SOLID-LIQUID-SOLID HYDROMETALLURGICAL METHOD FOR THE SOLUBILIZATION OF METALS FROM COPPER SULFIDE ORE AND / OR CONCENTRATES

Abstract

The present invention relates to a Solid-Liquid-Solid (SLS) hydrometallurgical method in the presence of hydrated and / or non-hydrated salts under supersaturation conditions. This method enhances the chemical and physical reactions on the ore or concentrates, thereby causing crystallization, recrystallization, and release of copper through non-stoichiometric decomposition of the sulfide, followed by precipitation with chloride. The invention comprises three stages: a) Wetting, b) Drying and Supersaturation, and c) Washing and Re-wetting. These stages occur at temperatures of 20 to 40°C, regardless of the redox potential, with minimal water and acid consumption and without the need for oxygen addition. The method reduces acid and water consumption because the sulfide transformation can be achieved using only hydrated salts and / or minimal acid and water.Furthermore, the present invention allows for a reduction in water usage during the agglomeration and / or agglomeration-curing stage. This is because, when the hydrated salt is mixed with the mineral, the water molecules in the hydrated salt moisten the mineral, reducing the volume of water that must be added during the wetting and agglomeration and / or curing stages. The method of the present invention can also be applied to sulfide base metals such as nickel, zinc, cobalt, lead, and molybdenum, among others, regardless of common impurities in sulfide minerals, such as the presence of arsenic.

Description

SOLID-LIQUID-SOLID HYDROMETALLURGICAL METHOD FOR THE SOLUBILIZATION OF METALS FROM SULFIDE COPPER MINERALS AND / OR CONCENTRATES. FIELD OF INVENTION The present invention relates 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 sulfides, mainly chalcopyrite, to obtain a desired metal. BACKGROUND OF THE INVENTION In recent decades, there has been significant growth in the production and consumption of minerals, mainly due to developing countries entering the global market. Mineral resources and climate change are closely linked, not only because mining requires large amounts of energy and water, but also because the world cannot address climate change without an adequate supply of raw materials to manufacture clean technologies (Alonso E. et al., 2012; Elshkaki A, et al., 2016). The mining industry is one of the industrial sectors with high energy and water consumption, which is why there is great concern about water and energy requirements and the potential environmental impacts in the future.The future availability of metals and other mineral products will depend on economic and market factors (metal prices, supply and demand), technological developments to improve extraction, and social and environmental pressures (Franks D. et al., 2014; Cochilco., 2017; Schipper B., et al., 2018). Global copper production and demand have increased significantly over the past 25 years due to population growth, economic expansion, and societal transitions toward sustainability (USGS, 2009). Copper is a widely used metal and is essential in various economic sectors, such as infrastructure, wiring, electric vehicles, electrical and electronic equipment, and renewable energy (Elshkaki A, et al., 2018). However, its Copper production has high energy and water consumption, and therefore a significant environmental impact, which will worsen in the coming decades due to a projected increase of over 200% in copper demand by 2050 (Elshkaki A. et al., 2016; Kuipers K. et al., 2018). Recent studies on the criticality and short-term risk assessment of mineral supply suggest that in the next two to three decades, the copper industry will have considerable difficulty meeting global demand, and substitutes are not readily available (Elshkaki A. et al., 2016; Meinert L. et al., 2016; Schipper B., et al., 2018). However, recycling this metal can help meet future demand to some extent. Climate change has had a significant impact on ecosystem changes and desertification, as well as generating unexpected weather phenomena, such as rain in areas where it didn't previously rain, and heat waves and cold spells in different parts of the world. Northern Chile, the region where most of the country's copper production is concentrated, has been affected by rains that have had a significant impact on copper production in the first three months of 2019, decreasing production by 5.1% compared to 2018. These rains have also caused serious damage to some mining operations, as some deposits were not designed to withstand heavy rainfall, leading to a halt in mining operations. According to COCHILCO, this resulted in losses of US$300 million.On the other hand, concern is focused on the active and inactive tailings dams in the northern zone, since the increase in the flow of the highland rivers and the heavy rains could cause a collapse of the dams, generating danger