WO2020099966A1 - Método hidrometalúrgico sólido-líquido-sólido para la solubilización de metales a partir de minerales y/o concentrados sulfurados de cobre - Google Patents
Método hidrometalúrgico sólido-líquido-sólido para la solubilización de metales a partir de minerales y/o concentrados sulfurados de cobre Download PDFInfo
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- WO2020099966A1 WO2020099966A1 PCT/IB2019/059258 IB2019059258W WO2020099966A1 WO 2020099966 A1 WO2020099966 A1 WO 2020099966A1 IB 2019059258 W IB2019059258 W IB 2019059258W WO 2020099966 A1 WO2020099966 A1 WO 2020099966A1
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B15/00—Obtaining copper
- C22B15/0063—Hydrometallurgy
- C22B15/0065—Leaching or slurrying
- C22B15/0067—Leaching or slurrying with acids or salts thereof
- C22B15/0069—Leaching or slurrying with acids or salts thereof containing halogen
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B15/00—Obtaining copper
- C22B15/0063—Hydrometallurgy
- C22B15/0065—Leaching or slurrying
- C22B15/0067—Leaching or slurrying with acids or salts thereof
- C22B15/0071—Leaching or slurrying with acids or salts thereof containing sulfur
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
- C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
- C22B3/10—Hydrochloric acid, other halogenated acids or salts thereof
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Definitions
- the present invention refers to a Solid-Liquid-Solid hydrometallurgical method that is capable of achieving, under the same method, the solubilization of minerals and concentrates, both in the form of oxides, as well as secondary and primary sulphides, mainly chalcopyrite, to obtain a desired metal.
- Copper is a widely used metal and is essential in various economic sectors, such as infrastructure, cabling, electric vehicles, electrical and electronic equipment, and renewable energy (Elshkaki
- Chalcopyrite is the most abundant primary copper sulfide and represents approximately 70-80% of the world's copper reserves (Hall S. et al., 1973; Kaplun et al., 2011). This mineral is stable and is the sulfide most refractory to hydrometallurgical processes. Furthermore, the formation of a passivating layer has been observed, when it is subjected to a variety of leaching agents, making its dissolution even more difficult (Dreisinger., 2006; Veloso el al., 2016). Enargite is also a primary copper sulfide and is present mainly in deposits in Peru and Chile, being of environmental concern as a source of arsenic and requires special concern in smelters. Therefore, most foundries penalize the content of arsenic in concentrates. Furthermore, arsenic is considered the most dangerous inorganic pollutant, causing environmental and health emergencies in various areas of the world (Mandal B. et al., 2002).
- hydrometallurgical processes that have been developed to leach the minerals and / or copper concentrates are based on solid-liquid, solid-liquid-gas or solid-liquid-gas-bacteria methods, where different reagents are used that act mainly as agents. oxidants, these processes could be divided into: chlorides, nitrates, sulfates, ammonia, iodides and bacteria, among others.
- the decrease in the hydrometallurgical participation in the type of mineral extracted is due to the exhaustion of leachable resources, to the appearance of primary refractory minerals (chalcopyrite) and therefore the closure of mining sites.
- the appearance of primary sulphides leads to high-grade ore being processed mainly by flotation, which will lead to generation of idle capacity in hydrometallurgical facilities, due to the fact that hydrometallurgical technology has not been reported at the industrial level. cost effective, for the treatment of primary low-grade copper sulphides (Cochilco, 2017).
- the increase in the production of concentrates will lead to an increase in the environmental liabilities (tailings) and in the processing capacity of the smelters.
- Hydrometallurgy is a science and technology of extraction of metals or materials by aqueous methods (Habashi F, 1993). In general, this discipline of extractive metallurgy is it develops in three different and sequential physical-chemical stages, called selective dissolution or leaching, purification / concentration and precipitation (Domic, 2001). This well-established science has competed vigorously with pyrometallurgical techniques, and in some cases has displaced such processes. In recent times, with the depletion of high-grade minerals and abundant low-grade primary minerals, hydrometallurgy appears as a possible economically viable option to treat primary minerals with low grades (Habashi, 2005).
- Chalcopyrite (CUFCST), enargite (CU 3 ASS 4 ) and bornite (CusFeSz are sulphide and primary copper minerals, refractory and semiconductor like the vast majority of sulfur minerals, with a crystalline structure where iron and copper ions they are in tetrahedral coordination with sulfur, in the case of chalcopyrite (Hall S. et al., 1973; Nikiforov K., 1999).
- Scope spectrum measurements of chalcopyrite and bornite have identified that the The electronic structure of both minerals is the same for copper (Cu 1+ ) and iron (Fe 3+ ), with a molecular weight for the first of 183.52 g / mol and for the second of 501.8 g / mol , providing each atom in its atomic weight the following percentages; Cu 34.6%; Fe 30.4%; S 34.9% and Cu
- Enargite (CU 3 ASS 4 ) is a copper sulfide with arsenic, like chalcopyrite and bornite has a valence +1 for copper; however, it has a molecular weight of
- This last phenomenon is proposed to be generated by the formation of different compounds, such as disulfide dichloride (S 2 CI 2 ), elemental sulfur, non-stoichiometric secondary sulphides and chlorocuprate I complexes, which are absorbed by the mineral surface ( Lu et al., 2000; Carneiro, 2007; Lundstróm et al., 2016; Nicol, 2017; Liu et al., 2017).
- S 2 CI 2 disulfide dichloride
- elemental sulfur elemental sulfur
- non-stoichiometric secondary sulphides and chlorocuprate I complexes
- Copper ions can form complexes with chloride ions and the prevalence of the complex will depend on the chloride concentration and leaching environment. In solutions with a high chloride concentration, there is a prevalence of cuprous complexes [CuCh],
- chlorocuprate (I) complexes increase their solubility as chloride concentration increases (Berger and Winand, 1983; Fritz, 1980, 1981; Lin et al., 1991; Winand, 1991; Yoo et al. , 2010).
- the beneficial effect of chlorocuprate complexes I on the dissolution of chalcopyrite has been little studied and they are considered dissolution inhibiting agents, for which reason, the aim is to maximize the presence of cupric ions as an oxidizing agent, over chlorocuprate complexes I (Winand, 1991; Liu el al., 2017).
