions exposed tsya sulfide precipitation. In an autoclave at a temperature of about 120 ° C (250 ° F) and a pressure of about 150 lb / ⁱⁿ² (10.55 kg / cm ²⁾ leaching liquid is heated and held sulphide precipitation using hydrogen sulphide (H ₂ S) as the precipitating reagent. In the initial mixed sulphide treatment scheme, the sulphide precipitate was washed and settled to a solids content of approximately 65 percent. It was then oxidized in an autoclave at a temperature of about 177 ° C (350 ° F) and a pressure of about 700 lbs / ⁱⁿ² (50 kg / cm ^2). Then this solution containing nickel and cobalt was neutralized with ammonia (NH ₃ ) to obtain a pH value of 5.35, sufficient to almost completely precipitate the residual iron, aluminum (Al) and chromium (Cr), using air as an oxidizing agent. After that, the precipitate was separated from the solution, and the solution of nickel and cobalt was adjusted to a pH value of approximately 1.5. To selectively precipitate all present impurities of copper (Cu), lead (Pb), and zinc (Zn), H ₂ S was introduced. The precipitate was separated from the solution by filtration and nickel was recovered by various methods, one of which was the treatment of a nickel-containing solution with hydrogen (H ₂ ) at elevated temperature and pressure to obtain nickel powder. Some laterite ores, in particular saprolite ores, usually have a high magnesium (Mg) content and a relatively low iron content compared to limonite, which has to be fought to efficiently remove nickel from the leached solution and to separate nickel from iron, magnesium and other impurities. A typical laterite with a high content of magnesium and iron usually contains by weight at least 5 percent magnesium and even, for example, 10 percent or more. The Moa Bay process is not suitable for the treatment of such ores, since an unacceptably high consumption of sulfuric acid is required due to the high content of magnesium in the form of magnesium oxide (MgO). A common industrial practice is the smelting of high-quality saprolite ores, usually containing more than 2 percent nickel, to produce either ferronickel or nickel matte. As regards limonite, in this case, nickel is recovered from the ore by high pressure leaching using sulfuric acid as the leaching agent and / or reducing calcination followed by ammonia leaching. Acid leaching of saprolite ore until recently was not commercially available because the process of nickel extraction from the leaching solution was not developed, which would be simple and economical. Nickel and cobalt were recovered from ocher ore (limonite) mainly by high pressure leaching using sulfuric acid as a leaching agent and / or reducing calcination followed by ammonia leaching. However, the process of autoclaved sulfuric acid leaching (HPAL) and ammonia-carbonate leaching, carried out at atmospheric pressure, have several disadvantages:

- the complexity of the hardware design, which leads to high investment;

- high energy consumption;

- the complexity of the process;

- the thickening of the original ore and autoclave pulps, which is an important factor for the capital intensity of the technology.

A known method for the extraction of Nickel, cobalt and other metals from laterite ores, disclosed in the description of the patent of the Russian Federation for invention No. 2418873 (C22B 23/00; C22B 3/24; publ. 2011.05.20). The disadvantage of this method is that copper, iron and aluminum are recovered at the same stage of ion-exchange extraction. This leads to unnecessary load on the ion exchange resin from aluminum and iron. At the same stage, the neutralization of the productive leaching solution is carried out. In the next step of ion-exchange extraction, nickel and cobalt are extracted together. The disadvantage is that the separation of nickel and cobalt requires the use of additional technologies. Also, this method does not provide for the integration of the processing of a productive leaching solution with leaching processes, for example, by recycling a portion of the solutions in the leaching-processing cycle as a whole. Ore roasting is not provided, which limits the degree of conversion of metals from ore to productive solution.

A known method for the extraction of Nickel, cobalt and other metals from laterite ores disclosed in the description of the patent of the Russian Federation for invention No. 2393250 (C22B 23/00; C22B 3/06; publ. 2010.06.27). According to this method, the ore is crushed and divided into two fractions, small and large. Fractions are granulated individually using acid solutions. Leaching, for example in heaps, is carried out in two process streams. In this case, the productive solution obtained by leaching the fine ore in one process leach stream is fed to the preparation of the leach solution to leach the large fraction ore in another process stream. The mass ratio of ore to acid solution is maintained equal to 1: 3. The neutralization of the productive solution is carried out, in particular, by the introduction of the processed ore. Metals are extracted from the neutralized productive solution by its processing using sorption processes. Part of the raffinate from the sorption stage of nickel and cobalt containing magnesium and iron is sent to the preparation of the leach solution, another part is sent for recycling. The disadvantage is that the method does not provide for the extraction and utilization of copper and does not disclose the steps for extracting magnesium and iron from the raffinate of sorption of nickel and cobalt. Nor is ore firing provided, which limits the degree of conversion of metals from ore to productive solution.

In accordance with the description of the patent of the Russian Federation for invention No. 2149910 (C22B 23/10; publ. 2000.05.27), a method is known for extracting nickel and other metals from oxidized ores, including leaching of ore at atmospheric pressure and ordinary temperatures. High magnesium lateritic ores (e.g., saprolite), such as Ni-Fe-Mg-containing ores, containing by weight at least about 5% magnesium, at least about 10% iron, and at least 0.5% nickel, leached in heaps, in tanks or leached with stirring ore with mineral acids, for example, hydrochloric acid (HCl), sulfuric acid and nitric acid (HNO ₃ ). Following the dissolution of nickel, the pH of the leach solution is adjusted to approximately 1 to 3 using the magnesium and iron oxides formed in this process or fresh ore. After separation of the solid phase from the leach solution, the solution is treated with an ion exchange resin, in particular a resin manufactured by Dow Chemical, called XFS-4195, on which nickel is selectively absorbed and nickel-depleted solution (raffinate) or rinse water returned to the leach system for its reuse. When hydrochloric or nitric acid is used as the leaching agent, nickel chloride or nickel nitrate is formed, followed by concentration by ion exchange. A solution of nickel chloride or nickel nitrate is subjected to pyrohydrolysis to obtain nickel oxide and a secondary acid, for example hydrochloric acid or nitric acid. Secondary acid can be used to prepare the leach solution and to prepare a stripping solution for the desorption step of nickel with nickel-loaded ion exchange resin. Pyrohydrolysis allows the isolation of magnesium oxide or iron oxide, which can be reused to adjust the pH of the leach solution to a level of about 1 ÷ 3 for nickel extraction by ion exchange. Pyrohydrolysis also allows the reduction of MgO solely as a by-product or product used to neutralize when the raffinate rises to 6 or 7 in order to precipitate and separate iron and other impurities. The solution of magnesium chloride (MgCl ₂ ) obtained after filtration is a mother liquor for pyrohydrolysis. Nickel oxide resulting from pyrohydrolysis can be used to produce metallic nickel, or nickel oxide in combination with iron oxide can be used to produce ferronickel. The disadvantage of this method is the stage of neutralization of a rich leach solution (productive leach solution) with oxides of magnesium and iron, which is accompanied by precipitation and partial withdrawal from acid turnover, loss of magnesium. Extraction of copper and cobalt is not provided. Ore roasting is not provided, which limits the degree of conversion of metals from ore to productive solution. The method disclosed in the description of the patent of the Russian Federation No. 2149910, does not allow to solve the problem of complex processing of oxidized nickel ore with reasonable labor, materials and energy.

The closest analogue of the invention is a method for the extraction of nickel and other metals from oxidized ores, disclosed in the description of the patent of the Russian Federation for invention No. 2355793 (C22B 23/00; C22B 3/08; publ. 2009.05.20). This method involves leaching the initial oxidized ore with prepared leaching solutions to produce productive solutions and processing the productive solutions. This method uses a continuous multi-stage countercurrent heap leaching method of extracted ore. It is intended to grind (crush) the initial mined ore and divide it into fractions, sintering (agglomeration). The disadvantage is that the method does not disclose in detail the stages of processing the productive leach solution. It is only indicated that the productive solution can be processed using known technologies, including ion exchange. Therefore, it is not envisaged to optimize the production process as a whole, in the relationship of the parameters of the process of obtaining a productive solution and the parameters of the process of processing a productive solution. Nor is ore firing provided, which limits the strength of the particles of agglomerated ore and limits the degree of conversion of metals from ore to productive solution. Washing of leached heaps and their further use is not provided.

The problem to which the invention is directed, is the creation of such a method for the extraction of nickel, cobalt and other metals from oxidized ores, carried out using technology for leaching at atmospheric pressure and ordinary temperature and processing technologies for productive leaching solutions using ion-exchange processes and sorbents, which will provide the most complete extraction of nickel and cobalt from low-grade (poor) ore and / or from small deposits at low cost material s and energy, and with a high degree of regeneration of materials and recycling of reagents used. In general, it was necessary to develop a more competitive method for the extraction of nickel and cobalt from oxidized ores, less demanding on capital costs and operating costs than the well-known established technological routes. Moreover, the method should ensure the extraction of copper, saving acid and simplifying the process of processing the productive solution, in comparison with the known analogues. The task of obtaining a nickel product of a high degree of purification from impurities was also set, and the purification of a nickel product from impurities should be performed as an integral part of the processing of productive solutions, and not as an additional (optional) operation. Also, the method should reduce the harmful effects of production on the environment. In private implementations, the method should ensure that the content of magnesium and iron in the circulating solutions is not higher than the acceptable levels, to ensure the removal of excessive amounts of magnesium and iron from the circulating solutions. In particular cases, additional integration tasks were set in one method of heap multi-stage counterflow leaching of extracted ore and underground ore leaching technology at the site, and in optimizing the parameters of such integration. In addition, the proposed method will expand the whole arsenal of hydrometallurgical technologies used to extract nickel, cobalt and other metals, as well as expand the arsenal of its individual technological processes.

The specified problem in the General case of the invention is solved as follows.

A method for extracting nickel, cobalt and other metals from oxidized ores includes: preparing leaching solutions containing an acid belonging to a group comprising hydrochloric acid, sulfuric acid, nitric acid, and acids formed by the vital activity of bacteria; leaching of the initial oxidized ore with prepared leaching solutions to obtain productive solutions; processing of productive solutions. The method is characterized in that the initial oxidized ore contains mined oxidized ore, leaching the mined oxidized ore is performed in the form of continuous multi-stage countercurrent heap leaching. In this case, the extracted oxidized ore is subjected to preliminary crushing. Crushed ore is agglomerated. Agglomerated ore is calcined. At least one heap sequence is formed from the calcined agglomerated ore. Each heap is subjected to at least two leaching stages. In each heap sequence, for each heap in the first stage of its leaching, a leach solution prepared from the mother liquor obtained in the second stage of leaching of the previous heap is fed. At each intermediate stage of its leaching, a leach solution prepared from the mother liquor obtained in the next stage of leaching the previous heap is fed. At the last stage of its leaching, an initial leach solution intended for heap leaching is fed. At the end of the last stage of its leaching, it is washed. The mother liquor obtained in the first stage of its leaching is fed for processing as a productive solution or as part of a productive solution. Continuous multi-stage countercurrent heap leaching is performed with such a number of stages that ensures the acidity of the mother liquors obtained in the first stages of heap leaching to the level necessary for the first stage of processing of productive solutions, or these mother liquors are additionally neutralized to the specified required acidity level by filtering on a heap of another breed before serving them for processing. Processing of productive solutions is carried out in stages using ion-exchange sorbents and ion-exchange processes, arranged in several stages, to obtain at each stage of processing an eluate enriched with metal corresponding to this stage of processing and depleted in other metals compared to the metal content in productive solutions and in eluates obtained on other stages of processing. At least one eluate obtained at the corresponding processing stage is purified from impurities to obtain a purified eluate, and the eluate is prepared with a saturation of the corresponding ion-exchange sorbent by supplying a portion of the obtained purified eluate to it. At least part of the solutions formed during processing, in which the acidity and impurities are preserved in dissolved form, and the nickel concentration does not exceed 0.3 g / l, are sent to leaching the heap and then to the preparation of leaching solutions. At least a portion of the solutions resulting from the processing is neutralized to obtain insoluble compounds of iron and other metals, and these insoluble compounds are separated from at least a portion of these neutralized solutions by filtration on a leached and washed heap or on a heap of another breed.

In all implementations of the invention, the common with the closest analogue is that the method of extraction of Nickel, cobalt and other metals from oxidized ores, including the preparation of leaching solutions containing acid belonging to the group comprising hydrochloric acid, sulfuric acid, nitric acid and acids formed by life bacteria, leaching of the initial oxidized ore by prepared leaching solutions to obtain productive solutions and processing of productive solutions, characterized The initial oxidized ore contains mined oxidized ore, the leaching of the mined oxidized ore is performed as continuous multi-stage countercurrent heap leaching, it is preliminarily crushed, the crushed ore is agglomerated, at least one heap sequence is formed from the agglomerated ore, each the heap is subjected to at least two stages of leaching, in each sequence of heaps for each heap in the first stage of its leaching, a leaching solution is fed, made from the mother liquor obtained in the second stage of leaching the previous heap, at each intermediate stage of its leaching, the leaching solution is prepared from the mother liquor obtained in the next stage of leaching the previous heap, and the initial leaching solution for heap leaching is fed at the last stage of leaching , at the end of the last stage of its leaching, it is washed, and the mother liquor obtained in the first stage of its leaching is fed to Processing as a productive solution or as an integral part of a productive solution, processing of productive solutions is carried out in stages using ion-exchange sorbents and ion-exchange processes, arranged in several stages, to obtain at each stage of processing an eluate enriched with a metal corresponding to this stage of processing and depleted in other metals by compared with the metal content in productive solutions and in eluates obtained at other stages of processing.

In all implementations, the present invention differs from the closest analogue in that:

- agglomerated ore is preliminarily fired before forming heap sequences from it;

- perform continuous multi-stage countercurrent heap leaching with such a number of stages that provides a decrease in the acidity of the mother liquors obtained in the first stages of heap leaching to the level necessary for the first stage of processing of productive solutions, or these mother liquors are additionally neutralized to the specified required acidity level by filtering them on a pile of another breed before serving them for processing;

- at least one eluate obtained at the corresponding processing stage is purified from impurities to obtain a purified eluate, the preparation of this eluate being carried out with the saturation of the corresponding ion-exchange sorbent by feeding part of the obtained purified eluate to it;

- at least part of the solutions formed during processing, in which the acidity and impurities are preserved in dissolved form, and the nickel concentration does not exceed 0.3 g / l, are sent to leaching the heap and then to the preparation of leaching solutions;

- at least a portion of the solutions resulting from the processing is neutralized to obtain insoluble compounds of iron and other metals and these insoluble compounds are separated from at least a portion of these neutralized solutions by filtration on a leached and washed heap or on a heap of another breed.