for the population and the environment. Chalcopyrite is the most abundant primary copper sulfide and represents approximately 70–80% of the world's copper reserves (Hall et al., 1973; Kaplun et al., 2011). This mineral is stable and is the most resistant sulfide to hydrometallurgical processes. Furthermore, the formation of a passivating layer has been observed when subjected to a variety of leaching agents, further hindering its dissolution (Dreisinger, 2006; Veloso et al., 2016). Enargite, also a primary copper sulfide, is found mainly in deposits in Peru and Chile. It is of environmental concern as a source of arsenic and requires special attention in the QQhcnn / ιζηζ / E / γίΛΐ smelters. Therefore, most smelters penalize the arsenic content in concentrates. Furthermore, arsenic is considered the most dangerous inorganic contaminant, causing environmental and health emergencies in various parts of the world (Mandal B. et al., 2002). The hydrometallurgical processes that have been developed to leach copper ores and / or concentrates are based on solid-liquid, solid-liquid-gas, or solid-liquid-gas-bacterial methods, where different reagents are used that act mainly as oxidizing agents. These processes could be divided into: chloride, nitrate, sulfate, ammoniacal, iodide, and bacterial, among others.However, regardless of the leaching agent used, it is always in an aqueous medium, with high concentrations of sulfuric acid, and ferric and / or cupric ions are typically used as oxidizing agents, in addition to the presence of oxygen and constant irrigation (Dutrizac, 1991; Habashi F, 1993; Domic E, 2001; Dreisinger, 2006; Senanayake, 2009; Kawashima et al., 2013; Waltling, 2014; Veloso et al., 2016). For the specific case of chalcopyrite and enargite concentrates, it can be added that most processes are carried out at temperatures above 80 degrees Celsius (McDonald et al., 2007a; Gupta, 2010; Waltling, 2014). The first use of chloride ions in metallurgy dates back to the 16th century in a process for amalgamating silver. The next important process was in 1860, when cuprous chloride was used for the direct decomposition of silver sulfide, which can be considered the beginning of the use of chloride in hydrometallurgy (Liddell, 1945). Since then, numerous investigations into chloride leaching have been carried out for the dissolution of sulfide minerals and copper concentrates (Dutrizac, 1991). The processes developed were mainly based on solid-liquid and solid-liquid-gas methods using chloride with oxidizing agents, such as cupric chloride (CuCb) and ferric chloride (FeCb), due to the advantages related to the high solubility of copper and ferric ion, sulfur control, and process economy (Dutrizac and MacDonald, 1974; Dutrizac J., 1981; Dutrizac 1, 1991; Habashi F, 1993; HavIikT.etaL, 1995; Domic E, 2001; Dreisinger, 2006; Carneiro, 2007; Nicol et L, 2016). For decades in the world's leading copper producer, mining activity has generated a A significant decrease in freshwater levels in the northern part of the country has led to complaints from local communities about water availability. In a belated response, the General Directorate of Water (DGA) has doubled the number of prohibited zones across Chile, from 30 to 70. These zones include mining areas, making it more difficult for mining companies to extract freshwater. Furthermore, mining companies' water demand is expected to increase in the future due to declining ore grades, which necessitates processing more material to maintain production levels (Bloomberg, February 21, 2019). The Escondida mine, owned by BHP, and the Zaldívar mine, owned by Antofagasta Hiñerais, are clear and complex examples of freshwater use in northern Chile. Both mines will need to adjust their current extraction levels if they wish to continue operating, as the aquifer's water availability is insufficient to maintain those levels. In the case of Zaldívar, it will have to close if it does not renew its water license, as it lacks an alternative plan. Conversely, Escondida inaugurated its desalination plant to extract seawater from 3,000 meters above sea level for its operations and has ambitiously set goals to cease using freshwater by 2030 (Bloomberg, February 21, 2019). Water scarcity in mining areas, such as northern Chile and southern Peru, has led mining operations to use seawater, either through desalination or direct use in the leaching process. The best water quality for mineral dissolution processes does not necessarily require complete desalination, as the presence of certain ions, such as chloride ions, can be beneficial in dissolving the mineral (Dixon, 2013; Cisternas et al., 2017). Seawater use in copper mining in Chile increased significantly between 2010 and 2015, and is projected to triple by 2029. Despite this, freshwater use in large-scale mining in the country is expected to grow by 12% by 2029 (Cochilco, 2017). The leaching of copper sulfides with seawater is