- chalcopyrite is oxidized to covelin, different from that proposed by Pihlaso et al. (2008), who mentions the formation of chalcosine.
- the use of high concentrations of a reagent can generate an increase in the reaction rate; however, it could also generate unwanted side reactions and be economically not viable (Habashi F., 1999);
- Agglomeration is a stage that is generally carried out before leaching in oxide and secondary sulphide piles, and consists of joining the fine particles to the coarser ones, in order to increase the permeability coefficient in the pile, and thus be able to have efficient irrigation and aeration conditions to improve the extraction process (Bouffard SC, 2005, 2008). Therefore, the agglomeration stage is of vital importance to maintain good hydrodynamics in the pile and to avoid overturning.
- the simplest agglomeration stage is carried out by adding water and acid, in order to moisten the mineral until achieving optimum surface tension.
- the presence of water in the agglomeration stage is of vital importance, since without the presence of water there are no glomers, nor an adequate distribution of the acid, which would cause inefficient curing (Domic E., 2001; Lu. J. el al., 2017).
- the mineral is also cured, by adding concentrated sulfuric acid so that it acts on all the mineral particles and generates the best conditions for the leaching process.
- the acidity, the curing stage and the Leaching solutions is very important, since it interacts with the mineral and with the gangue, therefore, the lack of acid could harm the extraction of copper (Bouffard SC, 2005; Lu J. et al., 2017).
- the mechanism and equipment for agglomeration and curing can be done by adding water and then acid to the mineral on a conveyor belt or by using an agglomerator drum that allows a wet particle to rotate around itself, allowing efficient formation of the glomer. (Domic E., 2001).
- Weathering is defined as the fragmentation or partial or total degradation of rocks and minerals when in contact with atmospheric agents. Natural weathering of rocks or minerals is carried out by chemical reactions (chemical weathering) and various processes of mechanical disintegration (physical weathering), such as thermal stress, increased volume of clay minerals and crystal growth in rock joints due to changes of phases.
- solvent crystallization The relevant changes that occur due to solutions in rock pores are called solvent crystallization and correspond to a freezing crystallization process; however, when the process occurs by a solute, it is called salt weathering or haloclasty, in both cases an increase in pressure occurs in the internal walls of the rock, which promotes wear or rupture of it (Wellman H al al, 1965; Goudies A. al al., 1997; Smith J., 2006).
- Chemical weathering and salt weathering represent different rock breakage mechanisms and generally operate in concert. However, it is difficult to differentiate its effects separately, since they are phenomena that are interrelated, because the products that can be generated by the dissolution of minerals are used for a new process of weathering by salts.
- An example of this is the generation of sulfates, which can be produced by the attack of sulfuric acid, which can be of volcanic origin, deposition of atmospheric sulfur dioxide or by the reactions of the dissolution of a rock.
- Sodium chloride and hydrated magnesium chloride are abundant salts found in nature, playing an active role as antifreeze and road pollution controllers.
- Inorganic chloride is born from the dissolution of hydrazic compounds and binary salts in aqueous media under certain homogeneous solubility conditions.
- the intermolecular forces of the solvent cause the total destruction of ionic and covalent bonds allowing the dissociation of the salts in their primitive polar ions, that is to say; a valent metal or non-metal cation (H + , Na + , Mg 2+ , Fe 3+ , K + , etc.) and the chloride anion in question.
- Bischofita is a hydrated salt whose chemical formula is MgClixótLO, being the active compound of bischofita magnesium chloride, which has various physical properties, such as deliquescence, the ability to increase the surface tension of water and vapor pressure.
- This salt is obtained as waste or discarded from the solar evaporation process to which the brines extracted from certain salt flats are subjected, mainly in the lithium triangle, made up of Chile, Argentina and Venezuela, necessary for the extraction of lithium and potassium.
- the Magnesium Chloride Hydrate or Bischofite Crystals is available worldwide. However, the bischofita produced in Chile has the advantage that it has a low level of impurities.
- Sodium and magnesium chloride salts are soluble salts with a tendency to supersaturation, which in solution are very mobile and can penetrate deeply into fractures or joints of rocks, generating efflorescence and crystallization of salts on the surface or inside of the mineral or rock, as special characteristics of these two salts.
- the location of soluble chloride salts with respect to the outer surface of a mineral depends on the saturation or supersaturation mechanism of the solution. In the case of being generated by an evaporation process, the mechanism will be controlled by two processes that act simultaneously. On the one hand, the rate of evaporation, and on the other, the rate of contribution of solution through the mineral.
- the diffusion rate of the steam is less than the migration rate of the solution, the latter can reach the external surface where the salts will evaporate and crystallize, this depends on the form of heat transfer, either by convection or radiation ( Gómez-Heras el al., 2016). This last phenomenon is called efflorescence. If, on the other hand, the solution migration rate is less than the water vapor diffusion rate, equilibrium will be reached at a certain distance from the surface, producing cryptoeflorescence. When the water vapor diffusion rates are higher, it will generate a greater precipitation of salts, which will enhance said phenomenon.
- Evaporation of a liquid in a porous medium involves complex phenomena of liquid, vapor transport, and phase changes.
- the determination of the rate of evaporation, together with the evolution of the distribution of the liquid within the pore space as the liquid phase is replaced by the gaseous phase are important for the supersaturation condition and predicting damage induced by the crystallization of salts.
- the slow evaporation processes are well known and can be exemplified by the process of evaporation of water from a solid at room temperature, in this case the evaporation rates are very small, therefore, the temperature variations due to the phase change they are insignificant (Prat M. et al., 2007).
- the REDOX potential is an important parameter in the methods and in a large part of the technologies proposed for the dissolution of chalcopyrite, since it has been proposed that the formation of leaching products, considered passivating agents, are dependent on the potential of the medium, favoring low potentials a greater extraction and high potentials a lower copper extraction (Elsherief, 2002; Hiroyoshi el al., 2001; Velásquez-Yévenes el al., 2010; 2018).
- the potential window in which these higher copper extractions are achieved is limited and difficult to control, which means that once the critical dissolution potential is exceeded, the extraction of chalcopyrite stops completely.
- Publication US20040060395 discloses a solid-liquid-gas oxidative procedure, and relates to a process that uses a chlorinated environment for the leaching of concentrates by the action of cupric chloride in the presence of oxygen at elevated temperatures.