In an improved implementation, this task is additionally solved, and the invention further differs in that:

- heaps form a height of 1 m ÷ 12 m;

- heap leaching is performed in at least one process stream;

- mother liquors obtained at different stages of heap leaching are collected in separate containers;

- the initial leach solutions intended for heap leaching are prepared with an acid concentration of 0.2 mol / l ÷ 2 mol / l and served on the surface of the heaps in the last stage of leaching, with an irrigation density of 10 l / h / m ² ÷ 20 l / h / m ² ;

- the mother liquor obtained at each, except for the first, stage of leaching of the heap, is fed to irrigate the surface of another heap located in the previous stage of leaching, with an irrigation density of 10 l / h / m ² ÷ 20 l / h / m ² ;

- heap leaching is performed in such a number of stages and in such a number of streams that, in at least one stream, the pH of the mother liquor obtained directly in the first leaching stage or after additional neutralization on a pile of another rock is from 1 to 3;

- as a productive solution or as part of a productive solution, a mother liquor with a pH value of 1 to 3 is obtained for processing, obtained in the first stage of one heap leaching process stream directly or after additional neutralization on a heap of another rock, or a pH value of 1 to 3 mixture of mother liquors obtained in the first stages of heap leaching in several process streams directly or after additional neutralization on a heap oh breed;

- as stages of processing a productive solution, at least a copper extraction step, a nickel extraction step, a cobalt extraction step are performed;

- as the first stage of processing the productive solution, the stage of copper extraction by the ion exchange method is performed, moreover, a sorbent capable of selectively extracting copper from a solution with a pH value from 1 to 3 is used as a sorbent;

- at the first stage of the copper extraction step, a copper-loaded sorbent and copper sorption raffinate are obtained;

- at the second stage of the copper extraction step, copper eluate is obtained from the copper-loaded sorbent by desorption of copper;

- copper eluate is fed to obtain copper-containing products;

- raffinate of copper sorption is fed to the second stage of processing the productive solution, which is performed as the stage of nickel extraction by ion exchange method;

- in this case, the nickel eluate is obtained as an eluate, which is purified from impurities to obtain a purified eluate and the preparation of which is carried out with the saturation of the corresponding sorbent by feeding part of the obtained purified eluate to it;

- the nickel extraction step is performed in two steps, the nickel eluate with impurities is obtained in the first step of the nickel extraction step, the impurities are cleaned of nickel eluate in the second step of the nickel extraction step;

- at the first stage of the first stage of the nickel extraction stage, a sorbent loaded with nickel contaminated with impurities and a nickel sorption raffinate are obtained;

- in the second stage of the first stage of the nickel extraction stage, the sorbent loaded with nickel is saturated with nickel and partially purified from impurities by supplying purified nickel eluate to it to obtain a saturated sorbent and saturation raffinate contaminated with impurities;

- in the third stage of the first stage of the Nickel extraction stage, nickel eluate is obtained from a desaturated sorbent by desorption with a nickel-containing solution;

- in the fourth stage of the first stage of the stage of extraction of Nickel from the sorbent receive Nickel secondary eluate by desorption with an acid solution;

- secondary nickel eluate is fed to the preparation of a nickel-containing solution for the third stage of the first stage of the Nickel extraction stage;

- the saturation raffinate is supplied as a solution in which acidity and impurities are preserved in dissolved form, for washing the leached heap and then for preparing leaching solutions;

- Nickel eluate is fed to the second stage of the Nickel extraction step;

- the raffinate of nickel sorption is divided into parts, while part of the raffinate of nickel sorption is fed to washing the leached heap and then to prepare leaching solutions, and the other part of the raffinate of nickel sorption is neutralized to obtain insoluble compounds of iron and other metals, and at least part of this another portion of the nickel sorption raffinate is neutralized using at least one of the materials belonging to the group comprising magnesium oxide, brucite, magnesite, and the neutralized portion of the sorption raffinate is fed of nickel to cobalt extraction step;

- at the first stage of the second stage of the nickel extraction stage, nickel eluate is purified by iron sorption, and a sorbent loaded with iron and other impurities and purified nickel eluate are obtained as an iron sorption raffinate;

- the purified nickel eluate is partly fed to the second stage of the first stage of the nickel extraction stage, partly is fed to prepare a nickel-containing solution for the third stage of the first stage of the nickel extraction stage, and partly is used to produce nickel-containing products;

- the iron-loaded sorbent is washed from nickel and fed to the step of desorption of iron with an acid solution to obtain a glandular eluate and washed sorbent;

- ferrous eluate is served as a solution in which acidity and impurities are preserved in dissolved form, for washing the leached heap and then for the preparation of leaching solutions;

- at the first stage of the cobalt extraction step, a cobalt-laden sorbent and cobalt sorption raffinate are obtained;

- the sorbent loaded with cobalt is fed to the stage of cobalt desorption with an acid solution to obtain cobalt eluate and the sorbent unloaded from cobalt;

- cobalt eluate is fed to produce cobalt-containing products;

- at least a portion of the cobalt sorption raffinate is fed as a solution neutralized to obtain insoluble compounds of iron and other metals to the washed leached heap or to a heap of another rock with separation of these insoluble compounds by filtration on a washed leached heap or on a heap of another breed, and to obtain a magnesium solution;

- the solution obtained by washing the leached heap is fed to the preparation of leaching solutions.

It is understood that:

- the term “ore crushing” means any grinding of ore used in the industry;

- the term “agglomeration” covers the terms “granulation”, “pelletizing”, “agglomeration”, “pelletizing”, etc., known in the industry;

- the term "solution" can be used in relation to pulp;

- the term "process stream" means in a broad sense a technological or production line or chain, thread, etc .;

- as containers for collecting the mother liquor leaching can be used, among other things, ponds, pools, etc .;

- for brevity of description in the text, abbreviated terms may be used in those cases where the abbreviation is obvious to a specialist, for example: “acid” instead of “acid solution”; “Solution” instead of “aqueous solution”; “Leached heap” instead of “leached ore heap”; “Nickel extraction step” instead of “the step of processing a productive solution in which nickel is recovered”, etc .;

The term "extraction" depending on the context may mean, in particular, "extraction from ore into a solution", "extraction from a solution into a sorbent", "extraction from a sorbent in an eluate".

In relation to the first stage of continuous multi-stage countercurrent heap leaching, the term “neutralization stage” can be used (for example, in the attached schemes), since at this stage the most significant decrease in the acidity of the mother liquor is achieved.

Also, for brevity, the abbreviations OR (oxidized ores), BP (leaching solution), PR (productive solution), KB (heap leaching), PV (underground leaching), W / T (volume ratio) can be used in the text of the present description and in the accompanying drawings. liquid to the mass of the solid phase).

It is assumed that in the proposed method, the heap sequence can be formed not only as separate heaps, but also as a composite heap, parts of which are leached sequentially in the same order in which the heap sequence is leached.

In the 1st particular case, the proposed method further differs from the improved implementation in that the extracted iron ore of the technological type is used as the whole oxidized ore mined.

In the first refinement of the first particular case, the proposed method is additionally characterized in that the initial leach solutions intended for heap leaching are prepared with an acid concentration of ~ 0.5 mol / l with a ratio of the solution to ore W / T from 1.5 m ³ / t to 3 m ³ / t.

In the second refinement of the first particular case, the proposed method is additionally characterized in that the crushing of the extracted ore of ferrous technological type is performed up to a class of 5 mm.

In the third refinement of the first particular case, the proposed method further differs in that the agglomeration of the crushed mined iron ore of technological type is performed until granules of 10 mm ÷ 20 mm in size are added with at least 0.1% ÷ 2% sodium chloride, 0 , 5% ÷ 5.5% elemental sulfur, 5% ÷ 15% water or industrial water by weight of ore.

In the fourth refinement of the first particular case, the proposed method is further characterized in that the sintering of the crushed mined ore of a ferrous technological type is performed at a temperature of 300 ° C ÷ 700 ° C and when supplying sharp steam with a temperature of 100 ° C ÷ 200 ° C.

In the 2nd particular case, the proposed method further differs from the improved implementation in that the mined ore of the magnesian technological type is used as the whole oxidized ore mined.

In the first refinement of the 2nd particular case, the proposed method is further characterized in that the initial leach solutions intended for heap leaching are prepared with an acid concentration of ~ 0.5 mol / l with a ratio of the solution to ore W / T from 1.5 m ³ / t to 3 m ³ / t.

In the second refinement of the 2nd particular case, the proposed method further differs in that the crushing of the mined ore of the magnesian technological type is performed up to a class of 10 mm.

In the third refinement of the 2nd particular case, the proposed method is further characterized in that the agglomeration of the crushed mined ore of the magnesian technological type is carried out until granules with a size of 20 mm ÷ 40 mm are formed with the addition of 5% ÷ 15% water or industrial water from the ore mass.

In the fourth refinement of the 2nd particular case, the proposed method is further characterized in that the firing of the agglomerated crushed mined ore of the magnesian technological type is carried out at a temperature of 200 ° C to 500 ° C.

In the 3rd particular case, the proposed method further differs from the improved implementation in that the extracted ore in the form of a mixture of mined ores of ferrous and magnesian technological types is used as the entire oxidized ore mined.

In the first refinement of the 3rd particular case, the proposed method is additionally characterized in that the initial leach solutions intended for heap leaching are prepared with an acid concentration of ~ 0.5 mol / l with a ratio of the solution to ore W / T from 1.5 m ³ / t to 3 m ³ / t.

In the second refinement of the 3rd particular case, the proposed method further differs in that the crushing of the extracted ore is carried out to a class of 5 mm.

In the third refinement of the 3rd particular case, the proposed method is further characterized in that the agglomeration of the crushed ore is carried out before the formation of granules with a size of 10 mm ÷ 20 mm with additives of at least 0.1% ÷ 2% sodium chloride, 0.5% ÷ 5.5% elemental sulfur, 5% ÷ 15% water or industrial water by weight of ore.

In the fourth refinement of the 3rd particular case, the proposed method is further characterized in that the agglomerated crushed mined ore is calcined at a temperature of 300 ° C ÷ 700 ° C and when supplying sharp water vapor with a temperature of 100 ° C ÷ 200 ° C.

In the 4th particular case, the proposed method further differs from the improved implementation in that the extracted ore of ferrous and magnesian technological types, separated by types, is used as the whole extracted oxidized ore, heap leaching is performed in at least two technological streams, while mined iron ore is leached in at least one of the process streams and magnesia is mined in at least one of the process streams new technological type.

In the first refinement of the 4th particular case, the proposed method is further characterized in that the initial leach solutions intended for heap leaching are prepared with an acid concentration of ~ 0.5 mol / l with a ratio of the solution to ore W / T from 1.5 m ³ / g to 3 m ³ / t.

In the second refinement of the 4th particular case, the proposed method further differs in that the crushing of the extracted ore of ferrous technological type is carried out to a class of 5 mm.

In the third refinement of the 4th particular case, the proposed method is further characterized in that the agglomeration of the crushed mined iron ore of the technological type is carried out until granules of 10 mm ÷ 20 mm in size are added with at least 0.1% ÷ 2% salt, 0 , 5% ÷ 5.5% elemental sulfur, 5% ÷ 15% water or industrial water by weight of ore.

In the fourth refinement of the 4th particular case, the proposed method is further characterized in that the firing of the agglomerated crushed mined iron ore of technological type is performed at a temperature of 300 ° C ÷ 700 ° C and when supplying sharp water vapor with a temperature of 100 ° C ÷ 200 ° C.

In the fifth refinement of the 4th particular case, the proposed method is further characterized in that the mined ore of the magnesian technological type is crushed to a class of 10 mm.

In the sixth refinement of the 4th particular case, the proposed method is further characterized in that the agglomeration of the crushed mined ore of the magnesian technological type is carried out until granules with a size of 20 mm ÷ 40 mm are formed with the addition of 5% ÷ 15% water or industrial water from the ore mass.

In the seventh refinement of the 4th particular case, the proposed method is further characterized in that the firing of the agglomerated crushed mined ore of the magnesian technological type is carried out at a temperature of 200 ° C to 500 ° C.

In the developed implementation, the proposed method further differs from the improved implementation in that the initial oxidized ore additionally contains ore at the occurrence site, belonging to the magnesian technological type, the leaching of ore at the occurrence site is performed in the form of underground leaching to obtain the mother liquors of underground leaching and the mother liquors of underground leaching for the preparation of leaching solutions, while using these mother liquors underground leaching for the preparation of leaching solutions intended for continuous multi-stage countercurrent heap leaching, and that part of the solutions formed during processing, which is fed to the preparation of leaching solutions, is used to prepare leaching solutions intended for underground leaching, and these leaching solutions are prepared for underground leaching, with an acid concentration of at least 0.5 mol / L.

In clarification of the developed implementation, the proposed method is further characterized in that the initial leach solutions intended for heap leaching are prepared with an acid concentration of preferably ~ 0.5 mol / l with a ratio of solution to ore W / T from 1.5 m ³ / t to 3 m ³ / t, while leaching solutions intended for underground leaching are prepared with an acid concentration of preferably ~ 0.75 mol / l with a ratio of solution to ore W / T from 3 m ³ / t to 6 m ³ / t.

In the 5th particular case, the proposed method further differs from the developed implementation in that iron ore of the technological type is used as the extracted ore, and its crushing is carried out to a class of 5 mm.

In the first refinement of the 5th particular case, the proposed method is further characterized in that the agglomeration of the crushed mined iron ore of technological type is carried out before the formation of granules of 10 mm ÷ 20 mm in size with additives of at least 0.1% ÷ 2% sodium chloride, 0 , 5% ÷ 5.5% elemental sulfur, 5% ÷ 15% water or industrial water by weight of ore.

In the second refinement of the 5th particular case, the proposed method is further characterized in that the sintering of the agglomerated crushed mined iron ore of technological type is performed at a temperature of 300 ° C ÷ 700 ° C and when supplying sharp water vapor with a temperature of 100 ° C ÷ 200 ° C.

In the 6th particular case, the proposed method further differs from the developed implementation in that mined ore of a magnesian technological type is used as mined ore, and its crushing is performed to a class of 10 mm.

In the first refinement of the 6th particular case, the proposed method is further characterized in that the agglomeration of the crushed mined ore of the magnesian technological type is carried out until granules with a size of 20 mm ÷ 40 mm are formed with the addition of 5% ÷ 15% water or industrial water from the ore mass.