associated with the use of chloride in the oxidative dissolution of secondary sulfides, such as chalcocite and covellite. Conversely, the use of chloride in the dissolution QQhcnn / 1 ζηζ / Ε / γίΛΐ of chalcopyrite has not been effective, due to slow kinetics and incomplete dissolution (Dreisinger, 2006; Al-Harahsheh etal, 2008; Nicol et al, 2016; Lundstrom M. etal, 2016; VelásquezY. etal, 2018). Chile produces one-third of the world's copper, and a significant shift in the final copper mining product structure is projected. This projection indicates that hydrometallurgical production will decrease from 30.8% to 12% by 2027, and concentrate production will rise from 69.2% to 89.9% by the same year (Cochilco, 2017). Unit water consumption for a concentrator plant in 2016 reached 0.5 m³ / min; however, for hydrometallurgy, consumption was only 0.1 m³ / min, resulting in significantly lower water usage in hydrometallurgical processes (Cochilco, 2017). The decrease in hydrometallurgical processing of the extracted ore is due to the depletion of leachable resources, the appearance of refractory primary minerals (chalcopyrite), and consequently, the closure of mining operations. Furthermore, the appearance of primary sulfides means that high-grade ore is primarily processed by flotation, leading to idle capacity in hydrometallurgical facilities. This is because no cost-effective hydrometallurgical technology for treating low-grade copper primary sulfides has been reported at an industrial level (Cochilco, 2017). On the other hand, the increased production of concentrates will lead to an increase in environmental liabilities (tailings) and in the processing capacity of smelters. Copper smelters involve three main processes: smelting, converting, and refining. All of these processes generate gases, such as carbon dioxide (CO2) and sulfur dioxide (SO2), which, if not recovered during the smelting process, are released into the environment, causing significant environmental impact and harming human health. In 2013, the Chilean state enacted Supreme Decree 28, which establishes emissions standards for copper smelters, with the aim of reducing emissions of sulfur dioxide (SO2), arsenic (As), and mercury (Hg), and with the objective of protecting human health and the environment. Decree QQhCOn / 1 7P7 / E / YILI establishes that the seven existing smelters must capture and fix more than 95% of the sulfur and arsenic by weight entering the process, well below the standards set by smelters in Europe and Asia, which are required to capture 99.9% of emissions. In 2018, four of the seven smelters in the country were not in compliance with the decree, mainly due to the high costs of investment, equipment upgrades, and the construction of sulfuric acid plants, all aimed at modernizing the smelters and meeting the regulations established for the new emission limits (Ramírez 1, 2019, Chilean Mining). DESCRIPTION OF PREVIOUS ART Hydrometallurgy is the science and technology of extracting metals or materials using aqueous methods (Habashi F, 1993). In general, this branch of extractive metallurgy is carried out in three different and sequential physicochemical stages: 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 them. More recently, with the depletion of high-grade ores and the abundance of low-grade primary ore, hydrometallurgy has emerged as a potentially economically viable option for processing these low-grade ores (Habashi, 2005).The selective dissolution of a solid using an aqueous solution has been applied to copper heaps, proving to be a well-established and successful process for oxidized ores and secondary copper sulfides, such as chalcocite and covellite. However, for primary sulfides, such as chalcopyrite, it remains a significant challenge for copper mining, both for ores and concentrates (Dreisinger, 2006; Nicol et al., 2016; Liu et al., 2017; Velásquez et al., 2018). The chemical leaching of minerals involves heterogeneous phenomena where the reaction takes place at the interface between a solid and a liquid, including solid-liquid, solid-liquid-gas, and solid-liquid-gas-bacterial interactions (Habashi F., 1999; Domic E., 2001; Dixon and Petersen, 2003). Generally speaking, the dissolution of a mineral in an aqueous medium can be described as... QQhcnn / 1 znz / E / YiAi governed by diffusional steps (Wen C., 1968; Crest A., 2000; Dixon and Petersen, 2003). In contrast, heterogeneous reactions involving solid-gas and solid-solid phases at room temperature, without the intervention of a liquid phase, have an extremely slow reaction rate (Lefebvre R.., 2001; Evans K., 2006). Chalcopyrite (CuFeS2), enargite (Cu3ASS4), and bornite (CusFeSi) are primary copper sulfide minerals, refractory and semiconducting like most sulfide minerals, with a crystalline structure in which iron and copper ions are in tetrahedral coordination with sulfur, in the case of chalcopyrite (Hall S. et al., Nikiforov K., 1999). Spectroscopic