- Publication US7491372 shows a solid-liquid oxidative procedure, and refers to a process that uses calcium chloride in order to improve the quality of the glomers and thus the permeability of a cell.
- the phenomenology of the process is based on favoring the generation of oxidizing agents (Fe 3+ and Cu 2+ ) by the action of oxygen and the double redox copper and iron, which causes the solubilization of sulfur minerals.
- Publication W02007134343 (Muller el al., 2007) refers to a hydrometallurgical method consisting of two stages: the first non-oxidative in an acid medium; and a second oxidative stage, which involves solid-liquid-gas interaction, for the recovery of copper from primary and secondary minerals, which involves leaching the material in an acidic solution with chloride at redox potentials less than 600 mV in the presence of oxygen dissolved and cupric ions as oxidizing agents.
- Publication W02016026062 (Pati ⁇ o el al., 2016) discloses a solid-liquid oxidative procedure that involves the addition of oxidizing agent and a pretreatment of the mineral in the presence of high concentrations of chloride and minimal presence of oxygen, with a redox potential greater than 700 mV for the solubilization of primary and secondary copper sulphides.
- Publication WO2016026062 ( ⁇ lvarez, 2016) reveals a chemical and bacterial procedure in a solid-liquid-gas medium, and is related to a leaching process of secondary and primary copper sulphides in a ferrous-ferric-chloride medium, with bacteria and archaea iron-oxidants adapted to high concentrations of chloride ions. In addition, it involves the injection of heated air, to raise the temperature and enhance the dissolution reactions of the mineral.
- WO2016179718 (Engdahl el al., 2017) refers to a solid-liquid-gas oxidative method, which is carried out in a three-phase mixing agglomeration drum, and to a mineral agglomeration procedure carried out inside said drum for mineral pretreatment in the presence of sodium chloride, both used mainly in hydrometallurgy. Said drum and method employ a chlorine gas recirculation system and step as part of the invention.
- the present invention differs from the state of the art, since it refers to a Solid-Liquid-Solid (SLS) hydrometallurgical method that is capable of achieving the solubilization of oxidized minerals, secondary and primary sulfides, mainly primary sulfides, such as chalcopyrite, under the same SLS method; without depending on parameters such as redox potential, oxygen and acid concentration.
- SLS Solid-Liquid-Solid
- the method of the present application is not a pretreatment or a prolonged stage of curing and irrigation-rest, but rather a continuous solid-liquid-solid method in a condition of supersaturation of unhydrated and / or hydrated chloride salts , such as sodium chloride and / or bischofita, a condition that is generated by the intentional and repetitive application of drying stages, wetting and rewetting stages, enhancing chemical and physical phenomena on the mineral or concentrates, thus causing the crystallization, recrystallization and release of copper and subsequent precipitation of it with chlorine in a non-stoichiometric decomposition of the primary or secondary sulfide.
- unhydrated and / or hydrated chloride salts such as sodium chloride and / or bischofita
- the method is carried out at a temperature of 20 to 40 ° C, with no or minimal addition of water and acid, without the need to add oxidizing or reducing agents, nor oxygen.
- This method in its entirety can be executed independently of the presence of habitual impurities, such as is the case of arsenic, since the decomposition of the mineral or concentrate occurs in a non-stoichiometric relationship.
- habitual impurities such as is the case of arsenic
- the method of the present application has the benefits of hydrometallurgy, in addition to reducing the consumption of acid and water, since the transformation of sulfide can be carried out only with the presence of water and / or the minimal addition of acid.
- this method reduces the use of water in the agglomerate and / or agglomerate-curing stage, since when a hydrated chloride salt (for example, bischofita) is mixed with the mineral, the water molecules of said salt hydrated they moisturize the mineral, reducing the volume of water that must be added in the agglomerate and / or curing stages.
- a hydrated chloride salt for example, bischofita
- the present invention would make the resources available to reserves, which would allow supplying the future demand for copper, reactivating the hydrometallurgical plants, and would change the projections of the final product of copper in the next decade, reducing the use of flotation, which generates a great environmental impact, due to the high consumption of energy and water; in addition to the generation of environmental liabilities and pollutants from the operation of the smelters.
- the present invention relates to a Solid-Liquid-Solid (SLS) hydrometallurgical method in the presence of non-hydrated and / or hydrated chloride salts such as, for example, sodium chloride and / or bischophyte, in a supersaturated condition, which It is achieved by the intentional and repeated application of wetting, rewetting and drying stages, enhancing the phenomena chemical and physical on the mineral or concentrates, thus causing the crystallization, recrystallization and release of copper in a non-stoichiometric decomposition of the sulfide and subsequent precipitation of it with chloride.
- SLS Solid-Liquid-Solid
- the method occurs at a temperature of 20 to 40 ° C, independent of the redox potential, with a minimum consumption of water and acid, without the need to add oxygen.
- the method allows to reduce the consumption of acid and water, since the transformation of the sulfide can be carried out only with the presence of hydrated salts and / or the minimal addition of acid and water.
- the method of the present invention allows to reduce the use of water in the agglomerate and / or agglomerate-curing stage, because when a hydrated chloride salt is mixed with the mineral, the water molecules of said hydrated salt (for For example, bischofita) wet the mineral, reducing the volume of water that must be added in the agglomerate and / or curing stages.
- the present invention refers to a Solid-Liquid-Solid method in a chlorinated medium, governed by physical and chemical weathering processes for the solubilization of sulfur minerals, by supersaturation and crystallization of salts, using the addition of: a) a salt of non-hydrated chloride, or b) a hydrated chloride salt, or c) a mixture of both salts, in a supersaturated condition, which is reached by repetitive and intentional drying stages, which promotes rapid evaporation kinetics, and consequently the solubilization of the mineral, particularly chalcopyrite.
- This method is made up of 3 stages, called “Wetting Stage,” Drying and Supersaturation Stage “and” Washing and Rewetting Stage ". These stages can be repeated as many times as necessary to achieve maximum solubilization of the primary and / or secondary copper sulfide, either in the mineral or in the concentrate, achieving greater extraction of the desired metal.
- the first stage corresponds to a stage of wetting the mineral with water or water and acid, in the presence of salts in a condition of non-supersaturation, non-oxidative, or reductive agglomeration, but always in the presence of a) an unhydrated chloride salt, or b) a hydrated chloride salt, or c) a mixture of both salts.