In the second refinement of the 6th particular case, the proposed method is further characterized in that the firing of the agglomerated crushed mined ore of the magnesian technological type is carried out at a temperature of 200 ° C ÷ 500 ° C.

In the 7th particular case, the proposed method further differs from the improved implementation in that, at the copper extraction stage, a chelate type ion-exchange resin is used as the sorbent, at the second stage of the copper extraction stage, copper desorption is performed with an ammonia solution with a pH value of at least 7 to obtain as copper eluate of a solution of copper ammonia and obtaining a sorbent purified from copper, then the sorbent purified from copper is washed from ammonium ion with water to obtain a solution of ammonium ion and regenerated sorben a.

In the first refinement of the 7th particular case, the proposed method is further characterized in that at least part of the copper ammonia solution obtained in the copper extraction step, copper is recovered by crystallization to obtain a copper salt and with the regeneration of ammonia, and at least a part regenerated ammonia is directed to the preparation of a solution of ammonia, which is the desorption of copper.

In the second refinement of the 7th particular case, the proposed method is further characterized in that the ammonium ion solution obtained by washing the copper-free sorbent is fed to the preparation of an ammonia solution that desorbs copper.

In the third refinement of the 7th particular case, the proposed method is further characterized in that the regenerated sorbent is returned to the first stage of the copper extraction step.

In the 8th particular case, the proposed method further differs from the improved implementation in that the acidity of the copper sorption raffinate is maintained in the pH range from 1 to 2, at the first stage of the nickel extraction step, a chelate-type ion-exchange resin is used as the sorbent, at the second stage of the first stage of the nickel extraction stage, purified nickel eluate with a nickel concentration of 60 g / l ÷ 90 g / l and a pH value of 1 to 2 is used as the purified nickel eluate, in the third stage of the first stage of the nickel extraction stage in As a nickel-containing solution, a nickel solution with a nickel concentration of 40 g / L ÷ 70 g / L and an acid concentration of 1 mol / L to 1.5 mol / L is used in the fourth stage of the first stage of the nickel extraction step in order to obtain a nickel eluate from a saturated sorbent. as an acid solution to obtain secondary nickel eluate from the sorbent, an acid solution with an acid concentration of 1 mol / L to 1.5 mol / L is used, then the sorbent is washed with water to obtain a regenerated sorbent and promoters, and the resulting promo is sent to the preparation acid solution for the fourth step of the first step of the nickel extraction step.

In clarifying the 8th particular case, the proposed method is further characterized in that at least a portion of the regenerated sorbent obtained by washing it with water is returned to the first stage of the first stage of the nickel extraction step.

In the 9th particular case, the proposed method further differs from the improved implementation in that an anion exchange resin AB-17x8 or a similar anion exchange resin is used as a sorbent in the second stage of the nickel extraction, and a purified nickel eluate with a nickel content of 80 g / is obtained as an iron sorption raffinate l ÷ 100 g / l.

In the 10th particular case, the proposed method further differs from the improved implementation in that from at least a portion of that portion of the purified nickel eluate obtained as an iron sorption raffinate, which is fed to nickel-containing products, nickel salt is obtained by crystallization as Nickel-containing product.

In the refinement of the 10th particular case, the proposed method is additionally characterized in that a solution of sulfuric acid is used as the acid contained in the solutions by which nickel eluate and secondary nickel eluate in the first step of the nickel extraction step are obtained by desorption, and obtained by crystallization as a nickel-containing product, a nickel salt having a composition of NiSO ₄ · 7H ₂ O.

In the 11th particular case, the proposed method further differs from the improved implementation in that from at least a portion of that portion of the purified nickel eluate obtained as an iron sorption raffinate, which is fed to nickel-containing products, cathode metal nickel is obtained by electrolysis in as a nickel-containing product.

In the 12th particular case, the proposed method further differs from the improved implementation in that from at least a portion of that portion of the purified nickel eluate obtained as an iron sorption raffinate, which is fed to nickel-containing products, metal nickel powder is obtained by electrolysis in as a nickel-containing product.

In clarifying the 9th particular case, the proposed method is additionally characterized in that the first stage of the second stage of the nickel extraction step on anion exchange resin AB-17x8 or a similar anion exchange resin is carried out at a pH of 1 to 3 of the sorbed solution, the iron-loaded anion exchange resin is washed from nickel with water to obtain a promo containing nickel, iron desorption is performed with an acid solution having an acid concentration of 0.5 mol / L ÷ 1 mol / L, then the washed anionite is regenerated with a sodium hydroxide solution with a pH value of 5 to 8 to obtain mother liquor of regeneration of anion exchange resin and regenerated anion exchange resin, then the regenerated anion exchange resin is washed with sodium ion with water until acid breakthrough in pH values from 4 to 5.

In the particular case of the refinement of the 9th particular case, the proposed method is further characterized in that the regenerated anion exchange resin washed from sodium ion is returned to the first stage of the second stage of the nickel extraction step.

In the particular case of the refinement of the 9th particular case, the proposed method is further characterized in that at least a portion of the nickel-containing product obtained by washing the iron with anion exchange resin loaded with water is added to the nickel eluate supplied to the first stage of the second stage of the nickel extraction stage.

In the particular case of the refinement of the 9th particular case, the proposed method further differs in that at least a portion of the mother liquor for regenerating the anion exchange resin is sent to prepare a solution of sodium hydroxide, which regenerates the anion exchange resin.

In the particular case of the refinement of the 9th particular case, the proposed method further differs in that at least a part of the anion exchange agent mother liquor is sent to prepare an acid solution with an acid concentration of 0.5 mol / L ÷ 1 mol / L, which is used to desorb iron.

In the 13th particular case, the proposed method further differs from the improved implementation in that they neutralize a portion of the nickel sorption raffinate supplied to the cobalt extraction step to a pH value of 3 to 5.

In the first refinement of the 13th particular case, the proposed method further differs in that as part of the nickel sorption raffinate supplied to the cobalt extraction step, a part of nickel sorption raffinate is used, in which the cobalt concentration reaches 0.8 g / l or more.

In the second refinement of the 13th particular case, the proposed method further differs in that in the cobalt extraction step an ion exchange resin is used as a sorbent, the cobalt desorption step is carried out with a mineral acid solution with an acid concentration of 0.5 mol / l ÷ 2 mol / l, preferably 1 5 mol / L.

In the private implementation of the second refinement of the 13th particular case, the proposed method further differs in that the ion-exchange resin unloaded from cobalt is washed with water and returned to the cobalt sorption stage, and the wash formed as a result of washing is directed to the preparation of a mineral acid solution, which is used during the desorption stage cobalt.

In a particular implementation of the second refinement of the 13th particular case, the proposed method is further characterized in that at least a portion of the cobalt eluate supplied to produce cobalt-containing products is obtained by crystallization of a cobalt salt.

In the third refinement of the 13th particular case, the proposed method is further characterized in that part of the cobalt sorption raffinate is fed as a solution neutralized to obtain insoluble compounds of iron and other metals to a pile of another rock with separation of these insoluble compounds on it and to obtain a magnesium solution .

In the 14th particular case, the proposed method further differs from the improved implementation in that at least a part of the magnesium solution obtained by filtering the cobalt sorption raffinate on the washed leached heap is subjected to purification from magnesium and partly serves to agglomerate the crushed ore, and part served on the preparation of leaching solutions.

In the first refinement of the 14th particular case, the proposed method is further characterized in that the purification from magnesium of at least a portion of the magnesium solution obtained by filtering the cobalt sorption raffinate on the washed leached heap is carried out by pyrohydrolysis to produce magnesium oxide and regenerated acid.

In the second refinement of the 14th particular case, the proposed method is further characterized in that the magnesium removal of at least a portion of the magnesium solution obtained by filtering the cobalt sorption raffinate on the washed leached heap is performed by crystallization to obtain a magnesium salt and water.

In the 15th particular case, the proposed method further differs from the improved implementation in that at least a part of the magnesium solution obtained by filtering the cobalt sorption raffinate on the washed leached heap is subjected to magnesium purification to obtain a solution that meets the fishery criteria for water quality , and direct him into the external environment.

In the private implementation of the first refinement of the 14th particular case, the proposed method is further characterized in that at least a portion of the regenerated acid obtained by pyrohydrolysis of the magnesium solution is returned to circulation and sent to the preparation of leaching solutions.

In the private implementation of the first refinement of the 14th particular case, the proposed method is further characterized in that at least a portion of the regenerated acid obtained by pyrohydrolysis of the magnesium solution is returned to circulation and used in the processing of productive solutions.

In the private implementation of the first refinement of the 14th particular case, the proposed method is further characterized in that at least a portion of the magnesium oxide obtained by pyrohydrolysis of the magnesium solution is used when performing neutralization to obtain insoluble compounds of iron and other metals of that part of the nickel sorption raffinate, which is fed to the cobalt extraction step.

In the 16th particular case, the proposed method further differs from the improved implementation in that, to make up for the loss of water in circulation, use water from available sources without further purification and add it to at least one of the following solutions: nickel sorption raffinate; cobalt sorption raffinate; solutions purified from magnesium, directed to the agglomeration of crushed ore or to the preparation of leaching solutions.

The features of the invention, common with the features of the closest analogue, provide the implementation of the purpose of the technical solution.

Distinctive features in combination with common features ensure the achievement of technical results.

Firing of agglomerated ore increases the proportion of soluble metal compounds in the ore, increases the degree of extraction of nickel and other metals, and increases the strength of ore granules. Strong ore granules increase the speed and uniformity of the movement of the solution in the heap, which reduces the proportion of heap sections that “fall out” of the leaching process. The maximum acceptable heap height increases (up to 12 m versus 7 m characterizing the closest analogue).

Reducing the acidity of the mother liquors obtained in the first stages of heap leaching, directly or with additional neutralization on a heap of another breed, to the level necessary for the first stage of processing of productive solutions, allows to simplify and reduce the cost of construction and installation of a processing section of a productive solution, since neutralization of the incoming productive solution at the processing site. The costs of neutralizing materials and the disposal of neutralization waste at the processing site are prevented, since the neutralization of these mother liquors is achieved along with the leaching of metals, or due to the free neutralizing resource of another breed (spent rock, etc.). At the same time, preliminary roasting of ore pellets (and the ability to increase the height of the heaps) speeds up the leaching and neutralization, reduces the number of heap leaching stages necessary for a given level of neutralization.

Obtaining a purified metal eluate allows the use of a purified eluate to saturate the sorbent loaded with this metal. In the process of this saturation, the impurity ions transferred to the sorbent from the sorbed solution together with the metal pass into the saturation solution (into the purified metal eluate). As a result, the efficiency of the sorption cycle for this metal increases. This increase in sorption efficiency is especially important in the proposed method, since a relatively high content of contaminants in the processed solutions is possible in comparison with the known methods, which include the operation of preliminary neutralization of the incoming productive solution at the processing site, accompanied by the deposition of part of the impurities. In the proposed method, the preservation of contaminants in the productive solution is involved in achieving a technical result. Impurities (and acid) are partially involved in the circulation of solutions, returned from processing to the preparation of leaching solutions. The presence of impurities in the prepared leach solution prevents the further transfer of impurities from ore to the leach solution at the leaching stages, and increases the proportion of metals in the extracted mass. The limitation of the concentration of nickel to not more than 0.3 g / l in the resulting solutions, which are sent from processing to the preparation of leaching solutions, is on average optimal, balanced, established experimentally taking into account the effect of this concentration on the requirements for the parameters of the stages of processing a productive solution. The decrease in nickel concentrations to values less than 0.3 g / l is difficult due to the increased content of impurities in the processed solutions (not counting the purified eluates), which is allowed by the proposed method.

The neutralization of the solutions formed during processing to obtain insoluble compounds of iron and other metals is performed to the extent necessary to reduce the concentration of iron, given that these solutions or part of them after separation of these insoluble compounds can be further directed to the preparation of leaching solutions, or for the agglomeration of crushed ore, or in the environment. The separation of these insoluble compounds by filtration on a washed leached heap or on a pile of another breed can reduce the cost of separating these insoluble compounds and their disposal and disposal, since it is not necessary to install filter equipment. In addition, precipitating, these compounds close the pores on the surface of the particles of leached ore or other rocks. As a result, the rate of migration of harmful substances from ore or rock particles to the environment decreases, and the costs of land restoration are reduced.

The formation of heaps more than 12 m in height leads to a violation of uniformity and a decrease in the degree of leaching of ore at the base of the heap. The formation of heaps less than 1 m high leads to an undesirable increase in the area occupied by the heaps, to an increase in evaporation losses in the dry season and to an excess supply of water in the wet season, as well as to the complication of irrigation equipment.

Performing heap leaching in at least one process stream allows you to use not only one, but if necessary two or more streams and leach different types of ore in different streams, which allows you to optimize leaching processes for each technological type of ore.

Washing the heaps with solutions preserving residual acidity, and subsequent filtering on the washed heaps of solutions containing insoluble compounds, is carried out with solutions of decreasing acidity (from washing to filtering), which increases the efficiency of the neutralization of production waste.

Collecting the mother liquors obtained at different stages of heap leaching in separate containers facilitates the optimal selection of the parameters of the leach solution for each leach stage.

The preparation of stock leach solutions intended for heap leaching with an acid concentration in the range of 0.2 mol / L ÷ 2 mol / L allows you to save acid and limits the corrosion load on the equipment. At a concentration of less than 0.2 mol / L, the leaching rate is unacceptably reduced. At a concentration of more than 2 mol / L, the costs of maintaining equipment performance are unacceptably increased, and the consumption of acid for the extraction of metals also increases.

The heap irrigation density at each leaching stage in the range of 10 l / h / m ² ÷ 20 l / h / m ² corresponds to the rate of leach solution leaking through the heaps formed from ore pellets subjected to calcination in accordance with the proposed method (including implementations in which as a leach solution, any other than the last leaching stage is fed directly to the mother liquor obtained in the next leach stage of the previous heap).

Performing heap leaching in such a number of stages and in such a number of streams that, in at least one stream, the pH of the mother liquor obtained directly at the first leaching stage or after additional neutralization on a heap of another rock is from 1 to 3, allows you to start processing of this mother liquor as a productive solution without carrying out preliminary neutralization at the processing site, while at the first stage of processing available and on-exchange sorbents with good selectivity properties for the extracted metal from solutions with a pH from 1 to 3.