measurements of chalcopyrite and bornite have identified that the electronic structure of both minerals is the same for copper (Cu1+) and iron (Fe3+), with a molecular weight for the former of 183.52 g / mol and for the latter of 501.8 g / mol, with each atom contributing the following percentages to their atomic weight: Cu 34.6%; Fe 30.4%; S 34.9% and Cu 63.3%; Fe 11.1%. S 25.5% respectively (Grguric B. et al, 1998; Mikhlin et al, 2004, Pearce et al, 2006).Enargite (CU3ASS4) is a copper sulfide with arsenic, like chalcopyrite and bornite it has a valence of +1 for copper; however, it has a molecular weight of 393.8 g / mol and each atom in its atomic weight is given by the following percentages; Cu 48.4%; As 19.0%; and S 32.6% (Li D. et al., 1994; Arribas J. 1995; www.mindat.org). The slow extraction kinetics of copper from primary sulfides under oxidative and / or reductive conditions in the presence of low and high chloride concentrations has generated a large body of research aimed at understanding primarily the oxidative dissolution of this mineral. This research is summarized in the following publications (Debernardi and Carlesi, 2013; Kawashima et al., 2013). Furthermore, it is proposed that the use of chloride in chalcopyrite dissolution faces several challenges for its implementation in a heap leaching process. One of these challenges is achieving the regeneration of oxidizing agents such as cupric and ferric ions, as well as controlling pH, redox potential, and passivation. This latter phenomenon is proposed to be generated by the formation of different compounds, such as disulfide dichloride (S₂Cl₂) and sulfur. QQhcnn / ιζηζ / E / γίΛΐ elemental, non-stoichiometric secondary sulfides and chlorocuprate I complexes, which are absorbed by the surface of the mineral (Lu et al, 2000; Carneiro, 2007; Lundstróm et al, 2016; Nicol, 2017; Liu et al, 2017). Copper ions can form complexes with chloride ions, and the prevalence of the complex depends on the chloride concentration and the leaching environment. In solutions with high chloride concentrations, cuprous complexes [CuCb]', [CuCb]'2, [Cu2Cl4]·2, [CusCb]'3 are more prevalent than cupric complexes [CuCl]+, [CuCb]0, [CuCb], [CuCb]2', whose solubility decreases as the chloride concentration increases. Conversely, the solubility of chlorocuprate(I) complexes increases with increasing chloride concentration (Berger and Winand, 1983; Fritz, 1980, 1981; Lin et al., 1991; Winand, 1991; Yoo et al., 2010).The beneficial effect of chlorocuprate I complexes on the dissolution of chalcopyrite has been little studied and they are considered dissolution inhibitors, therefore, the aim is to maximize the presence of cupric ions as an oxidizing agent, over chlorocuprate I complexes (Winand, 1991; Liu et al., 2017). The use of chloride in the dissolution of chalcopyrite in an oxidative medium has been applied using saturated and unsaturated chloride solutions. It has been found that, at low and high chloride concentrations, passivation of the mineral could be avoided due to the low redox potentials achieved under these conditions (Velásquez et al., 2010; 2018). Conversely, the use of concentrated chloride and acid solutions has improved the dissolution of primary sulfides through long curing and pretreatment periods of the mineral, which is subsequently subjected to a leaching process at low or high redox potentials (Patiño et al., 2014; Velásquez et al., 2018). Recent studies by Velásquez (Velásquez et al., 2018) show that increasing curing periods helps to solubilize primary sulfides. However, the process results in an incomplete dissolution of chalcopyrite.Conversely, at temperatures of 50°C, the solubilization of a chalcopyrite concentrate in a flooded medium (reactor) increases to over 85%. Furthermore, studies derived from Patiño's results show that solubilization... The extraction of copper from a chalcopyrite concentrate with concentrated chloride solutions in an oxidizing medium only achieved a copper extraction of 19% (Lundstrom M. et al., 2016). Furthermore, it is proposed that chalcopyrite is oxidized to covellite, contrary to the proposal by Pihlaso et al. (2008), who mention the formation of chalcocite. The use of high concentrations of a reagent can increase the reaction rate; however, it could also generate unwanted side reactions and be economically unfeasible (Habashi F., 1999). Moreover, it becomes economically unfeasible due to the need to constantly transport large quantities of salts to the operation to maintain a constant supply. On the other hand, some studies propose that chalcopyrite could be reduced by cuprous ions in an aqueous medium with acetonitrile and / or chloride at high temperatures, reducing chalcopyrite to chalcocite or bornite (Avraamides et al., 1980; Winand, 1991).Furthermore, according to thermodynamic studies, it is proposed that chlorocuprate I complexes in a chloride medium increase the critical potential, which would lead to