- the addition of water there may or may not be the addition of water, since in the case of the hydrated chloride salt, the humidification provided by the water molecules of said salt is sufficient when mixing it with the mineral, without adding water or adding a minimal dose; however, for the use of a non-hydrated chloride salt (for example, sodium chloride) the addition of a solution is required, the addition of liquid at this stage generates the solvation process of the salts, allowing to leave active ions to react and migrate through the joints of the mineral. All these conditions cause variable conditions of pH and minimal presence of oxygen to be generated, achieving the optimal conditions for the second stage of the process.
- a non-hydrated chloride salt for example, sodium chloride
- the second stage corresponds to a Drying process that promotes the supersaturation, crystallization, recrystallization and precipitation of salts, both inside and outside the mineral or concentrate. Drying can start on the conveyor belt and continue on the stack or be done directly on the stack, by injecting dry or hot air, increasing the temperature and / or promoting low relative humidity. In this stage, physical and chemical weathering is promoted, generated by the use of chloride salts in a supersaturated condition.
- the dissolution of the primary and / or secondary copper sulfide is governed by a supersaturation and precipitation condition, which causes a non-stoichiometric decomposition of the sulfide, therefore, the process does not depend on the redox potential , pH, presence of oxygen or reducing or oxidizing agents.
- the drying time is variable and concludes with the beginning of the mineral or concentrate washing stage.
- the third stage corresponds to a washing stage in which an acidulated or unsaturated acidified solution of chloride salts is added to remove the chlorinated soluble species from the target metal (for example, copper), generated in the second stage, in addition to restoring salt concentrations and mineral wetting.
- a new stage of Drying and Oversaturation begins, where the mineral is dried again to promote the evaporation and supersaturation of salts, during periods of variable times.
- the wash can be acid-chlorinated and / or simply sea water and is aimed at removing the precipitated copper in the second process stage.
- Figure 1 Graph of copper extraction in relation to the concentration of acid in the stage of
- Figure 4 Graph of copper extraction in relation to the drying time in the Drying and Oversaturation stage, using Mineral 1.
- Figure 5 Graph of copper extraction in relation to the simulation of a continuous regime, using Mineral 1.
- Figure 6 Graph of Copper Extraction in relation to the first cycle of the Solid-Liquid-Solid method versus Prolonged Curing Times, using Mineral 1.
- Figure 7 Graph of Copper Extraction in relation to two cycles of the Solid-Liquid method- Solid versus Prolonged Cure Times of 120 days, using Mineral 1.
- Figure 8 Graph of Copper Extraction in relation to a first cycle of the Solid-Liquid-Solid method, using a mixture of salts and Mineral 1.
- Figure 11 Graph of copper extraction in relation to the Solid-Liquid-Solid method versus
- Figure 12 Graph of Copper Extraction in relation to the solid-liquid-solid method (S-L-S) versus Bio leaching and Chlorinated Leaching, using Mineral 3.
- Figure 13 Graph of water contribution by use of bischofita in the wetting stage to achieve a humidity of 6% and 10%.
- the present invention relates to a Solid-Liquid-Solid hydrometallurgical method in the presence of an unhydrated chloride salt and / or a hydrated chloride salt, in a supersaturated condition, which is achieved by the intentional and repeated application of steps drying and wetting, enhancing the chemical and physical phenomena on the mineral or concentrates, thus causing the crystallization, recrystallization and release of copper in a non-stoichiometric decomposition of the sulfide and subsequent precipitation of it with chloride.
- the method occurs at a temperature of 20 to 40 ° C, independent of the redox potential, with a minimum consumption of water and acid, without the need to add oxygen.
- the method allows to reduce the consumption of acid and water, since the transformation of the sulfide can be carried out only with the presence of hydrated salts and / or by the minimal addition of acid and water. Furthermore, the method of the present invention allows to reduce the use of water in the agglomerate and / or agglomerate-curing stage, because when the hydrated salt is mixed with the mineral, the water molecules of the hydrated chloride salt wet the mineral, reducing the volume of water that must be added in the agglomerate and / or curing stages.
- the present invention refers to a Solid-Liquid-Solid hydrometallurgical method in a chlorinated medium, governed by physical and chemical weathering processes for the solubilization of sulphurated minerals, by supersaturation and crystallization of salts, using the addition of: a) an unhydrated chloride salt, or b) a hydrated chloride salt, or c) a mixture of both salts, in a supersaturated condition, which is reached by repetitive and intentional drying stages, which generates a rapid evaporation kinetics, and consequently the supersaturation of the salts, which promotes the solubilization of the sulphurated minerals, particularly chalcopyrite.
- This method is made up of 3 stages, called “Wetting Stage,” Drying and Oversaturation Stage “and” Washing and Rewetting Stage “. These stages can be repeated as many times as necessary to achieve maximum solubilization of the primary and / or secondary copper sulfide, either in the mineral or in the concentrate, achieving greater extraction of the desired metal.
- an unhydrated chloride salt selected from the group consisting of sodium chloride, potassium chloride, magnesium chloride, anhydrous ferrous chloride, anhydrous ferric chloride can be used.
- the hydrated chloride salt is selected from the group consisting of magnesium chloride hexahydrate (bischofite), ferrous chloride heptahydrate, ferric chloride hexahydrate, among others.
- This stage begins with exposing the crushed ore to a step of agglomerate or agglomerate and curing in an agglomerator drum or on a conveyor belt, in order to wet, form glomers and dissolve the sodium chloride, or bischofita, using methods and conventional procedures.
- This stage can be carried out in the following ways:
- the first is that the addition of water and acid is joint. On the contrary, in a classic process of agglomerate and curing, the acid and the water are added separately.
- the second is that bischofite and / or sodium chloride can be added in solid form, depending on the characteristics of the mineral itself and the concentration of salts necessary for the dissolution of the mineral, which range between 20 and 80 kg / t.
- the third is that this stage can only be carried out with the addition of bischofite, without the addition of water and acid, which would allow the salt to be added directly to the conveyor belt.
- this stage can be carried out with the addition of a mixture of salts and water or with water and acid. In the case of using only water, the curing stage would not be carried out.
- the circulating or recirculating solutions will be used for the wetting and / or agglomerate-curing process; in addition to the replacement of the concentration of salts that were retained in the rubble of the treated mineral.