Submission for processing as a productive solution having a pH value from 1 to 3 of the mixture of mother liquors obtained in the first stages of heap leaching in several process streams directly or after additional neutralization on a heap of another breed, allows you to use the mother liquor of one of the process streams with a pH value less than 1 without additional neutralization, if the pH of the mixture of mother liquors falls within the range from 1 to 3.

The implementation as the stages of processing the productive solution in its improved implementation of at least the copper extraction stage, the nickel extraction stage, the cobalt extraction stage, provides additional copper extraction.

The implementation as the first stage of processing the productive solution of the stage of extraction of copper by ion exchange, together with the use of a sorbent capable of selectively extracting copper from a solution with a pH value of 1 to 3, avoids the preliminary neutralization of the productive solution at the processing site, since the indicated range of pH values sorbed solution from 1 to 3 is more favorable for the extraction of copper than for the extraction of Nickel and cobalt using known ion-exchange materials and METHODS.

Performing the nickel extraction step as the second stage of processing the productive solution allows you to take advantage of the fact that the copper extraction stage is accompanied by a decrease in the raffinate acidity compared to the acidity of the productive solution, and therefore, no additional neutralization of the copper extraction raffinate is required before it is fed to the nickel extraction stage.

Performing the nickel extraction stage in two stages allows combining nickel extraction in the first stage and iron extraction in the second stage in one processing stage of the productive solution, and at the same time to obtain purified nickel eluate as a result of iron extraction from nickel eluate, using purified nickel eluate in the first stage the stage of extraction of Nickel as a solution for the saturation loaded with Nickel sorbent.

Feeding part of the nickel sorption raffinate for leaching of the leached heap, provides a partial decrease in the acidity of the leached ore, as a result of which the harmful effect of the leached ore on the environment is reduced. Washing each heap after the last stage of its leaching is completed with a portion of the nickel sorption raffinate and further supplying this part of the raffinate to the preparation of the leach solution allows the acid retained by the leached heap to be returned to circulation.

The leaching of the leached heap raffinate of nickel sorption is preferably provided provided that the concentration of cobalt in it does not exceed, for example, 0.8 g / l, i.e. extracting cobalt from the solution will be ineffective. At the same time, they get the opportunity to submit the raffinate or part of it to the preparation of leaching solutions after washing the heap. Since nickel sorption raffinate contains cobalt, its supply to the preparation of leaching solutions leads to recirculation of cobalt during heap leaching and to a gradual increase in the cobalt concentration in the product solution and, consequently, to an increase in the cobalt concentration in nickel sorption raffinate. That part of the nickel sorption raffinate in which the cobalt concentration is sufficiently high, for example, above 0.8 g / l, should preferably be neutralized and fed to the cobalt recovery step. As a result, the cobalt recovery efficiency is increased.

By feeding cobalt sorption raffinate or part of it to the washed leached heap, they provide a further decrease in the acidity of the leached ore.

The use of ferrous and / or magnesian technological types of ore, separately or in parallel technological flows or in a mixture, in various private implementations as ore directed to heap leaching, separately, facilitates the regulation of hydrometallurgical production parameters when changing the parameters of the raw material base. The preparation of a heap leach solution with an acid concentration of ~ 0.5 mol / l with a ratio of solution to ore W / T from 1.5 m ³ / t to 3 m ³ / t provides an optimal balance between the flow rate of the liquid to prepare the solution and the concentration of recoverable metals in the production solution for most oxidized ores. A decrease in W / T of less than 1.5 m ³ / t reduces the extraction of nickel in the solution and increases the viscosity of the suspension, which impairs mixing. Exceeding the W / T value of 3.0 m ³ / t leads to an increase in the residual acidity of the mother liquor and may require an increase in the number of leaching stages.

The firing of ferrous technological type ore or a mixture of ferrous and magnesian technological types of ore at a temperature of 300 ° C ÷ 700 ° C and the supply of sharp water vapor with a temperature of 100 ° C ÷ 200 ° C significantly increases the proportion of soluble metal compounds, especially in iron-type ore. At lower temperatures, the process is not efficient enough. At higher temperatures, the formation of ferrites, complicating the extraction of Nickel, as well as increased energy consumption. Water vapor prevents the oxidative effects of atmospheric oxygen, which oxidizes iron-containing minerals, which are rich in iron ore of a technological type, at high temperature, to acid-resistant hematite, which leads to a sharp decrease in the extraction of nickel and cobalt.

The roasting of ore of the magnesian technological type at a temperature of 200 ° C ÷ 500 ° C increases the proportion of soluble metal compounds and increases the filtration capacity of the ore. At lower temperatures, the process is not efficient enough. At higher temperatures, there is no improvement in firing results.

The selected preparation conditions (crushing, sintering, roasting) of ore for heaps significantly reduce the acid consumption for heap leaching.

Direction to heap leaching of only part of the initial oxidized ore, together with underground leaching of the rest of the initial oxidized ore, which is used as a magnesian technological type ore, can reduce the cost of extracting ore from underground, given the fact that it is possible to use well-known underground technologies leaching, which give good results with respect to ore of the magnesian technological type.

The direction of the mother liquor of the underground leaching of magnesian ore to the preparation of a leaching solution intended for heap leaching allows a higher concentration of nickel and other metals in the productive solution, which is sent for processing using ion-exchange processes, and a more complete use of acid, taking into account that the stock solution of underground leaching of magnesian technological type ore is relatively poor in the content of recoverable meta llov.

The preparation of a leach solution intended for underground leaching of magnesian technological type ore with an acid concentration of preferably ~ 0.75 mol / L (i.e., higher than the average for heap leaching) allows an acceptable level of metal conversion to solution, taking into account that during underground leaching of magnesian technological type ore, a significant amount of acid is bound by the ore.

Preparation of a leach solution intended for heap leaching with an acid concentration of ~ 0.5 mol / l with a ratio of solution to ore L / T from 1.5 m ³ / t to 3 m ³ / t, in conjunction with the preparation of a leach solution intended for underground leaching, with an acid concentration of ~ 0.75 mol / L in the ratio of solution to ore W / T from 3 m ³ / t to 6 m ³ / t, for given concentrations it is possible to calculate and maintain the optimal ratio of ore mass in one heap to mass ore underground, in this case equal to ~ 2, when used the same volume of solution for heap and underground leaching. This ensures the effective integration of heap and underground leaching, rational and economical consumption of leaching solutions. In addition, an increased L / T ratio for underground leaching is required due to worse hydrodynamic conditions compared to conditions in a heap of agglomerated ore.

The invention is illustrated by examples with the use of the following images.

Figure 1. Dependence of the degree of extraction of nickel from ferrous and magnesian ores in the leach solution on the duration of leaching.

Figure 2. The scheme of the proposed method in hydrometallurgical production.

Figure 3. Scheme of the continuous multi-stage countercurrent heap leaching section (containers for collecting the mother liquors are not shown).

Figure 4. Scheme of integration of underground leaching and continuous multi-stage countercurrent heap leaching.

Figure 5. Scheme of the area for processing productive solutions (copper extraction stage).

6. Scheme of the area for processing productive solutions (nickel extraction stage).

7. Scheme of the processing of productive solutions (stage of cobalt extraction).

Fig. 8. The scheme of the proposed method in hydrometallurgical production with the processing of magnesium solution.

Fig.9. The scheme of the proposed method on the example of hydrometallurgical processing of extracted ore of ferrous technological type.

Figure 10. The scheme of the proposed method on the example of hydrometallurgical processing of a mixture of mined ores of ferrous and magnesian technological types.

11. The scheme of the proposed method on the example of hydrometallurgical processing of mined ore of the magnesian technological type.

Fig. 12. The scheme of the proposed method is an example of a joint hydrometallurgical processing of mined ore of a magnesian technological type and ore of a magnesian technological type at the location.

Fig.13. The scheme of the proposed method is an example of a joint hydrometallurgical processing of mined ores of ferrous and magnesian technological types, separated by type.

Fig.14. The scheme of the proposed method on the example of a joint hydrometallurgical processing of extracted ore of ferrous technological type and ore of magnesian technological type at the place of occurrence.

In the examples, the preparation of finished metallurgical products from metal eluates extracted from the OP by the proposed method is additionally indicated.

The hydrometallurgical production in which the present invention is used consists of preparing oxidized ores for leaching, leaching by contacting the ore with mineral acids, for example, H ₂ SO ₄ , HCl, HNO ₃ , and acids formed as a result of bacterial activity, and subsequent ion-exchange sorption processing productive solution.

Oxidized ores are processed depending on the amount of magnesium and iron oxides represented in them. These ores are divided into categories depending on the relative content of magnesium and iron in them, for example ores of the magnesian technological type (saprolite), or ores of the ferrous technological type, such as limonite.

Oxidized ores of the ferrous technological type contain at least 0.5% nickel, 0.06% cobalt, 10% iron and 1.5% magnesium, and oxidized ores of the magnesian technological type contain at least 0.3% nickel , 0.01% cobalt, 3% iron and 7.5% magnesium

The iron content in magnesia ore may be at a high level, for example 12.39 wt.%. Table 1 presents the chemical composition of the glandular and magnesian technological types of ore.

Table 1. The chemical composition of oxidized ore The chemical composition of the ore,% Type of oxidized ore Ni Co Fe Mn Mg Ca SiO ₂ Magnesia ore 0.84 0,025 12.39 0.37 8.79 8.5 31,4 Iron ore 1.22 0.12 37.87 1,6 3.45 7 twenty

As can be seen from table 1, the magnesian technological type of ore has a relatively high magnesium content of about 8.79% by weight. The ferrous technological type of ore has a significantly lower magnesium content — approximately 3.45% by weight.

The differences in leachability, studied in tests under static conditions, observed between the magnesian and ferrous technological type of ore, are clearly visible when considering the curves presented in figure 1, where it is shown that the leachability of these two ores is completely different under the same conditions in the environment of leaching sulfuric acid .

As for the glandular and magnesian technological types of ore, the following leaching conditions with sulfuric acid were used in their processing:

particle size - 10 mm;

the concentration of H ₂ SO ₄ - 100 g / l;

W / T - 3 m ³ / t;

leaching temperature - room temperature (23 ° C);

leaching time - 1488 hours;

mixing - 1 time per day.

As a result of leaching under static conditions at room temperature, Ni recovery of 52.84% for magnesia ore was achieved, and for iron ore, recovery reached 29.03%. Therefore, it is not advisable to leach iron ore directly. To increase the extraction of nickel during leaching of iron ore of a technological type, special reducing roasting with steam was used.

The presence of fine-grained and clay components (minerals) in oxidized ore primarily determines the need for agglomeration (granulation) of ore in the case of using the most economical method of heap leaching to ensure a sufficiently high speed and uniformity of leaching solutions throughout the ore volume while maintaining the shape and high mechanical compressive strength of ore granules.

In the diagram of figure 2 the following stages of the hydrometallurgical processing of oxidized ore (OR) in accordance with the invention in the General case are indicated:

I - crushing mined ore 1;

II - agglomeration of crushed ore 2;

III - roasting agglomerated crushed ore 3;

IV - the formation of sequences of heaps 5 from calcined ore 4;

V - preparation of leaching solutions (BP), intended for heap leaching 6;

VI - continuous multi-stage countercurrent heap leaching to obtain productive solutions (PR) 7 and leached heaps 8;

VII - washing the leached heaps 8 using solutions 9, with the formation of washed heaps 10 and an acidic solution 11 containing impurities in dissolved form;

VIII - processing of productive solutions 7 with the formation of solutions 9, in which the acidity and impurities are preserved in dissolved form, and the nickel concentration does not exceed 0.3 g / l, and with the formation of solutions 12, neutralized to obtain insoluble compounds (NS) of iron and other metals;

IX - separation of insoluble compounds on the washed heap 10 or on a heap of another breed with the formation of a solution 13 containing magnesium.

In the diagram of FIG. 4, stage X is additionally indicated (underground leaching of the initial OR of magnesian type at the bed 15 to obtain the mother liquors 17) of the hydrometallurgical processing of oxidized ore (OR) in accordance with the developed implementation of the present invention. The preparation of BP in this implementation includes the preparation of BP for underground leaching 16.

To carry out heap leaching of the extracted oxidized ore of the glandular type, the ore is subjected to preliminary preparation (example 1, see Fig. 9):

- crushing (I) to a size of 5 mm;

- granulation (II) is carried out to a size of 10 ÷ 20 mm, while sulfur is added in an amount of at least 0.5% ÷ 5.5%, sodium chloride in an amount of at least 0.1% ÷ 2% and 5% ÷ 15% of water or industrial water;

- firing (III) is carried out at a temperature of 300 ° C ÷ 700 ° C, with the supply of sharp steam at a temperature of 100 ° C ÷ 200 ° C, contact with oxygen is not allowed when unloading and cooling the ore to 100 ° C;

- the formation of heaps (IV) of iron ore type is carried out up to 12 m high.

To carry out heap leaching of oxidized ore of magnesian type, the ore is subjected to preliminary preparation (example 2, see Fig. 11):

- crushing (I) is carried out to a size of 10 mm;

- Pelletizing (II) is carried out up to a size of 20–40 mm, while additives are added 5–15% of water or industrial water, and binder additives, such as water glass and / or cement, are also added if necessary;

- firing (III) is carried out at a temperature of 200 ° C ÷ 500 ° C;

- the formation of heaps (IV) of magnesia-type ore is carried out up to 6 m high.

Heap leaching of oxidized ores of both the glandular type and the magnesian type is carried out with mineral acids, for example, H ₂ SO ₄ , and / or HCl, and / or HNO ₃ , and / or acids formed as a result of bacterial activity. The concentration of acids used to leach the ore is at least 0.2 mol / L. The concentration of acid used can be constant or have an upward trend as the ore leaches. The relative volume of the leach solution is:

W / T = 1.5 m ³ / t ÷ 3 m ³ / t.

The heap leaching of VI oxidized ores is continuous countercurrent, containing at least two stages, preferably three stages, the process shown in Fig.3. Countercurrent heap leaching is characterized by the fact that the ore and the leaching solution move towards each other. At the first stage VI-1, neutralization is carried out on a freshly formed heap 5 of the mother liquor 6 ₂ , which came from the second stage VI-2 of heap leaching. In the second stage VI-2 of heap leaching, leaching is performed with mother liquor 6 ₁ , which came from the third stage VI-3 of heap leaching, heaps 5 ₁ received after the first stage VI-1. In the third stage VI-3 of heap leaching with leach solution 6, which came from stage V of the preparation of the leach solution, heaps 5 ₂ received after the second stage VI-2. The solution obtained after the first stage VI-1 of heap leaching is a productive solution 7, which is sent for processing VIII. If fourth VI-4 is used, etc. stage, the ore (ore pile) from the third stage of VI-3 leaching enters the fourth stage of VI-4, and from the fourth to the fifth, etc. The spent ore after the final stage VI-3 leaching goes to washing VII, and the solutions move in the opposite direction from washing VII to the preparation of V BP 6, from the preparation of BP V to the last stage VI-3, from the last stage VI-3 to the first stage VI -1 leaching VI, from the first stage VI-1 to the processing of VIII productive solution 7.