increased copper extraction from chalcopyrite, following the model proposed by Hiroyoshi (Yoo et al., 2010). However, there is a limited amount of thermodynamic research on concentrated chloride solutions, making this an underexplored field (Fritz, 1980, 1981; Winand, 1991; Yoo et al., 2010). During the mechanical preparation of the ore, fine particles are generated, which can affect the permeability of the heap. Agglomeration is a stage that is generally carried out before leaching in secondary oxide and sulfide heaps, and consists of joining the fine particles to the coarser ones, in order to increase the permeability coefficient in the heap, and thus be able to have efficient irrigation and aeration conditions to improve the extraction process (Bouffard S.C., 2005, 2008). Therefore, the agglomeration stage is vital for maintaining good hydrodynamics in the heap and preventing pooling. The simplest agglomeration stage is carried out by adding water and acid to moisten the ore until optimal surface tension is achieved. Therefore, the presence of water in the agglomeration stage is crucial, since without water there are no agglomerates and no adequate acid distribution, which would lead to inefficient curing (Domic E., 2001; Lu. 1 et al., 2017). QQhCnn / 1 7Π7 / E / YILI Furthermore, during this stage, the ore is also cured by adding concentrated sulfuric acid so that it acts on all the ore particles and creates optimal conditions for the leaching process. The acidity of the curing stage and the leaching solutions is crucial, as it interacts with both the ore and the gangue. Therefore, a lack of acid could negatively impact copper extraction (Bouffard SC, 2005; Lu et al., 2017). The agglomeration and curing mechanism and equipment can be implemented by adding water and then acid to the ore on a conveyor belt, or by using an agglomeration drum that allows a moist particle to rotate, enabling efficient agglomeration formation (Domic E., 2001). Weathering is defined as the fragmentation or partial or total degradation of rocks and minerals upon contact with atmospheric agents. The natural weathering of rocks or minerals occurs through chemical reactions (chemical weathering) and various mechanical disintegration processes (physical weathering), such as thermal stress, the increase in volume of clay minerals, and the growth of crystals in rock dyadases due to phase changes. The relevant changes that occur due to solutions in rock pores are called solvent crystallization and correspond to a freeze-thaw crystallization process; however, when the process occurs due to a solute, it is called salt weathering or haloclasty. In both cases, there is an increase in pressure on the internal walls of the rock, which promotes its wear or fracturing (Wellman H. et al., 1965; Goudies A. et al., 1997; Smith l., 2006).Physical weathering by salts affects porous materials, such as rock outcrops and minerals. Chemical species (anions and cations) are transported by aqueous solutions, which can penetrate the minerals through their pores and / or joints. The concentration of salts in solution will vary during circulation through the mineral or rock, which can be caused by the following conditions: chemical interaction with the mineral, water evaporation, temperature variations, and variations in relative humidity. The increase in the concentration of a salt due to water evaporation, under given environmental conditions, will lead to its precipitation. QQhcnn / 1 ζηζ / E / γίΛΐ which will occur when the salt concentration is such that the solubility product is equal to or greater than the equilibrium constant. When the solubility product is equal to the equilibrium constant, the condition is equilibrium and the solution is called saturated, while when the solubility product is greater than the equilibrium constant, the condition is disequilibrium and the solution is called supersaturated (Grossi CM et al., 1994; Desarnaud J. et al., 2016). Chemical weathering and salt weathering represent different mechanisms of rock breakdown and generally operate together. However, it is difficult to differentiate their effects separately, as they are interrelated phenomena. This is because the products generated by the dissolution of minerals are used in subsequent salt weathering processes. An example of this is the generation of sulfates, which can be produced by sulfuric acid attack, whether from volcanic sources, atmospheric sulfur dioxide deposition, or the reactions inherent in rock dissolution. Sodium chloride and hydrated magnesium chloride are abundant salts found in nature, playing an active role as antifreeze and road pollution control agents. Inorganic chlorides are formed from the dissolution of hydracids and binary salts in aqueous media under certain homogeneous solubility conditions. The intermolecular forces of the solvent (for example, water) cause the complete breakdown of ionic and covalent bonds, allowing the salts to dissociate