- Bischofita and / or sodium chloride will be replaced by adding solid in an amount of 5 to 15 kg / t, depending on the chloride content in the process recirculation solution.
- the addition of fresh and / or circulating sulfuric acid ranges from 0 to 30 kg / t of mineral, with a final moisture content of the agglomerated mineral that varies between 8 and 15%, depending on the characteristics of the gangue, hygroscopicity and granulometry of the mineral. .
- This second stage occurs in a solid-liquid-solid (SLS) condition and consists of promoting the supersaturation of the salts by drying the mineral by vaporization and / or evaporation methods, which includes injection of dry and / or hot air, low temperature or relative humidity.
- This stage can begin on the conveyor belt, partially reducing the surface moisture of the mineral and / or directly in the pile, by using some of the drying methods that allow generating and promoting constant drying kinetics, while promoting supersaturation and physical phenomena in the mineral, such as crystallization, precipitation, and haloclasty.
- the first cycle of the method ends when the copper extraction decreases significantly, because the vaporization or evaporation kinetics stops, because the mineral surface is covered by the precipitated copper-chloride complexes and the salt crystals, since in the case of sodium chloride the crystallization process takes place mainly on the surface of the solid.
- the first wash begins, in order to remove the extracted copper.
- a second drying and supersaturation cycle begins, in order to achieve maximum supersaturation and copper extraction.
- Bischophyte and / or sodium chloride, water or acid and water are required at this stage. No need for the addition of oxidizing agents such as cupric ions, nor the addition of oxygen by constant irrigation.
- This Drying and Oversaturation Stage ends with the start of continuous or intermittent irrigation of variable duration, using an acidic and unsaturated solution of bischofite and / or sodium chloride.
- the third stage of washing and re-wetting begins, by irrigation with an unsaturated acidic chloride solution.
- the objective of the Wash is to remove copper and soluble species, replace salts, clean the mineral surface and re-wet the bed.
- the three stages, Wetting, Drying and Oversaturation and Washing, can be repeated as many times as necessary, as long as wetting and chloride concentrations are promoted again, to achieve maximum solubilization of the copper contained in the primary or secondary mineral .
- This stage begins with the mixing of the concentrate with the bischofite and / or sodium chloride, and after that, water or water and acid are added, in order to achieve optimal wetting of the concentrate and solvation.
- concentration of bischophyte and / or sodium chloride used ranges from 20 to 120 kg / t in a solid-liquid-solid condition.
- concentration of fresh and / or circulating sulfuric acid will be necessary to achieve a pH between 0.5 and 3.
- the final humidity varies between 8 to 20%, depending on the hygroscopic characteristics of the salt and the concentrate. .
- This second stage of Drying and Oversaturation consists of drying the wet concentrate for a variable time, in order to generate the condition of chloride supersaturation and the Selective transformation of the concentrate to soluble chlorinated copper species and the precipitation of soluble species.
- the drying time increases, the humidity decreases and the supersaturation condition is enhanced, due to the vaporization and / or evaporation of the water.
- the prolonged drying period encourages salt crystallization and the cryptoeflorescence phenomenon in the concentrate particles.
- the drying process of the concentrate is carried out in greenhouses that have temperatures ranging from 25 to 40 degrees Celsius, promoting low relative humidity, allowing constant evaporation kinetics in the stacks or piles of concentrates, to promote supersaturation and copper extraction.
- the concentrate that was subjected to the Drying and Oversaturation stage is transported to washing pools, where the concentrate is subjected to a Washing stage with an acidulated solution or chloride and acid, to obtain soluble copper. Subsequently the concentrate is filtered and dried, in order to start a new process cycle if the total copper extraction is insufficient.
- the copper-rich solution, obtained from washing the concentrate is sent to a solvent extraction plant and subsequently to an electrowinning plant. However, the solution can also pass directly to new electrowinning plants, which can generate a cathode without a previous solvent extraction step and directly treat copper-rich solutions.
- the present invention specifically refers to a Solid-Liquid-Solid hydrometallurgical method for the solubilization of metals from minerals and / or concentrates of sulphurated minerals of primary and / or secondary origin that contain them, comprising the following sequential steps and / or overlapping: I. Humidification, where the mineral or concentrate is humidified by the addition of water or water-acid and hydrated and / or non-hydrated chloride salts;
- stage I the contact of the mineral or concentrate is made with recirculating solutions of the same process that may contain chloride, iron and copper ions, in an unsaturated environment, and where the Three stages are carried out independently of the potential REDOX that the medium has.
- the hydrated chloride salt is selected from the group consisting of magnesium chloride hexahydrate (bischofite), ferrous chloride heptahydrate, ferric chloride hexahydrate, among others.
- the non-hydrated chloride salt is selected from the group consisting of sodium chloride, potassium chloride, magnesium chloride, anhydrous ferrous chloride, anhydrous ferric chloride, and calcium chloride, among others.
- the non-hydrated and / or hydrated chloride salt is sodium chloride and / or bischophyte which is added in solid or in solution, preferably in an amount of sodium chloride and / or bischophyte that is added goes between 20 to 80 kg per ton of material, preferably between 30 and 60 kg / t.
- steps I and II can be carried out only with the addition of bischofita and / or bischofita and water and / or process solutions.
- the addition of chloride salts can include a mixture of hydrated and / or non-hydrated salts.
- step I the addition of water and acid in step I is carried out separately or together, preferably together.
- addition of sulfuric acid ranges from 0 to 30 kg per ton of material, preferably between 5 and 15 kg / t.
- the final moisture of the agglomerated mineral can be between 6 and 20%, preferably between 8 and 10%.
- stage I can be carried out in an agglomerating drum or directly on the conveyor belt.
- stage II in stage II the drying of the mineral is carried out with the pile covered and protected to generate the increase in temperature.
- stage II in stage II the condition of supersaturation of species and salts is achieved by means of intentional and repetitive drying cycles and / or by drying the mineral by air injection and / or temperature increase and / or by periods without addition of solutions and, where in stage II the cell can be covered or covered during the drying cycles.
- the concentrations of salts to be replaced in the continuous regime system are between 5 and 20 kg / t.
- steps I, II and III of the method can be repeated one or more successive times until the greatest extraction of the desired metal is achieved.