The magnesian type of oxidized ores, satisfying natural criteria, such as the degree of water cut of the ores, their filtration properties, the presence of impermeable water-proofs, the mineral form of the metal compound, which is relatively easily opened by the solvent, is suitable for underground leaching.

In the present invention, it is conditionally possible to consider underground leaching X as the final stage in a continuous multi-stage counterflow, containing at least three stages, heap and underground leaching process (see figure 4), the first stages of which is the heap leaching VI, shown in figure 3 .

In the heap and underground leaching of oxidized ores, leaching is carried out with mineral acids, for example, H ₂ SO ₄ , and / or HCl, or / and HNO ₃ , and / or acids formed as a result of the vital activity of bacteria. In this process, acidity is adjusted both before underground leaching and before heap leaching. The concentrations of acids used to leach the ore are at least 0.75 mol / L for underground leaching and 0.5 mol / L for heap leaching. The concentration of acid used can be constant or have an upward trend as the ore leaches. The volume of leach solution per ore mass is L / T = 1.5 m ³ / t ÷ 3 m ³ / t for heap leaching and L / T = 3 m ³ / t ÷ 6 m ³ / t for underground leach, therefore the mass ratio T (KV) of the ore used for leaching one heap, and the mass of T (PV) of ore during underground leaching is:

T (KV) / T (PV) = 2,

because for each leaching process (KB and PV) the same volume of leach solution is used.

Obtained and neutralized to a pH value of 1 ÷ 3, productive solution 7 is subjected to processing VIII using ion-exchange processes to isolate copper, nickel and cobalt from the solution in the form of eluates, from which finished products are then obtained.

The first stage VIII-Cu processing VIII is the extraction of copper from the productive solution 7, a diagram of which is presented in figure 5. Its first stage VIII-Cu-1 (sorption of copper) is carried out on a chelate type sorbent 18, for example, Dowex M4195, to obtain a sorbent loaded with copper 20. Then its second stage VIII-Cu-2 (copper desorption) with a solution of 21 ammonia 1 is performed % ÷ 10% to extract copper and obtain a copper-unloaded sorbent 23. At the end, the sorbent is washed (stage VIII-Cu-3) with water 24 from ammonia and a sorbent washed from ammonia 18 is obtained, which enters stage VIII-Cu-1. As a result of sorption, raffinate 19, purified from copper, is formed. Another solution formed after desorption of copper is a solution of copper ammonia 22, which is sent for crystallization (stage VIII-Cu-4) to obtain copper hydroxide 28 and regenerated ammonia 27. The third solution formed after washing the sorbent is solution 25 containing ammonium ion, which is used to prepare (stage VIII-Cu-5) from ammonia 29 and regenerated ammonia 27 ammonia solution for desorption of copper 21.

The second stage of the VIII-Ni processing (see Fig.6) is the stage of extraction of Nickel from the raffinate 19 of copper sorption, which is performed in two stages 1-Ni and 2-Ni. In the first stage 1-Ni-1 of the first stage 1-Ni, nickel is sorbed on a chelate type sorbent 30, for example, Dowex M4195, with a pH value of 1 ÷ 2, to obtain a nickel-loaded sorbent 31. In the second stage, 1-Ni- 2, the sorbent is supplemented with nickel to obtain a saturated sorbent 32, which is carried out with solution 33a (purified nickel eluate) with a concentration of 60 g / l ÷ 100 g / l for nickel and a pH of 1 ÷ 2. The first desorption of nickel, where the main discharge of the saturated sorbent 32 from nickel is performed, is carried out in the third stage with 1-Ni-3 solution 35 containing 40 g / l ÷ 70 g / l nickel and 1 mol / l ÷ 1.8 mol / l acid , with obtaining the unloaded sorbent 34. At the fourth stage 1-Ni-4, a second desorption is performed, where the final unloading of the sorbent 34 from nickel is performed to obtain an additional unloaded sorbent 36 with an acid solution of 37 molar concentration of 1 mol / L ÷ 1.8 mol / L. After nickel desorption, the sorbent 36 is washed (fifth stage 1-Ni-5) with water 38 from acid to obtain a washed sorbent 30, which returns to stage 1-Ni-1. As a result of the first stage of the first stage of the nickel extraction step (i.e., nickel sorption), a nickel sorption raffinate 39 is obtained containing the main impurities of iron, magnesium and cobalt, part 39a of which is sent to be combined into solution 9 for washing the VII heap after leaching, after which the resulting solution 11 is fed to the preparation of V leach solution. The other part of raffinate 396 sorption of nickel, after reaching a concentration of at least 0.8 g / l in cobalt in raffinate 39 as a result of the solution turnover in the leaching-processing cycle, goes to the third stage of processing VIII-Co - the stage of cobalt extraction. The second solution formed after the saturation stage (second stage 1-Ni-2) yields the saturation raffinate 40, which is sent to be combined into solution 9 for washing the VII heap after leaching. The third solution, formed after desorption in the third stage of the first stage of the nickel extraction stage, is nickel eluate 41 (80 g / l ÷ 100 g / l in Ni) containing an impurity in iron; it goes to the second stage of the 2-Ni stage of nickel extraction VIII-Ni - obtaining purified nickel eluate 33. The fourth solution obtained after desorption of nickel in the fourth stage 1-Ni-4 of the first stage 1-Ni of the stage of nickel extraction VIII-Ni is secondary nickel eluate 42 is an acidic nickel solution, which, together with a solution of acid 43 and a solution of 336 concentration of 60 g / l ÷ 100 g / l of nickel and a pH of 1-2, is sent to prepare (stage 1-Ni-6) desorbing solution 35 for the third stage 1-Ni-3 of the first stage of the Nickel extraction stage. The fifth solution 44, formed after washing the sorbent from the acid, is sent together with the acid solution 45 to the preparation (stage 1-Ni-7) of the acid stripping solution 37 for the fourth stage 1-Ni-4 of the first stage of the nickel extraction step.

или Cl^- форме, в зависимости от используемой кислоты, при кислотности pH сорбируемого раствора, равной 1÷3, с получением нагруженного железом сорбента 47. Затем производится промывка (стадия 2-Ni-2) сорбента 47 от никелевого раствора водой 48 с получением промытого сорбента 49. После этого производится десорбция (стадия 2-Ni-3) железа раствором 50 кислоты с концентрацией 0,5 моль/л ÷ 1 моль/л, с получением разгруженного от железа сорбента 51. После этого производится регенерация сорбента (стадия 2-Ni-4) раствором 52 гидроксида натрия с кислотностью pH, равной 5÷8, с получением регенерированного сорбента 53. Заключительной стадией 2-Ni-5 является промывка сорбента 53 водой 54 до проскока по кислоте в значения pH, равные 4÷5, для получения промытого от иона натрия сорбента 46. В результате сорбции железа образуется очищенный никелевый элюат 33, одна часть 33 а которого расходуется на стадии 1-Ni-2, вторая часть 336 расходуется на стадии 1-Ni-6, третья часть 33в расходуется на получение готового продукта - на стадии электролиза 2-Ni-8 с получением металлического никеля 61 и/или металлического никелевого порошка 62 и/или никелевой соли (NiSO₄*7H₂O) 63 на стадии кристаллизации 2-Ni-9. Вторым образованным раствором 55 является промвода, образованная промывкой насыщенного железом сорбента 47 от никеля, содержащая значительное количество никеля; она отправляется для объединения с никелевым элюатом 41, поступающим с первой ступени 1-Ni этапа извлечения никеля па вторую ступень 2-Ni (на стадию сорбции железа 2-Ni-1). Третий раствор, образуемый в результате десорбции железа, железистый элюат 56, который объединяется в раствор 9 и направляется на промывку кучи VII, пришедшей после кучного выщелачивания. Четвертый раствор 57, образованный после регенерации сорбента 51, содержащий ионы натрия, делится на части; одна часть 57а отправляется вместе с раствором кислоты 58 на производство (стадия 2-Ni-6) десорбирующего раствора 50 для стадии десорбции железа, другая часть 576 вместе с пятым раствором 59, образующимся после промывки регенерированного сорбента 53 от иона натрия, направляется на приготовление (стадия 2-Ni-7) раствора 52 регенерации сорбента, где доукрепляется гидроксидом натрия 60.The second step of the 2-Ni stage VIII-Ni extraction of nickel is to obtain purified nickel eluate 33. The first step 2-Ni-1 of the second step is the sorption of iron and other impurities from the nickel eluate 41 obtained from the first step 1-Ni containing iron impurity. Iron sorption is carried out on anion exchange resin grade 46 AB-17x8

or Cl ^- form, depending on the acid used, at an acidity of pH of the sorbed solution equal to 1 ÷ 3, to obtain iron-loaded sorbent 47. Then, the sorbent 47 is washed (stage 2-Ni-2) from the nickel solution with water 48 to obtain washed sorbent 49. After this, desorption (stage 2-Ni-3) of iron is carried out with a solution of 50 acid with a concentration of 0.5 mol / l ÷ 1 mol / l, to obtain sorbent 51 unloaded from iron. After that, the sorbent is regenerated (stage 2- Ni-4) with a solution of 52 sodium hydroxide with a pH of 5 ÷ 8, to obtain a regenerated sorbent 53. The final stage of 2-Ni-5 is washing the sorbent 53 with water 54 until acid breakthrough to a pH value of 4 ÷ 5 to obtain a sorbent 46 washed from sodium ion. As a result of iron sorption, a purified nickel eluate is formed 33 , one part 33 of which is consumed in stage 1-Ni-2, the second part 336 is consumed in stage 1-Ni-6, the third part 33c is spent on the finished product - in the electrolysis stage 2-Ni-8 to obtain metallic nickel 61 and / or metallic nickel powder 62 and / or nickel howl salt (NiSO ₄ * 7H ₂ O) 63 2 9-Ni-crystallization step. The second formed solution 55 is a promoter formed by washing the iron-saturated sorbent 47 from nickel, containing a significant amount of nickel; it is sent to combine with the nickel eluate 41 coming from the first stage of the 1-Ni stage of nickel extraction to the second stage of 2-Ni (to the stage of sorption of iron 2-Ni-1). The third solution, formed as a result of iron desorption, is a glandular eluate 56, which combines in solution 9 and is sent to the washing of heap VII, which came after heap leaching. The fourth solution 57, formed after regeneration of the sorbent 51, containing sodium ions, is divided into parts; one part 57a is sent together with the acid solution 58 to produce (stage 2-Ni-6) a stripping solution 50 for the iron desorption step, the other part 576, together with the fifth solution 59 formed after washing the regenerated sorbent 53 from the sodium ion, is sent to prepare ( stage 2-Ni-7) of the sorbent regeneration solution 52, where it is further fortified with sodium hydroxide 60.

The third stage VIII-Co of processing VIII is the stage of cobalt extraction (see Fig. 7) from part 396 of the nickel sorption raffinate 39, in which the cobalt concentration reaches 0.8 g / L. In the first stage of VIII-Co-1, part 396 of the nickel sorption raffinate is neutralized using brucite, and / or magnesium oxide, and / or magnesite, and / or sodium hydroxide 64, as a result of which its acidity is adjusted to pH values from approximately 3 to 6. The resulting pulp 65, depending on the iron content in the raffinate of nickel sorption, contains glandular cake (insoluble compounds of iron and other metals) in a ratio equal to W / T = 10 m ³ / t ÷ 100 m ³ / t. The neutralized solution (pulp) 65 in the second stage of the VIII-Co-2 stage of cobalt extraction is subjected to sorption processing on an ion exchange resin 66, for example, Lewatit TP207, Lewatit TP220, Purolit S960, Dowex M4195. At this stage, a cobalt-loaded ion-exchange resin 67 is obtained. Then, the third stage VIII-Co-3 is performed — desorption of cobalt with a solution of 68 mineral acid, for example, H ₂ SO ₄ , and / or HCl, or / and HNO ₃ , preferably H ₂ SO ₄ , the result is a cobalt-discharged ion exchange resin 69. The fourth step of VIII-Co-4 is to wash the discharged ion-exchange resin 69 from the acid with water 70 to obtain a washed ion-exchange resin 66, which is returned to the sorption stage of cobalt VIII-Co-1. As a result of sorption of cobalt (stage VIII-Co-2 of the cobalt extraction stage), cobalt sorption raffinate 12 is formed, which consists of a solution containing a significant amount of solid iron hydroxide and is sent to the compartment IX of insoluble iron compounds (ferrous cake) and other metals by filtration on spent (i.e. leached) and washed at the washing stage VII with a combined solution of 9 heap, or on a heap of another breed. The result is a solution 13 containing magnesium. The volume of pulp 12 fed to the filtration of iron, to the mass of ore Ж / Т is 0.1 m ³ / t ÷ 1 m ³ / t. The second solution formed at the stage of cobalt extraction is cobalt eluate 71 formed at the desorption stage of VIII-Co-3, from which cobalt 72 is obtained at the stage of electrolysis of VIII-Co-5 and / or cobalt salt (CoSO ₄ * 7H ₂ O) 73 at the crystallization stage VIII-Co-6. The third resulting solution 74 is the promoter, which, together with the acid solution 75, is sent to prepare (stage VIII-Co-7) a stripping solution 68 for the cobalt desorption stage VIII-Co-3.

The diagram of Fig. 8 additionally depicts the preparation of a finished magnesium product from a solution 13 obtained after filtration of the sorption raffinate of cobalt 12 containing HC iron in stage IX. The first part 13 a of the magnesium solution 13 is consumed in stage V (preparation of the leaching solution), the second part 136 of the magnesium solution 13 is consumed in the agglomeration stage II, and the third part 13 in is used to produce regenerated acid 76 and magnesium oxide 77 in the pyrohydrolysis stage XI and / or magnesium salt (MgSO ₄ * 7H ₂ O) 78 in the crystallization step XII. The regenerated acid 76 is sent to stage V for the preparation of BP 6, and magnesium oxide 77 can be either a finished product or a working reagent used in the stage of VIII-Co cobalt extraction to neutralize (stage VIII-Co-1) nickel sorption raffinate 39b. The resulting magnesium salt 78 is a finished product.