into their original polar ions: a valent metallic or non-metallic cation (H+, Na+, Mg2+, Fe3+, K+, etc.) and the chloride anion. Bischofite is a hydrated salt with the chemical formula MgCbxótLO. The active compound in bischofite is magnesium chloride, which has various physical properties, such as deliquescence and the ability to increase the surface tension and vapor pressure of water.This salt is obtained as a residue or byproduct of the solar evaporation process applied to brines extracted from certain salt flats, primarily in the Lithium Triangle, comprised of Chile, Argentina, and Bolivia, a process necessary for the extraction of lithium and potassium. Hydrated magnesium chloride, or bischofite crystals, is available worldwide. However, the bischofite produced in Chile has the advantage of being present in low concentrations. QQhcnn / 1 znz / E / YiAi of impurities. The main use of bischofite is for road stabilization; however, there are no production capacity restrictions for this salt, as the main producing companies have abundant bischofite deposits, which increase every year, with production far exceeding demand. For example, in 2015, bischofite sales were close to 150,000 tons, which corresponds to less than 10% of the total produced by the companies during that year, and the same occurred for the other years (National Economic Prosecutor's Office, 2017), demonstrating that supply greatly exceeds demand and that there is an opportunity to utilize this salt. Sodium and magnesium chloride salts are soluble salts with a tendency toward supersaturation. In solution, they are highly mobile and can penetrate deeply into fractures or joints in rocks, generating efflorescence and crystallization of the salts on the surface or within the mineral or rock, a characteristic feature of these two salts. The location of soluble chloride salts relative to the outer surface of a mineral depends on the saturation or supersaturation mechanism of the solution. If generated by evaporation, the mechanism is controlled by two processes acting simultaneously: the rate of evaporation and the rate of solution input through the mineral.If the vapor diffusion rate is lower than the solution migration rate, the solution will reach the external surface where it will evaporate and the salts will crystallize. This depends on the mode of heat transfer, whether by convection or radiation (Gómez-Heras et al., 2016). This latter phenomenon is called efflorescence. Conversely, if the solution migration rate is lower than the water vapor diffusion rate, equilibrium will be reached at a certain distance from the surface, resulting in cryptoefflorescence. Higher water vapor diffusion rates generate greater salt precipitation, thus intensifying this phenomenon. Crystallization inside the fractured mineral, due to the evaporation of aqueous solutions, will produce the growth of chloride crystals, which will generate pressures and loss of cohesion of the mineral (Winkler, 1973; Amoroso et al., 1983; Lewin, 1989; Desarnaud et al., 2016).Temperature variations and. The relative humidity of the air in contact with the precipitated salts induces dilution and precipitation processes of salts. However, these processes are accompanied by hydration and dehydration phenomena, which induce phase transitions, generating an increase in the size of the soluble salt crystals, and therefore, the fragmentation of the rock, a phenomenon called haloclasty (Gupta et al., 2014; Desarnaud et al., 2016). The evaporation of a liquid in a porous medium involves complex phenomena of liquid and vapor transport and phase changes. However, determining the evaporation rate, along with the evolution of the liquid distribution within the pore space as the liquid phase is replaced by the gaseous phase, is important for assessing supersaturation and predicting damage induced by salt crystallization. Slow evaporation processes are well known and can be exemplified by the evaporation of water from a solid at room temperature. In this case, evaporation rates are very low, and therefore, temperature variations due to the phase change are negligible (Prat M. et al., 2007).In the case of the use of saturated sodium chloride solutions, efflorescence is an important factor, since the crystallization process occurs mainly on the surface of the solid, which significantly decreases the evaporation kinetics, due to the blocking of the solid surface by the efflorescence (Sghaier N. et al., 2009), causing low physical damage inside the mineral. The redox potential is an important parameter in the methods and many of the technologies proposed for chalcopyrite dissolution, since it has been suggested that the formation of leaching products, considered passivating agents, is dependent on the potential of the medium. Low redox potentials favor higher copper extraction, while high redox potentials favor lower copper extraction (Elsherief, 2002; Hiroyoshi et al., 2001; Velásquez-Yévenes