- the sulphurated minerals and / or mineral concentrates are subjected to drying cycles ranging from 15 to 90 days, where it generates the supersaturation condition and the crystallization of salts and precipitation of soluble chlorinated metal species occurs.
- the sulphided mineral that can be of primary origin mainly chalcopyrite
- the sulphurized mineral that may be of secondary origin mainly chalcosine and covelin, is subjected to 2 or 3 drying cycles ranging from 15 to 45 days, preferably 15-day cycles.
- step III the mineral is washed by continuous or intermittent irrigation with a solution containing acidified water, or acid and chloride.
- the metals to be solubilized are selected from the group that includes copper, zinc, nickel, molybdenum, cobalt, lead, among others.
- stage III in stage III it is washed, by limited or prolonged irrigation, promoting the presence of Cu (I) or Cu (II), respectively.
- the solubilization of the target metal can be carried out in the same way from sulphured minerals with arsenical contents and / or concentrated arsenical sulphurous minerals that contain it.
- steps I, II and III can be applied to copper minerals and / or concentrates, preferably chalcopyrite, bornite, tennantite, enargite, chalcoxin and covelin.
- stage II can be applied in a drying chamber or greenhouse, which allows a constant kinetics of evaporation of the liquid to be generated.
- the chloride ions can be incorporated into the method in the form of bischophyte, sodium chloride, potassium chloride, magnesium chloride, ferrous chloride, ferric chloride, calcium chloride or through the use of recirculating solutions of the same method containing chloride, iron and copper ions.
- the metal to be solubilized is copper and the sulphided mineral is a sulphided secondary mineral of copper.
- step II is carried out in a solid-liquid-solid condition.
- stages I of wetting and II of drying and supersaturation can be performed at pH between 0.5 and 5.
- stages I of wetting, II of drying and supersaturation and III of washing can be carried out independent of the potential, below 700 mV or above 700 mV (Eh).
- washing step III can be carried out with a reused solution with the presence of chloride and iron ions.
- steps I and II can use chloride salts, which can come from seawater, desalination plant brines, halite, bischophyte, and commercial sodium chloride.
- steps I, II and III can be carried out at room temperature, preferably between 20 to 40 ° C.
- the solution obtained from step II can follow the traditional steps of solvent extraction and electrowinning or go directly to electrowinning.
- Table 1 shows the quantitative mineralogical analysis obtained for four top samples of copper sulphide minerals, named as Mineral 1, 2, 3 and 4.
- Mineral 1, 2, 3 and 4 used light microscopy and modal analysis, supported by sequential copper chemical analysis.
- the mineralogical analysis for total copper indicated that there were low and high grade minerals; however, by copper species, the analysis showed that for Minerals 1, 2, 3 and 4, the chalcopyrite percentage is 99.8%, 81.7%, 45% and 11.7% respectively.
- Example 2 Copper extraction in relation to the acid concentration in the step of
- the Thermal Drying stage was started, directly on the column, for a period of 45 days.
- the third stage of washing began, with an irrigation rate of 5 L / h / m for 12 hours, using a sodium chloride solution of 180 g / L at pH 1.
- Example 3 Copper extraction in relation to the percentage of humidity in the
- the third stage of Washing began with an irrigation rate of 5 L / h / m for 24 hours, using an artificial refining solution containing 180 g / L chloride. sodium, 5 g / L of ferric, 2 g / L of ferrous and 10 g / L of acid.
- the Drying and Oversaturation stage began, for a period of 45 days, where there was no irrigation and the columns were covered, to maintain the temperature 25-30 ° C.
- the third stage of washing began at an irrigation rate of 7 L / h / m for 12 hours, using an artificial refining solution containing 180 g / L sodium chloride, 5 g / L of ferric, 2 g / L of ferrous and 10 g / L of acid.
- Example 5 Copper extraction in relation to the drying time in the Drying stage
- the Drying and Oversaturation stage began for different periods of time (5, 15, 30, 45, 60 and 90 days).
- the third stage of washing began with an irrigation rate of 5 L / h / m for 24 hours with an artificial refining solution containing 180 g / L chloride sodium, 5 g / L ferric, 2 g / L ferrous and 10 g / L acid.
- Example 6 Copper extraction in relation to the simulation of a continuous regime, using Mineral 1.
- Example 7 Copper extraction in relation to the first cycle of the Solid-Liquid-Solid method versus Prolonged Curing Times, using Mineral 1. The results of Figure 6 were obtained in column tests, using Mineral 1.
- the minerals were subjected to a traditional crushing process until reaching a particle size of 100% under 1 ⁇ 2 inch. Subsequently, six loads of said mineral were prepared, immediately the mineral loads were subjected to the Wetting stage, performing the agglomeration and curing process with the addition of water and acid together for the SLS method and separately for the test of prolonged cure.
- the four long cure tests were fillers, 2 for a 60 day cure and 2 for a 120 day period, as shown in Example 8.
- the addition of bischophyte and sodium chloride solidly directly onto the mineral was performed with the following concentrations and conditions:
- Example 8 Copper extraction in relation to two cycles of the Solid-Liquid-Solid method versus Prolonged Curing Times of 120 days, using Mineral 1.
- the third stage of Washing and Irrigation for all tests was started, at an irrigation rate of 10 L / h / m for 12 hours, using an artificial refining solution that it contained 180 g / L sodium chloride, 5 g / L ferric, 2 g / L ferrous and 10 g / L acid.
- the minerals were subjected to a traditional crushing process until reaching a particle size of 100% under 1 ⁇ 2 inch. Subsequently, two loads of said mineral were prepared, immediately all the mineral loads were subjected to the Wetting stage, where agglomeration and curing were carried out with the addition of water and acid together. The addition of bischofita and sodium chloride in solid form directly on the mineral was carried out with the following concentrations and conditions:
- Example 10 Copper extraction in relation to the Solid-Liquid-Solid method versus Prolonged Curing Times, using 1 m columns.
- the Washing stage was started with an irrigation rate of 5 L / h / m for 24 hours with an artificial refining solution containing 200 g / L sodium chloride, 5 g / L of ferric, 2 g / L of ferrous and 10 g / L of acid and 240 g / L of bischofite, 5 g / L of ferric, 2 g / L of ferrous and 10 g / L of acid.
- a second drying cycle was started for 60 days.