Depending on the size of the deposit, the nickel content in the ore, the presence of magnesia and gland type ore, the possibility of their separation, as well as the availability of underground leaching (PV) of the magnesia type ore at the site, we highlight the following features in the implementation of the proposed method for nickel extraction, cobalt and other metals from oxidized ores:

- heap leaching of mined iron-type ore (Fig. 9);

- heap leaching of a mixture of mined ore of ferrous and magnesian types (figure 10);

- heap leaching of mined ore of the magnesian type (11);

- heap leaching of mined ore of magnesian type and underground leaching of magnesian ore at the place of occurrence (Fig. 12);

- separate heap leaching of mined ore of ferrous and magnesian types (Fig.13);

- heap leaching of mined iron-type ore and underground leaching of magnesian-type ore at the occurrence site (Fig. 14).

The scheme of carrying out the hydrometallurgical process according to the present invention, among other possible schemes, may include any of the schemes shown in figures 9, 10, 11, 12, 13 or 14. The indices "g" or / and "m", which are used in the figures to denote some positions indicate the connection of this position, respectively, with a glandular and / or magnesian technological type of ore.

Figure 9 illustrates an example implementation of a process for the integrated hydrometallurgical processing of oxidized ores of a ferrous type. The hydrometallurgical processing scheme for mined iron ore contains, in particular, the following stages:

- crushing (Izh) to a size of 5 mm;

- granulation (agglomeration IIg) is carried out up to a size of 10 ÷ 20 mm, while sulfur 2a is added in an amount of at least 0.5% ÷ 5.5%, table salt 26 in an amount of at least 0 , 1% ÷ 2% and 5% ÷ 15% of water or industrial water;

- firing (IIIg) is carried out at a temperature of 300 ° C ÷ 700 ° C, with the supply of sharp steam 3a with a temperature of 100 ° C ÷ 200 ° C, contact with oxygen is not allowed when unloading and cooling the ore to 100 ° C;

- the formation of heaps (1Uzh) of iron ore is carried out up to 12 m high.

Figure 10 presents an example of a hydrometallurgical processing scheme for mined oxidized ore (ferrous and magnesian types), which cannot be divided by types due to economic or technological conditions.

Figure 11 presents an example of a hydrometallurgical processing scheme for mined oxidized ore of the magnesian type. Differences in the hydrometallurgical processing of magnesia-type ore from the processing of iron-type ore are reflected under the conditions of the following stages:

- crushing (Im) is made up to a size of 10 mm;

- Pelletizing (agglomeration of IIm) is carried out up to a size of 20–40 mm, with additions of 5% ÷ 15% of water or industrial water, and, if necessary, binders, such as water glass and / or cement, are added;

- firing (IIIm) is carried out at a temperature of 200 ° C ÷ 500 ° C;

- the formation of heaps (IVm) of magnesian type ore is carried out up to 6 m high.

On Fig presents a variant of the total scheme, combining the scheme depicted in Fig.9 and 11, where separately in two process streams of heap leaching, the mined ore is processed, respectively, of glandular and magnesian type. The common intersection of these two parallel processes is:

- preparation of V leaching solution 6, which is divided into part 6g sent to KV VIzh of iron ore, and part 6m sent to KV VIm of magnesian ore;

- processing of VIII productive solution 7, which combines solutions 7zh (PR after KV VIzh of iron ore) and 7m (PR after KV VIm of magnesian ore);

solution 9 obtained after processing VIII, containing impurities in dissolved form, is divided into solution 9g, sent for washing VIIg of the spent glandular heap, and solution 9m, sent for washing VIIm of the spent magnesian heap.

As an example of the use of the present invention on a laboratory scale, we consider dynamic leaching in columns of iron ore and magnesia type ore (hereinafter, for brevity, glandular and magnesian ore). The numbering of the stages and steps in the laboratory process may not coincide with the corresponding numbering in the above examples of the industrial process.

Agglomeration study was carried out in 6 columns: 3 columns with ferruginous ore and 3 columns with magnesia ore.

For the agglomeration of ferruginous ore, the extracted ferruginous ore was used, over which operations were carried out:

- crushing to class - 5 mm;

- granulation with the addition of sulfur in 2%, table salt in 1%, water 5% to sizes:

a) 5 mm ÷ 10 mm (column No. 1);

b) 10 mm ÷ 20 mm (column No. 2);

c) 20 mm ÷ 40 mm (column No. 3);

- firing pellets at a temperature of 500 ° C and a steam supply of 100 ° C.

For agglomeration of magnesia ore, mined magnesia ore was used, over which operations were performed:

- crushing to class - 10 mm;

- granulation with the addition of water 5% to sizes:

a) 10 mm ÷ 20 mm (column No. 4);

b) 20 mm ÷ 40 mm (column No. 5);

c) 40 mm ÷ 50 mm (column No. 6);

- firing pellets at a temperature of 200 ° C.

The chemical composition of the agglomerated ore is presented in table 2.

Table 2. The chemical composition of sinter ore No. p / p Ore type Chemical composition, % Ni Co Fe Mg Mn Cr one Agglomerated iron ore 0.87 0.08 28.90 13.30 1.30 0.60 2 Agglomerated Magnesia Ore 0.63 0,03 12.39 8.79 0.37 0.24

After agglomeration, the ore was loaded into columns 1 m high and 0.2 m in diameter. Then, a solution of sulfuric acid was fed to the top of the column at a rate of 10 l / h / m ² , concentration of 50 g / l (0.5 mol / l) and the volume of leach solution equal to W / T = 3 m ³ / t for 90 days. After passing the BP, the mother liquor was supplemented with sulfuric acid to a concentration of 50 g / l (0.5 mol / l). The result of the experiment to determine the optimal size of the agglomeration of glandular and magnesian ore is presented in table 3.

Table 3. Dependence of the degree of Ni extraction during leaching from agglomeration of glandular and magnesian ore. No. p / p Ore type Extraction of Ni with different agglomeration,% 5 mm ÷ 10 mm 10 mm ÷ 20 mm 20 mm ÷ 40 mm 40 mm ÷ 50 mm one Agglomerated iron ore 78.89 77.63 56.25 - 2 Agglomerated Magnesia Ore - 69.35 67.58 51.34

From table 3 it can be seen that the agglomeration size of 10 mm ÷ 20 mm is optimal for glandular ore, and 20 mm ÷ 40 mm for magnesian ore. At a higher dimension of the granules, there is a decrease in the extraction of Ni from the ore, and at a lower dimension of the granules, the filtration rate of the ore in the columns decreases, which can cause blockage of pores on the heaps and termination of leaching.

For the KB study, the results of dynamic leaching were taken in column No. 2 for agglomerated gland ore of size 10 mm ÷ 20 mm and column No. 5 for agglomerated magnesia ore in size of 20 mm ÷ 40 mm. The results are presented in table 4.

In the aforementioned leach study, the concentration of free H ₂ SO ₄ remaining in the leach solution ranged from 19.09 g / L to 27.7 g / L (pH <1). Since high acidity can cause certain difficulties when working at the ion-exchange stage of the nickel extraction process, the solution, after leaching, is passed through a newly formed OP pile to neutralize the residual free acid in the solution to a pH of 1 to 3.

To neutralize the mother liquors obtained after leaching in column No. 2 and column No. 5, two additional additional columns were prepared with sizes as columns No. 1 ÷ No. 6, containing:

- agglomerated glandular ore with a size of 10 mm ÷ 20 mm (column No. 7);

- agglomerated magnesia ore with a size of 20 mm ÷ 40 mm (column No. 8).

The mother liquors were neutralized by supplying the mother liquor after column No. 2 to the top of column No. 7, and the mother liquor after column No. 5 to the top of column No. 8. Stock solutions were supplied at a rate of 10 l / h / m ² .

The results of the KB experiment are presented in table 4.

Table 4. HF Simulation Experiment Results No. p / p Ore type Ore mass, kg Volume of solution, l The chemical composition of the mother liquor after leaching and neutralization, g / l Recovery% Ni Co Cu Fe Mg H ₂ SO ₄ Ni Co Fe Mg one Agglomerated iron ore (column No. 2) thirty 83.6 2.46 0.2 0,03 16.29 4.61 19.09 77.63 68,43 15,5 9.54 2 Agglomerated magnesia ore (column No. 5) thirty 90.64 1.68 0.08 0.01 11.28 14.91 27.7 67.58 65.01 23.09 38.03 3 Agglomerated iron ore (column No. 7) thirty 76 2.54 0.20 0,03 12.55 5.44 pH = 1.98 2,5 0.71 -3.56 1.72 four Agglomerated magnesia ore (column No. 8) thirty 82,4 1.71 0.08 0.01 10.52 16.15 pH = 1.72 1.33 0.28 -1.69 3.87

An advantage of the process according to the present invention is that the neutralizing agent is ore. Thus, there is a saving on acid and neutralizing reagents, such as soda, sodium hydroxide, magnesite, brucite, lime, etc. There is also no need for hardware design of the solution neutralization process

Processing OL

For processing, PR was taken after column No. 7 (agglomerated glandular ore).

The obtained PR is sent for processing using an ion-exchange process, comprising the step of extracting copper, the step of extracting nickel, the step of extracting cobalt.

Copper sorption is carried out on a chelate type Dowex M4195 resin. The active functional group was bis-picoliamine. Since the resin is an amine, this resin is protonated in an acid solution.

The first stage of the laboratory ion-exchange process is the sorption of copper impurities, since the affinity for Dowex M4195 sorbent for copper is higher than for nickel. Depending on the type of ore, the concentration of copper in the PR can reach values up to 0.1 g / l.

The copper sorption experiment was carried out in a glass tube with a diameter of 15 mm and a height of 100 mm, densely filled with a Dowex M4195 sorbent. The solution was supplied at a speed of 5 m / h and with a ratio W / T equal to 443.

Desorption was performed with a 5% ammonia solution. The results of the experiment on the sorption of copper are presented in table 5.

Table 5 (start). The results of the experiment on the stage of copper extraction No. p / p Stage Type of solutions Vp / vc Volume of solution, l The chemical composition of solutions, g / l Sorbent capacity, g / l Ni Co Cu Fe Mg H ₂ SO ₄ Ni Co Fe Cu one Cu-1 ETC 339.70 60 2.54 0.20 0.10 12.55 5.44 pH = 1.98 0 0 0 0 2 Copper sorption raffinate 339.70 60 2,53 0.20 0.00 12.55 5.44 pH = 1.81 4.12 0 0 33.97 3 Cu-2 Ammonia 3.00 0.53 pH = 10.5 four Copper eluate 3.00 0.53 1.36 11.21 pH = 10.2 0 0 0 0

For the end of table 5, see page 42.

End of table 5. 5 Cu-3 Water 1.00 0.18 pH = 7 6 Promvoda 1.00 0.18 0.01 0.11 pH = 8.9 0 0 0 0

The second stage of the laboratory ion-exchange process of processing of PR is the stage of extraction of nickel from the raffinate of copper sorption, received after the sorption purification of PR from copper.

The Nickel extraction stage is divided into 2 stages.

The experiment in the first stage of the nickel extraction stage was carried out in a glass tube with a diameter of 25 mm and a height of 250 mm, densely filled with a Dowex M4195 sorbent, and with a solution being supplied from below.

The first stage of the first stage is nickel sorption. The copper sorption raffinate solution was fed at a speed of 5 m / h. The result was a nickel-loaded sorbent and a solution of nickel sorption raffinate.

In the second stage (saturation), a saturation solution with a nickel concentration of 90 g / l and a pH of 1.8 was supplied at a speed of 1 m / h. The result was a maximally nickel-loaded sorbent and a solution of raffinate saturation.

At the third stage, primary desorption of nickel was carried out with desorption solution No. 1 with a concentration of 60 g / l for nickel and 100 g / l for sulfuric acid supplied at a speed of 1 m / h. The result was a partially unloaded sorbent and a solution of nickel eluate.

In the fourth stage, secondary desorption of nickel was carried out with desorption solution No. 2 with a concentration of 150 g / l of sulfuric acid, supplied at a speed of 1 m / h. The result was a completely unloaded sorbent and a solution of secondary nickel eluate.

At the fifth stage, the sorbent was washed from an acid solution with water supplied at a speed of 1 m / h. The result was a washed sorbent and promv. The experimental results for the first stage of the Nickel extraction stage are presented in table 6.

Table 6. The results of the experiment on the first stage of the Nickel extraction stage No. p / p Stage Type of solutions Vp / vc Volume of solution, l Chemical composition Solution capacity, g / l sorbent, g / l Ni Co Fe Mg H ₂ SO ₄ Ni Co Fe one 1-Ni-1 Copper sorption raffinate 5.09 6.24 2,53 0.20 12.55 5.44 pH = 1.81 12.30 0.68 5.40 2 Nickel sorption raffinate 5.09 6.24 0.11 0,07 11.49 5.44 pH = 1.52 3 1-Ni-2 Saturation Solution 0.73 0.89 90.00 - pH = 1.8 65.40 0.00 0.89 four Saturation Raffinate 0.73 0.89 0.18 0.55 3.68 - 8.69 5 1-Ni-3 Desorption solution No. 1 1.78 2.18 60.00 - 100.00 10.50 0.00 0.12 6 Nickel Eluate 1.78 2.18 90.85 0.00 0.63 - pH = 1.71 7 1-Ni-4 Desorption solution No. 2 1.30 1,59 150.00 0.00 0.00 0.00 8 Secondary Nickel Eluate 1.30 1,59 8.08 0.09 - 80.69 9 1-Ni-5 Water 1.00 1.23 - 0.00 0.00 0.00 10 Promvoda 1.00 1.23 - 15.23

The experiment in the second stage of the nickel extraction stage was carried out in a glass tube with a diameter of 25 mm and a height of 250 mm, densely filled with anion exchange resin AB-17 × 8, and with a solution being supplied from below.

- форму, с подачей раствора со скоростью 1 м/ч. В результате получался нагруженный железом(III) сорбент и очищенный никелевый элюат.At the first stage of the second stage of the nickel extraction stage, sorption of iron (III) from nickel eluate obtained in the previous experiment is performed. Sorption was carried out on anionite AB-17x8, charged in

- form, with the supply of a solution at a speed of 1 m / h The result was an iron (III) loaded sorbent and purified nickel eluate.