et al., 2010; 2018). However, the potential window in which these higher copper extractions are achieved is limited and difficult to control. This leads to a situation where, once the critical dissolution potential is exceeded, chalcopyrite extraction either stops completely or is only incomplete, due to the leaching products blocking the mineral surface. QQhcnn / ιζηζ / Ε / γίΛΐ its dissolution (Dixon & Petersen, 2006; L¡ eta / ., 2010; Ahmadi eta / ., 2010; Kaplun eta!, 2011; Nicol, 2017; Liu etal, 2017). Studies of chalcopyrite dissolution phenomena and mechanisms have focused on the types of leaching agents, dissolution parameters, redox potential, curing times, pretreatments, and passivation. Conversely, the role of the aqueous medium on the mineral surface has been largely overlooked, despite water and acid being the most abundant chemical species in hydrometallurgical processes. Furthermore, Oliveira C. et al. (2010) and Ferreira de Lima et al. (2011) studied water adsorption on the chalcopyrite surface at the molecular level and found the formation of sulfur dimers and hydrophobic zones. These findings are proposed by the authors as a possible explanation for the slow dissolution kinetics of chalcopyrite in aqueous media. Publication US20040060395 (Hamalainen, 2004) discloses a solid-liquid-gas oxidative procedure, and relates to a process that uses a chloride environment for the leaching of concentrates by the action of cupric chloride in the presence of oxygen at high temperatures. Publication US7491372 (Faine, 2005) describes a solid-liquid-gas oxidative process that uses calcium chloride to improve the quality of the agglomerates and, consequently, the permeability of a battery. Furthermore, the process relies on promoting the generation of oxidizing agents (Fe3+ and Cu2+) through the action of oxygen and the redox reaction of copper and iron, which leads to the solubilization of sulfide minerals. The publication WO2007134343 (Muller et al., 2007) refers to a hydrometallurgical method consisting of two stages: the first non-oxidative in an acidic medium; and a second oxidative stage, which involves solid-liquid-gas interaction, for the recovery of copper from primary and secondary minerals, comprising leaching the material in an acidic chloride solution at redox potentials less than 600 mV in the presence of dissolved oxygen and cupric ions as oxidizing agents. QQhCnn / 1 7Π7 / E / YILI The publication WO2016026062 (Patiño et al., 2016) discloses a solid-liquid oxidative procedure that involves the addition of an oxidizing agent and a pretreatment of the ore in the presence of high chloride concentrations and minimal oxygen, with a redox potential greater than 700 mV for the solubilization of primary and secondary copper sulfides. The publication WO2016026062 (Álvarez, 2016) describes a chemical and bacterial procedure in a solid-liquid-gas medium, related to a leaching process of secondary and primary copper sulfides in a ferric-ferrous chloride medium, using iron-oxidizing bacteria and archaea adapted to high chloride ion concentrations. It also involves the injection of heated air to raise the temperature and enhance the mineral dissolution reactions. Document WO2016179718 (Engdahl et al., 2017) relates to a solid-liquid-gas oxidation method, carried out in a three-phase mixing agglomeration drum, and to a mineral agglomeration process performed inside said drum for the pretreatment of minerals in the presence of sodium chloride, both used primarily in hydrometallurgy. The drum and process employ a chlorine gas recirculation system and stage as part of the invention. The document US7749302 (Hyvárinen et al, 2006) refers to the HydroCopper™ technology, developed by Outokumpu, which consists of an oxidative method in a solid-liquid-gas medium, for the leaching of copper concentrates in high concentrations of cupric chloride and sodium chloride, with the help of oxygen and temperature between 85-95°C. The dissolution of chalcopyrite has been extensively studied, both by chemical and biotechnological processes, over the last 60 years (Watling HR, 2013; Li Y. et al., 2013; Liu et al., 2017). Many pathways and mechanisms of dissolution have been proposed in the presence of different salts and oxidizing agents, but these always depend on the solid-liquid, solid-liquid-gas, solid-liquid-gas-bacteria method, or pre-treatment stages with long curing and irrigation-settling periods. Furthermore, the conditions traditionally used in leaching are unsaturated solutions and depend on parameters such as redox potential, pH, and the presence of oxidizing agents. QQhcnn / ιζηζ / E / γίΛΐ reducing agents. Finally, all the leaching methods applied industrially from the 1950s to the present day have been effective for one type of mineral, such as oxidized minerals (acidic medium), secondary sulfides (sulfate and chloride medium) or primary sulfides, but a single, cross-cutting method capable of solubilizing both