- irrigation was started at a rate of 5 L / h / m for 24 hours with an artificial refining solution of 150 g / L sodium chloride, 5 g / L of ferric, 2 g / L of ferrous and 10 g / L of acid.
- irrigation-rest periods were carried out every 5 days at a rate of 5 L / h / m for 12 hours, until the 120 days of testing were reached.
- the S-L-S method presents a higher concentration of copper, with respect to total iron, with a copper-iron ratio of approximately 5: 1 for sodium chloride and almost 10: 1 for bischophyte. In contrast, in prolonged curing the copper to iron ratio is approximately 1: 1 for both salts. It can also be seen that the redox potentials are similar and no significant differences are observed indicating that the potential difference may affect the solubilization of copper.
- Example 11 Irrigation Ratio in relation to the Solid-Liquid-Solid method versus Times
- Example 12 Copper extraction in relation to the Solid-Liquid-Solid method versus Prolonged Curing Times, using Mineral 2.
- the Washing stage was started with an irrigation rate of 5 L / h / m for 24 hours with an artificial refining solution containing 200 g / L sodium chloride, 5 g / L of ferric, 2 g / L of ferrous and 10 g / L of acid and 240 g / L of bischofite, 5 g / L of ferric, 2 g / L of ferrous and 10 g / L of acid.
- a second drying cycle was started for another 60 days.
- irrigation was started at a rate of 5 L / h / m for 24 hours with an artificial refining solution of 150 g / L chloride. sodium, 5 g / L of ferric, 2 g / L of ferrous and 10 g / L of acid.
- stand-by irrigation was performed every 5 days at a rate of 5 L / h / m for 12 hours, until reaching 120 test days.
- Example 13 Copper extraction in relation to the solid-liquid-solid (SLS) method versus Bioleaching and Chlorinated Leaching, using Mineral 3
- SLS solid-liquid-solid
- Example 13 Copper extraction in relation to the solid-liquid-solid (SLS) method versus Bioleaching and Chlorinated Leaching, using Mineral 3
- the results of Figure 12 were obtained in tests in 1 m columns, using Mineral 3, the which has a total copper grade of 0.36% and a percentage by copper species of 45% chalcopyrite (see Table 1).
- the minerals were subjected to a traditional crushing process until reaching a particle size of 100% under 1 ⁇ 2 inch. Subsequently, 3 loads of said mineral were prepared, immediately the mineral loads were subjected to the Wetting stage, performing the agglomeration and curing process with the addition of water and acid together for the SLS method and separately for the test of Chlorinated leaching and Bioleaching.
- the addition of chloride Sodium in solid form directly on the mineral was made with the following concentrations and conditions:
- the chlorinated leaching and bioleaching tests were carried out on lm columns by a metallurgical laboratory expert in this type of tests.
- the classic secondary sulphide leaching methods were carried out in Mineral 3.
- the chlorinated leaching was carried out with a concentration of 150 g / L of sodium chloride, 30 kg / t of acid and 10% humidity. The process lasted 90 days, through stages of irrigation and rest.
- the test was performed with a bacterial consortium composed of oxidizing iron and sulfur microorganisms, 10% humidity and 50 kg / t of acid. The process lasted 90 days through irrigation-rest stages.
- Example 14 Water supply by use of Bischofita in the wetting stage to achieve a humidity of 6% and 10%.
- Example 15 Copper extraction using the solid-liquid-solid method in Mineral 4.
- the results of Figure 14 were obtained from column tests, using Mineral 4, which has a total copper grade of 0, 67% and a percentage by copper species of 76.24% of chalcoxine and 11.7 chalcopyrite (see Table 1).
- the minerals were subjected to a traditional crushing stage to achieve a 100% particle size under 1 ⁇ 2 inch. Subsequently, 2 loads of said mineral were prepared, immediately the mineral loads were subjected to the SLS method, starting with the Wetting stage, where it agglomerated with the addition of water and acid together, according to the conditions described below :
- the Washing and rewetting stage began with an irrigation rate of 5 L / h / m for 24 hours with an artificial refining solution containing 200 g / L chloride. sodium, 5 g / L of ferric, 2 g / L of ferrous and 10 g / L of acid. Then a second drying cycle was started for another 15 days. After the time of the second cycle of drying, the second wash was performed with an acidified pH 1 solution at an irrigation rate of 5
- a high copper extraction is expected to occur during the test on a mineral that has a total copper greater than 70% in the form of chalcosine.
- the solid-liquid-solid method according to the invention with only two 15-day cycles it is possible to extract the maximum concentration of copper.
- Example 17 Extraction of copper in a chalcopyrithic concentrate, using the method
- the second stage of the process began, where the concentrates were stored in a drying chamber at 30 ° C for 25 days.
- the third stage of the process began, where the concentrate was transferred to the washing pools, carrying out the process with a solution at pH 1 for 30 minutes. Once the washing was carried out, the concentrate was filtered and subsequently dried to start a second cycle of Wetting and Drying.
- the sample was subjected to the Wetting step, where 100 kg / t of NaCl, 100 kg / t of bischofite and 100 kg / t of FcChx 63 ⁇ 40 were added in solid form to the concentrate.
- the concentrate was weighed, then the sample was subjected to the Wetting step, which consisted of adding 100 kg / t of ferric sulfate to the concentrate in solid form, and then a solution was added composed of water and acid with 2 g / L of ferrous and 3 g / L of ferric, until reaching a final humidity of 12%.
- the second stage of the process began, where the concentrates were stored in a drying chamber at 30 ° C for 25 days.
- the third stage of the process began, where the concentrate was transferred to the washing pools, carrying out the process with a solution at pH 1 for 30 minutes. Once the washing was done, the concentrate was filtered and then dried to start a second cycle of Wetting and Drying.
- Example 18 SEM microscopy images of Concentrate 1 after the Wetting and Drying step.
- Image A General image of the concentrate sample, where the precipitates can be identified throughout the sample and that were generated during the second stage of the method.
- Image B Specific area of general image A (white circle), where you can see in detail the shape of the precipitates and crystals, which correspond to copper and chlorine complexes, presenting a shape defined by the loss of moisture during the drying and supersaturation stage.
- Image C Specific area of general image A (black circle), where you can see in detail the shape of the precipitates and crystals, which correspond to copper and chlorine complexes, presenting a shape defined by the loss of moisture during the drying and supersaturation stage.