In the second stage, the anion exchange resin was washed from nickel with water at a speed of 1 m / h. The result was anion exchange resin and nickel solution loaded with iron (III) and washed with nickel.

In the third stage, iron (III) was desorbed with a desorption solution with a sulfuric acid concentration of 150 g / l, supplied at a speed of 1 m / h. As a result, anion exchange resin and iron (III) eluate unloaded from iron (III), but loaded with sulfuric acid, were obtained.

- форму регенерирующим раствором гидроксида натрия с кислотностью pH, равной 8, подаваемым со скоростью 5 м/ч. В результате получался регенерированный в

- форму анионит и промвода.At the fourth stage, anion exchange resin was regenerated in

- the form of a regenerating solution of sodium hydroxide with a pH of 8 equal to 5 m / h. The result was regenerated in

- the form of anion exchange resin and promv.

At the fifth stage, washing of sodium anion exchange resin with water at a speed of 5 m / h was carried out. The result was washed regenerated anion exchange resin and promv.

The experimental results for the second stage of the Nickel extraction stage are presented in table 7.

Table 7 (beginning). The results of the experiment on the second stage of the Nickel extraction stage No. p / p Stage Type of solutions Vp / vc Volume of solution, l The chemical composition of solutions, g / l Sorbent capacity, g / l Ni Co Fe H ₂ SO ₄ Fe H ₂ SO ₄ one 2-ni-1 Nickel Eluate 8.24 2.18 90.85 0.00 0.63 pH = 1.71 5.17 0.00 2 Purified Nickel Eluate 8.24 2.18 90.00 0.00 pH = 1.8 3 2-ni-2 water 0.50 0.13 pH = 7 four Nickel solution 0.50 0.13 14.01 pH = 1.82 5 2-ni-3 Desorption solution 2.00 0.53 150.00 0.00 193.0 6 Glandular eluate 2.00 0.53 2.59 53.40

For the end of table 7, see page 45.

The end of table 7 7 2-ni-4 Regenerating solution 3.00 0.79 pH = 8 0.00 0.00 8 Promvoda 3.00 0.79 pH = 4 9 2-ni-5 water 1.00 0.26 pH = 7 0.00 0.00 10 Promvoda 1.00 0.26 pH = 5

The third stage of the laboratory ion-exchange process is the stage of extraction of cobalt from a portion of the nickel sorption raffinate solution.

For the cobalt extraction step, a reverse solution of nickel sorption raffinate is used, which has reached a cobalt concentration above 0.8 g / l.

For the experiment on the cobalt extraction step, the nickel sorption raffinate previously obtained was nickel enhanced to 0.8 g / L.

At the first stage of the cobalt extraction stage, a part of nickel sorption raffinate with brucite was neutralized to a pH value of 5. The process was carried out in a 1 L glass beaker while stirring with a mechanical stirrer for 0.5 hour. As a result, a neutralized portion of the nickel sorption raffinate (pulp) was obtained.

In the second stage, sorption of cobalt from the neutralized part of the raffinate of nickel sorption (pulp) was carried out by introducing a LewatitTP 207 sorbent in a ratio of L / T equal to 15. To accelerate sorption of cobalt, mechanical stirring was performed for 30 min. After sorption, the raffinate of sorption of cobalt and cobalt-loaded sorbent were separated on a sieve.

In the second stage, cobalt was desorbed with a desulfurization solution of sulfuric acid with a concentration of 100 g / l and a relative volume of V _p / V _c equal to 2. Desorption was carried out in a glass of 200 ml with constant mechanical stirring for 30 min. The result was a cobalt eluate and an unloaded sorbent, which were separated on a sieve.

At the third stage, the sorbent was washed with acid (V _p / V _c equal to 1) in a 200 ml beaker with constant mechanical stirring for 30 minutes. The result was washed sorbent and promvod, which was divided on a sieve.

The results of the experiment on the stage of extraction of cobalt are presented in table 8.

Table 8. The results of the experiment on the stage of cobalt extraction No. p / p Stage Type of solutions Vp / vc Volume of solution, l The chemical composition of solutions, g / l Sorbent capacity, g / l Ni Co Fe Mg H ₂ SO ₄ Ni Co Fe one Co-1 Nickel sorption raffinate 15.00 0.60 0.11 0.80 11.49 5.44 pH = 1.52 2 Neutralized Nickel Sorption Raffinate 16.50 0.66 0.10 0.73 10.44 4.95 pH = 5 3 Co-2 Neutralized Nickel Sorption Raffinate 16.50 0.66 0.10 0.73 10.44 4.95 pH = 5 1.65 11.81 5.82 four Cobalt sorption raffinate 16.50 0.66 0.00 0.01 10.09 pH = 2.5 5 Co-3 Desorption solution 2.00 0.08 100.00 6 Cobalt Eluate 2.00 0.08 0.83 5.91 2.91 30.67 7 Co-4 Water 1.00 0.04 pH = 5 8 Promvoda 1.00 0.04 8.93

The next step is the utilization of iron hydroxide from the solution (pulp) after sorption of cobalt.

For the experiment, two types of model solution were prepared with an iron content of 7.5 g / l and 47.8 g / l, and these solutions were neutralized to a pH value of 4 with magnesium oxide.

The filtration experiment was carried out on 4 columns with a diameter of 200 mm and a length of 1 m, which were previously used:

- columns No. 2 and No. 7, agglomerated glandular ore after leaching;

- columns No. 5 and No. 8, agglomerated magnesia ore after leaching.

In columns No. 1 and No. 2, cake was loaded after leaching and washing of granular glandular ore. In columns No. 3 and No. 4, cake was loaded after leaching and washing of the agglomerated magnesia ore.

A pulp of iron hydroxide with a concentration of 7.5 g / l of iron was poured into columns No. 2 and No. 5, and a pulp with a concentration of 47.8 g / l of iron was poured into columns No. 7 and No. 8. At lower concentrations of solid particles in the pulp, a large breakthrough through the ore layer of solid particles occurs, and at high concentrations, the ore pores in the column are rapidly clogged. The pulp was poured in a ratio of W / T equal to 1, and the slip of the solid phase was measured at the output.

The results of the filtration experiment are presented in table 9.

Table 9. Filtration Experiment Results No. Type of solutions The composition of the solution for experiment No. 1, g / l The composition of the solution for experiment No. 2, g / l H ₂ SO ₄ Fe Tv H ₂ SO ₄ Fe Tv one Cobalt sorption raffinate pH = 4.3 7.5 14.35 pH = 4.4 47.8 91.47 2 The solution after filtering the pulp through the cake of spent agglomerated glandular ore pH = 3.4 0.34 0,03 pH = 3.8 0.35 0.05 3 The solution after filtering the pulp through the cake of spent agglomerated magnesia ore pH = 2.5 0.13 0.01 pH = 3.2 0.14 0,03

Laboratory and industrial experiments carried out under the control of the applicants showed that the implementation of the proposed method is possible using known samples of hydrometallurgical equipment, known reagents and materials.

Claims (63)