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Priority Applications (18)
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MX2021005466A MX2021005466A (es) | 2018-11-14 | 2019-10-29 | Metodo hidrometalurgico solido-liquido-solido para la solubilizacion de metales a partir de minerales y/o concentrados sulfurados de cobre. |
BR112021009356-7A BR112021009356A2 (pt) | 2018-11-14 | 2019-10-29 | Método hidrometalúrgico sólido-líquido-sólido para a solubilização de metais a partir de minerais e/ou concentrados de sulfeto de cobre |
PE2021000715A PE20211766A1 (es) | 2018-11-14 | 2019-10-29 | Metodo hidrometalurgico solido-liquido-solido para la solubilizacion de metales a partir de minerales y/o concentrados sulfurados de cobre |
CN201980080843.8A CN113166845B (zh) | 2018-11-14 | 2019-10-29 | 用于从硫化铜矿物和/或精矿溶解金属的固-液-固湿法冶金方法 |
CA3120395A CA3120395C (en) | 2018-11-14 | 2019-10-29 | Solid-liquid-solid hydrometallurgical method for the solubilization of metals from sulfide copper minerals and/or concentrates |
US17/292,585 US20220002838A1 (en) | 2018-11-14 | 2019-10-29 | Solid-liquid-solid hydrometallurgical method for the solubilization of metals from sulfide copper minerals and/or concentrates |
EP19809914.5A EP3882366A1 (en) | 2018-11-14 | 2019-10-29 | Solid-liquid-solid hydrometallurgical method for the solubilization of metals from sulfide copper minerals and/or concentrates |
MX2022005072A MX2022005072A (es) | 2018-11-14 | 2020-10-01 | Procedimiento hidrometalurgico solido-liquido-solido optimizado para aumentar la solubilizacion de metales a partir de minerales y/o concentrados en medio acido-clorurado. |
BR112022008222A BR112022008222A2 (pt) | 2018-11-14 | 2020-10-01 | Processo hidrometalúrgico sólido-líquido-sólido otimizado para aumentar a solubilização de metais a partir de minérios e/ou concentrados em meio de cloreto de ácido |
EP20800781.5A EP4053297A1 (en) | 2018-11-14 | 2020-10-01 | Solid-liquid-solid hydrometallurgical process optimized to increase the solubilization of metals from ores and/or concentrates in acid-chloride medium |
US17/772,470 US20220356544A1 (en) | 2018-11-14 | 2020-10-01 | Solid-Liquid-Solid Hydrometallurgical Process Optimized to Increase the Solubilization of Metals from Ores and/or Concentrates in Acid-Chloride Medium |
PCT/CL2020/050110 WO2021081679A1 (es) | 2018-11-14 | 2020-10-01 | Procedimiento hidrometalúrgico sólido-líquido-sólido optimizado para aumentar la solubilización de metales a partir de minerales y/o concentrados en medio ácido-clorurado |
CN202080082881.XA CN114761586A (zh) | 2018-11-14 | 2020-10-01 | 经优化以提高在酸-氯化物介质中从矿石和/或精矿溶解金属的固-液-固湿法冶金方法 |
CA3159331A CA3159331A1 (en) | 2018-11-14 | 2020-10-01 | Solid-liquid-solid hydrometallurgical process optimized to increase the solubilization of metals from ores and/or concentrates in acid-chloride medium |
PE2022000690A PE20221212A1 (es) | 2018-11-14 | 2020-10-01 | Procedimiento hidrometalurgico solido-liquido-solido optimizado para aumentar la solubilizacion de metales a partir de minerales y/o concentrados en medio acidoclorurado |
AU2020376989A AU2020376989B2 (en) | 2018-11-14 | 2020-10-01 | Solid-liquid-solid hydrometallurgical process optimized to increase the solubilization of metals from ores and/or concentrates in acid-chloride medium |
CL2021003432A CL2021003432A1 (es) | 2018-11-14 | 2021-12-21 | Procedimiento hidrometalúrgico sólido-líquido-sólido optimizado para umentar la solubilización de metales a partir de minerales y/o concentrados en medio ácido-clorurado |
ECSENADI202241277A ECSP22041277A (es) | 2018-11-14 | 2022-05-24 | Procedimiento hidrometalúrgico sólido-líquido-sólido optimizado para aumentar la solubilización de metales a partir de minerales y/o concentrados en medio ácido-clorurado |
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PCT/IB2019/059258 WO2020099966A1 (es) | 2018-11-14 | 2019-10-29 | Método hidrometalúrgico sólido-líquido-sólido para la solubilización de metales a partir de minerales y/o concentrados sulfurados de cobre |
PCT/CL2020/050110 WO2021081679A1 (es) | 2018-11-14 | 2020-10-01 | Procedimiento hidrometalúrgico sólido-líquido-sólido optimizado para aumentar la solubilización de metales a partir de minerales y/o concentrados en medio ácido-clorurado |
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2018
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PE20211766A1 (es) | 2021-09-07 |
US20220356544A1 (en) | 2022-11-10 |
MX2021005466A (es) | 2021-06-18 |
CN113166845A (zh) | 2021-07-23 |
PE20211138A1 (es) | 2021-06-25 |
US20220042139A1 (en) | 2022-02-10 |
CA3120395A1 (en) | 2020-05-22 |
BR112021009356A2 (pt) | 2021-09-28 |
WO2021081679A1 (es) | 2021-05-06 |
MX2022005072A (es) | 2022-05-19 |
CN113166845B (zh) | 2022-10-21 |
CL2021001218A1 (es) | 2021-12-24 |
AU2020376989A1 (en) | 2022-06-09 |
CA3120395C (en) | 2024-01-23 |
EP3882366A1 (en) | 2021-09-22 |
CL2021003432A1 (es) | 2022-10-14 |
CA3159331A1 (en) | 2021-05-06 |
EP3882365A1 (en) | 2021-09-22 |
PE20221212A1 (es) | 2022-08-11 |
US20220002838A1 (en) | 2022-01-06 |
EP4053297A1 (en) | 2022-09-07 |
ECSP22041277A (es) | 2022-06-30 |
BR112022008222A2 (pt) | 2022-07-12 |
CN114761586A (zh) | 2022-07-15 |
WO2020099912A1 (es) | 2020-05-22 |
AU2020376989B2 (en) | 2023-09-14 |
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