1. The method of extraction of metals, mainly nickel and cobalt, from oxidized ores, including the preparation of leaching solutions containing acid belonging to the group comprising hydrochloric acid, sulfuric acid, nitric acid and acids formed by the vital functions of bacteria, leaching of the initial oxidized ore by prepared leaching solutions with obtaining productive solutions and processing of productive solutions, while the initial oxidized ore contains mined oxidized ore, leaching is mined of oxidized ore is carried out in the form of continuous multi-stage countercurrent heap leaching, and it is preliminarily crushed, the crushed ore is agglomerated, at least one heap sequence is formed from the agglomerated ore, each heap is subjected to at least two leaching stages, in each heap sequence for each heap at the first stage of its leaching, a leach solution prepared from the mother liquor obtained in the second stage of leaching the previous heap is fed to For the intermediate stage of its leaching, a leach solution prepared from the mother liquor obtained in the next stage of leaching the previous heap is fed, at the last stage of its leaching, the initial leaching solution intended for heap leaching is fed, at the end of the last stage of its leaching, it is washed and the mother liquor, obtained in the first stage of its leaching, served for processing as a productive solution or as part of a productive solution, The processing of productive solutions is carried out in stages by ion exchange using ion-exchange sorbents in several stages, with the preparation of eluate enriched in each stage of processing with metal and depleted in other metals compared to the content of metals in productive solutions and in eluates obtained at other stages processing, while the agglomerated ore is preliminarily fired before forming heap sequences from it, and a continuous multi-stage counter Accurate heap leaching is carried out with the number of stages that ensure the acidity of the mother liquors obtained in the first stages of heap leaching is reduced to the level necessary for the first stage of processing of the productive solutions, or these mother liquors are additionally neutralized to the indicated required acid level by filtering them on a heap of another rocks before submitting them for processing, while at least one eluate obtained at the corresponding stage of processing is cleaned of this to obtain a purified eluate, and the receipt of the aforementioned eluate is carried out with the saturation of the corresponding ion-exchange sorbent by feeding on it part of the obtained purified eluate, and at least part of the solutions formed during processing, in which acidity and impurities are preserved in dissolved form, and concentration nickel does not exceed 0.3 g / l, sent to leaching the leached heap and then to the preparation of leaching solutions, and at least part of the solutions formed during SRI processing, neutralized to yield the insoluble iron compounds and other metal and separating the insoluble compounds from at least a portion of the neutralized leached solution by filtration and washed on the heap or on the heap another species. 2. The method according to claim 1, characterized in that the heaps form a height of 1 ÷ 12 m, heap leaching is performed in at least one process stream, the mother liquors obtained at different stages of heap leaching are collected in separate containers, the original leach solutions, intended for heap leaching, prepared with an acid concentration of 0.2 ÷ 2 mol / l and served on the surface of the heaps that are at the last stage of leaching, with an irrigation density of 10 ÷ 20 l / h / m ² , the mother liquor obtained on each, except first, higher stage heap leaching, is fed to the surface of another heap, which is at the previous leaching stage, with an irrigation density of 10 ÷ 20 l / h / m ² , heap leaching is performed in such a number of stages and in such a number of flows that the pH value in at least one stream The mother liquor obtained directly in the first leaching stage or after additional neutralization on a heap of another breed ranged from 1 to 3, as a productive solution or as part of a productive solution for processing a mother liquor with a pH value of 1 to 3 is obtained, obtained in the first stage of one heap leaching process stream directly or after additional neutralization on a heap of another breed, or a mixture of mother liquors obtained in the first stages of heap leaching with a pH value of 1 to 3 is fed in several process streams directly or after additional neutralization on a heap of another breed, at least the stage is extracted as stages of processing a productive solution I copper, the stage of extraction of nickel, the stage of extraction of cobalt, as the first stage of processing the productive solution, the stage of extraction of copper by the ion exchange method is performed, moreover, a sorbent capable of selectively extracting copper from a solution with a pH value from 1 to 3 is used as a sorbent in the first stage of the copper extraction step, copper-laden sorbent and copper sorption raffinate are obtained, in the second stage of the copper recovery step, copper eluate is obtained from the copper-laden sorbent by desorption of copper, copper eluate is fed to obtain copper of rusting products, the copper sorption raffinate is fed to the second stage of processing the productive solution, in which the stage of nickel extraction is carried out by ion exchange, and the nickel eluate is obtained as an eluate, which is purified from impurities to obtain purified eluate and the preparation of which is carried out with saturation corresponding to it the sorbent by feeding on it a portion of the obtained purified eluate, the nickel extraction step is carried out in two steps, at the first step of the nickel extraction step, nickel eluate is mixed and, at the second stage of the nickel extraction stage, the nickel eluate is purified from impurities, at the first stage of the first stage of nickel extraction, a nickel-loaded sorbent contaminated with impurities and nickel sorption raffinate are obtained, at the second stage of the first stage of the nickel extraction stage, the nickel-loaded sorbent is saturated with nickel and partially they are purified from impurities by supplying purified nickel eluate to it to obtain a saturated sorbent and an additional saturation raffinate contaminated with impurities in the third stage of the first stage of the extraction stage nickel is obtained from a saturated sorbent of nickel eluate by desorption with a nickel-containing solution; in the fourth stage of the first step of the nickel extraction step, a secondary nickel eluate is obtained from the sorbent by desorption of an acid solution, a secondary nickel eluate is fed to a nickel-containing solution for the third stage of the first stage of the nickel extraction step, the saturation raffinate served as a solution in which acidity and impurities are retained in dissolved form, for leaching of the leached heap and then for cooking e leaching solutions, Nickel eluate is fed to the second stage of the Nickel extraction stage, the Nickel sorption raffinate is divided into parts, while part of the Nickel sorption raffinate is washed in leached heaps and then the preparation of leaching solutions, and the other part of Nickel sorption raffinate is neutralized to obtain nera iron and other metals, wherein at least a portion of this other portion of the nickel sorption raffinate is neutralized using at least one of the materials belonging to the group, including magnesium oxide, brucite, magnesite, and the neutralized portion of the nickel sorption raffinate is fed to the cobalt extraction step; in the first step of the second step of the nickel extraction step, nickel eluate is purified by iron sorption, and a sorbent loaded with iron and other impurities is obtained and purified nickel eluate as iron sorption raffinate, purified nickel eluate, partially fed to the second stage of the first stage of the nickel extraction step, partially fed to the preparation of a nickel-containing solution for the third stage of the first stage, step nickel extraction, partly served to obtain nickel-containing products, the sorbent loaded with iron is washed from nickel and fed to the step of desorption of iron with an acid solution to obtain a ferrous eluate and washed sorbent, the ferrous eluate is served as a solution in which acidity and impurities are preserved in dissolved form, on washing the leached heap and then preparing leaching solutions, in the first stage of the cobalt extraction step, a sorbent loaded with cobalt and cobalt sorption raffinate are obtained, loaded the cobalt sorbent is fed to the stage of desorption of cobalt with an acid solution to obtain a cobalt eluate and the sorbent discharged from cobalt, the cobalt eluate is fed to produce cobalt-containing products, at least a portion of the cobalt sorption raffinate is fed as a solution neutralized to obtain insoluble iron and other metal compounds washed leached pile or onto a pile of another breed with separation of these insoluble compounds by filtration, respectively, on the washed leached pile or on a pile of dr goy breed and to obtain the magnesium solution, a solution obtained by washing the leached heap leaching is fed to the preparation of solutions. 3. The method according to claim 2, characterized in that the extracted ore of a ferrous technological type is used as the whole oxidized ore mined. 4. The method according to claim 3, characterized in that the source leach solutions intended for heap leaching are prepared with an acid concentration of approximately 0.5 mol / l, with a ratio of the solution to ore W / T from 1.5 to 3 m ³ / t. 5. The method according to claim 3, characterized in that the crushing of the extracted ore of ferrous technological type is performed up to a class of 5 mm. 6. The method according to claim 3, characterized in that the agglomeration of the crushed mined ore of a ferrous technological type is carried out before the formation of granules with a size of 10 ÷ 20 mm with additives of at least 0.1 ÷ 2% of sodium chloride, 0.5 ÷ 5.5% elemental sulfur, 5 ÷ 15% of water or industrial water by weight of ore. 7. The method according to claim 3, characterized in that the firing of the agglomerated crushed mined iron ore of technological type is performed at a temperature of 300 ÷ 700 ° C and when supplying sharp water vapor with a temperature of 100 ÷ 200 ° C. 8. The method according to claim 2, characterized in that the mined ore of the magnesian technological type is used as the whole oxidized ore mined. 9. The method according to claim 8, characterized in that the initial leach solutions intended for heap leaching are prepared with an acid concentration of approximately 0.5 mol / l, with a ratio of the solution to ore W / T from 1.5 to 3 m ³ / t. 10. The method according to claim 8, characterized in that the crushing of the mined ore of the magnesian technological type is performed up to a class of 10 mm. 11. The method according to claim 8, characterized in that the agglomeration of the crushed mined ore of the magnesian technological type is carried out before the formation of granules with a size of 20 ÷ 40 mm with the addition of 5 ÷ 15% water or industrial water by weight of the ore. 12. The method according to claim 8, characterized in that the firing of the agglomerated crushed mined ore of the magnesian technological type is performed at a temperature of 200 ÷ 500 ° C. 13. The method according to claim 2, characterized in that the extracted ore in the form of a mixture of mined ores of ferrous and magnesian technological types is used as the entire oxidized ore mined. 14. The method according to item 13, wherein the initial leach solutions intended for heap leaching are prepared with an acid concentration of approximately 0.5 mol / l, with a ratio of solution to ore W / T from 1.5 to 3 m ³ / t. 15. The method according to p. 13, characterized in that the crushing of the extracted ore is performed up to a class of 5 mm. 16. The method according to item 13, wherein the agglomeration of crushed mined ore is carried out before the formation of granules with a size of 10 ÷ 20 mm with the addition of at least 0.1 ÷ 2% of sodium chloride, 0.5 ÷ 5.5% of elemental sulfur, 5 ÷ 15% of water or industrial water by weight of ore. 17. The method according to item 13, characterized in that the agglomerated crushed mined ore is calcined at a temperature of 300 ÷ 700 ° C and with the supply of sharp water vapor with a temperature of 100 ÷ 200 ° C. 18. The method according to claim 2, characterized in that the extracted ore of ferrous and magnesian technological types, separated by types, is used as the whole extracted oxidized ore, heap leaching is performed in at least two process streams, while in at least one of process streams leached mined ore of a ferrous technological type and in at least one of the process streams leached mined ore of a magnesian technological type. 19. The method according to p. 18, characterized in that the source leach solutions intended for heap leaching are prepared with an acid concentration of approximately 0.5 mol / l, with a ratio of solution to ore W / T from 1.5 to 3 m ³ / t. 20. The method according to p. 18, characterized in that the crushing of the extracted ore of ferrous technological type is performed up to a class of 5 mm. 21. The method according to p. 18, characterized in that the agglomeration of crushed mined iron ore of technological type is performed until the formation of granules with a size of 10 ÷ 20 mm with additives of at least 0.1 ÷ 2% of table salt, 0.5 ÷ 5.5% elemental sulfur, 5 ÷ 15% of water or industrial water by weight of ore. 22. The method according to p. 18, characterized in that the sintering of agglomerated crushed mined iron ore of technological type is performed at a temperature of 300 ÷ 700 ° C and when supplying sharp water vapor with a temperature of 100 ÷ 200 ° C. 23. The method according to p. 18, characterized in that the crushing of the mined ore of the magnesian technological type is performed up to a class of 10 mm. 24. The method according to p. 18, characterized in that the agglomeration of crushed mined ore of the magnesian technological type is performed until granules of 20 ÷ 40 mm in size are added with the addition of 5-15% of water or industrial water by weight of the ore. 25. The method according to paragraph 18, characterized in that the firing of the agglomerated crushed mined ore of the magnesian technological type is carried out at a temperature of 200 ÷ 500 ° C. 26. The method according to claim 2, characterized in that the additional leaching of oxidized ore belonging to the magnesian technological type and at the same time located at the site of occurrence, by underground leaching to obtain mother liquors of underground leaching, which are sent to the preparation of leaching solutions intended for continuous multi-stage countercurrent heap leaching, and part of the solutions formed during the processing, which is fed to the preparation of leaching solutions, is used for the preparation of leaching solutions intended for in-situ leaching, and the leaching solutions were prepared intended for in-situ leaching, acid at a concentration of at least 0.5 mol / l. 27. The method according to p. 26, characterized in that the source leach solutions intended for heap leaching are prepared with an acid concentration, preferably approximately equal to 0.5 mol / l, with a ratio of solution to ore W / T from 1.5 to 3 m ³ / t, while leaching solutions intended for underground leaching are prepared with an acid concentration of preferably approximately 0.75 mol / l, with a ratio of solution to ore W / T from 3 to 6 m ³ / t. 28. The method according to p. 26, characterized in that the ore of ferrous technological type is used as the extracted ore and its crushing is carried out to a class of 5 mm. 29. The method according to p. 28, characterized in that the agglomeration of crushed mined ore of ferrous technological type is performed until the formation of granules with a size of 10 ÷ 20 mm with additives of at least 0.1 ÷ 2% of sodium chloride, 0.5 ÷ 5.5% elemental sulfur, 5 ÷ 15% of water or industrial water by weight of ore. 30. The method according to p. 28, characterized in that the firing of agglomerated crushed mined iron ore of technological type is performed at a temperature of 300 ÷ 700 ° C and when supplying sharp water vapor with a temperature of 100 ÷ 200 ° C. 31. The method according to p. 26, characterized in that as the mined ore use mined ore of the magnesian technological type and its crushing is carried out to a class of 10 mm 32. The method according to p. 31, characterized in that the agglomeration of the crushed mined ore of the magnesian technological type is performed until granules of 20 ÷ 40 mm in size are added with the addition of 5-15% of water or industrial water by weight of the ore. 33. The method according to p, characterized in that the sintering of agglomerated crushed mined ore of the magnesian technological type is performed at a temperature of 200 ÷ 500 ° C. 34. The method according to any one of claims 2-33, characterized in that at the stage of copper extraction, the chelate type ion-exchange resin is used as a sorbent, at the second stage of the stage of copper extraction, copper desorption is carried out with an ammonia solution with a pH value of at least 7 to obtain as copper eluate of a solution of copper ammonia and obtaining a sorbent purified from copper, then the sorbent purified from copper is washed from ammonium ion with water to obtain a solution of ammonium ion and a regenerated sorbent. 35. The method according to clause 34, characterized in that at least part of the copper ammonia solution obtained in the copper extraction step, copper is recovered by crystallization to obtain a copper salt and with the regeneration of ammonia, and at least a portion of the regenerated ammonia is sent to prepare an ammonia solution, which perform the desorption of copper. 36. The method according to clause 34, wherein the ammonium ion solution obtained by washing the copper-free sorbent is fed to a solution of ammonia, which is used to desorb copper. 37. The method according to clause 34, wherein the regenerated sorbent is returned to the first stage of the stage of copper extraction. 38. The method according to any one of claims 2-33, characterized in that the acidity of the copper sorption raffinate is maintained in the pH range from 1 to 2, at the first stage of the nickel extraction step, a chelate type ion-exchange resin is used as the sorbent, at the second stage of the first stage of the nickel extraction step, purified nickel eluate with a nickel concentration of 60 ÷ 90 g / l and a pH value of 1 to 2 is used as the purified nickel eluate, and in the third step of the first step of the nickel recovery step as a nickel-containing solution for production from an unsaturated of the nickel eluate sorbent, a nickel solution with a nickel concentration of 40 ÷ 70 g / l and an acid concentration of 1 to 1.5 mol / l is used; in the fourth stage of the first stage of the nickel extraction step, a solution is used as an acid solution to obtain secondary nickel eluate from the sorbent acid with an acid concentration of 1 to 1.5 mol / L, then the sorbent is washed with water to obtain a regenerated sorbent and promoters, and the resulting promoter is sent to prepare an acid solution for the fourth stage of the first stage of the nickel extraction stage. 39. The method according to § 38, characterized in that at least a portion of the regenerated sorbent obtained by washing it with water is returned to the first stage of the first stage of the nickel extraction step. 40. The method according to any one of claims 2-33, characterized in that an anion exchange resin AB-17x8 or a similar anion exchange resin is used as a sorbent in the second step of the nickel extraction process, and a purified nickel eluate with a nickel content of 80 ÷ 100 is obtained as an iron sorption raffinate g / l 41. The method according to any one of claims 2 to 33, characterized in that from at least a portion of that portion of the purified nickel eluate obtained as an iron sorption raffinate, which is fed to nickel-containing products, nickel salt is obtained by crystallization as a nickel-containing product . 42. The method according to paragraph 41, characterized in that as the acid contained in the solutions with which nickel eluate and secondary nickel eluate in the first step of the nickel extraction step are obtained by desorption, a sulfuric acid solution is used, and obtained by crystallization as a nickel-containing product a nickel salt having a composition of NiSO ₄ · 7H ₂ O. 43. The method according to any one of claims 2-33, characterized in that from at least a portion of that portion of the purified nickel eluate obtained as iron sorption raffinate, which is fed to nickel-containing products, cathode metal nickel is obtained by electrolysis as nickel-containing product. 44. The method according to any one of paragraphs.2-33, characterized in that from at least a portion of that portion of the purified nickel eluate obtained as an iron sorption raffinate, which is supplied to produce nickel-containing products, a nickel-metal powder is obtained by electrolysis as nickel-containing product. 45. The method according to p. 40, characterized in that the first stage of the second stage of the stage of nickel extraction on anion exchange resin AB-17x8 or a similar anion exchange resin is performed at a pH of the sorbed solution from 1 to 3, the iron-loaded anion exchange resin is washed from nickel with water to obtain a promo containing nickel, iron desorption is carried out with an acid solution having an acid concentration of 0.5 ÷ 1 mol / L, then the washed anionite is regenerated with a sodium hydroxide solution with a pH value of 5 to 8 to obtain a mother liquor for the regeneration of anionite and regenerated ani onite, and then the regenerated anion exchange resin is washed from the sodium ion with water until acid breakthrough in pH from 4 to 5. 46. The method according to item 45, wherein the regenerated anion exchange resin washed from sodium ion is returned to the first stage of the second stage of the Nickel extraction stage. 47. The method according to item 45, wherein at least a portion of the promoter containing nickel obtained by washing with water anionite loaded with iron is added to the nickel eluate supplied to the first stage of the second stage of the Nickel extraction stage. 48. The method according to item 45, wherein at least a portion of the mother liquor regeneration of anion exchange resin is directed to the preparation of a solution of sodium hydroxide, which perform the regeneration of anion exchange resin. 49. The method according to item 45, characterized in that at least part of the mother liquor for the regeneration of anion exchange resin is directed to the preparation of an acid solution with an acid concentration of 0.5 ÷ 1 mol / l, which is used to desorb iron. 50. The method according to any one of claims 2 to 33, characterized in that they neutralize a portion of the nickel sorption raffinate fed to the cobalt extraction step to a pH of 3 to 5. 51. The method according to p. 50, characterized in that as part of the raffinate of sorption of Nickel supplied to the stage of extraction of cobalt, use part of the raffinate of sorption of Nickel, in which the concentration of cobalt reaches 0.8 g / l or more. 52. The method according to p. 50, characterized in that at the stage of cobalt extraction, an ion-exchange resin is used as a sorbent, the stage of cobalt desorption is performed with a solution of mineral acid with an acid concentration of 0.5 ÷ 2 mol / L, preferably 1.5 mol / L. 53. The method according to paragraph 52, wherein the ion-exchange resin unloaded from cobalt is washed with water and returned to the cobalt sorption stage, and the wash formed as a result of washing is directed to the preparation of a mineral acid solution, which is used to perform the cobalt desorption stage. 54. The method according to paragraph 52, wherein at least part of the cobalt eluate supplied to obtain cobalt-containing products is obtained by crystallization of a cobalt salt. 55. The method according to p. 50, characterized in that part of the cobalt sorption raffinate is fed as a solution neutralized to obtain insoluble compounds of iron and other metals, to a heap of another breed with separation of these insoluble compounds on it and to obtain a magnesium solution. 56. The method according to claim 2, characterized in that at least part of the magnesium solution obtained by filtering the cobalt sorption raffinate on the washed leached heap is subjected to purification from magnesium and partly serves to agglomerate the crushed ore, and partly serves to prepare leach solutions . 57. The method according to p, characterized in that the purification from magnesium of at least part of the magnesium solution obtained by filtering the cobalt sorption raffinate on the washed leached heap is carried out by pyrohydrolysis to obtain magnesium oxide and regenerated acid. 58. The method according to p, characterized in that the purification from magnesium of at least part of the magnesium solution obtained by filtering the cobalt sorption raffinate on the washed leached heap, is performed by crystallization to obtain a magnesium salt and water. 59. The method according to claim 2, characterized in that at least a portion of the magnesium solution obtained by filtering the cobalt sorption raffinate on the washed leached heap is subjected to magnesium purification to obtain a solution that meets the fishery criteria for water quality and is sent to an external one Wednesday 60. The method according to clause 57, wherein at least a portion of the regenerated acid obtained by pyrohydrolysis of a magnesium solution is returned to circulation and sent to the preparation of leaching solutions. 61. The method according to clause 57, wherein at least a portion of the regenerated acid obtained by pyrohydrolysis of a magnesium solution is returned to circulation and used in the processing of productive solutions. 62. The method according to clause 57, wherein at least a portion of the magnesium oxide obtained by pyrohydrolysis of a magnesium solution is used when performing neutralization to obtain insoluble compounds of iron and other metals of that part of the nickel sorption raffinate, which is fed to the cobalt extraction step. 63. The method according to claim 2, characterized in that to compensate for the loss of water in circulation, use water from available sources without further purification and add it to at least one of the solutions of nickel sorption raffinate or cobalt sorption raffinate, in solutions purified from magnesium, directed to the agglomeration of crushed ore or to the preparation of leaching solutions.

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