oxides and secondary and primary sulfides has not been implemented. The present invention differs from the state of the art, as it relates 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.Furthermore, the method described in this application is not a pretreatment or a prolonged curing and watering-resting stage, but rather a continuous solid-liquid-solid method under a supersaturation condition of non-hydrated and / or hydrated chloride salts, such as sodium chloride and / or bischofite. This condition is generated by the intentional and repeated application of drying, wetting, and rewetting stages, enhancing the chemical and physical phenomena on the ore or concentrates. This results in the crystallization, recrystallization, and release of copper, followed by its precipitation with chlorine in a non-stoichiometric decomposition of the primary or secondary sulfide. The method is carried out at a temperature of 20 to 40°C, with little to no addition of water and acid, and without the need to add oxidizing or reducing agents, or oxygen.This method, in its entirety, can be executed regardless of the presence of common impurities, such as arsenic, since the decomposition of the ore or concentrate occurs in a non-stoichiometric ratio. From an environmental perspective, the method described in this application offers the benefits of hydrometallurgy, in addition to reducing acid and water consumption, as the sulfide transformation can be carried out with only water and / or a minimal addition of acid. Furthermore, this method allows for reduced water usage in the agglomeration and / or agglomeration-curing stage, since when a hydrated chloride salt (for example, bischofite) is mixed with the ore, the water molecules of that salt are absorbed. QQhcnn / 1 ζηζ / E / γίΛΐ hydrated moisten the mineral, reducing the volume of water that must be added in the agglomeration and / or curing stages. Furthermore, the present invention would make resources available to reserves, which would allow future copper demand to be met, reactivating hydrometallurgical plants, and would change projections for the final copper product in the next decade, decreasing the use of flotation, which generates a great environmental impact due to high energy and water consumption; in addition to the generation of environmental liabilities and pollutants from the operation of smelters. BRIEF DESCRIPTION OF THE INVENTION 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 sodium chloride and / or bischofite, under supersaturation conditions. This supersaturation is achieved through the intentional and repeated application of wetting, rewetting, and drying stages, enhancing the chemical and physical phenomena on the ore or concentrates. This results in the crystallization, recrystallization, and release of copper through a non-stoichiometric decomposition of the sulfide, followed by its precipitation with chloride. The method operates at temperatures of 20 to 40°C, independent of the redox potential, with minimal water and acid consumption and without the need for oxygen addition. The method reduces acid and water consumption because the sulfide transformation can be carried out using only hydrated salts and / or minimal acid and water addition.Furthermore, the method of the present invention allows for a reduction in the use of water in the agglomeration and / or agglomeration-curing stage, because when a hydrated chloride salt is mixed with the mineral, the water molecules of said hydrated salt (for example, bischofite) moisten the mineral, reducing the volume of water that must be added in the agglomeration and / or curing stages. The present invention relates to a Solid-Liquid-Solid method in a chloride medium, governed by physical and chemical weathering processes for the solubilization of sulfide minerals, by means of supersaturation and crystallization of salts, using the addition of: a) a non-hydrated chloride salt, b) a hydrated chloride salt, c) a mixture of both salts, in a condition QQhcnn / 1 znz / E / YiAi of supersaturation, which is achieved through repeated and intentional drying stages, promotes rapid evaporation kinetics and, consequently, the solubilization of the mineral, particularly chalcopyrite. This method consists of three stages: 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, whether in the ore or concentrate, resulting in greater extraction of the desired metal. These three overlapping or sequential stages are governed by physical and chemical solid-liquid-solid phenomena, independent of redox potential and across a wide pH range. This is achieved using non-hydrated and / or hydrated chloride salts, resulting in supersaturation and crystallization of salts, and consequently, the selective and non-stoichiometric solubilization of primary and / or secondary copper sulfide. The first stage, called Wetting, involves wetting the mineral with water or water and acid, in the presence of salts under non-supersaturation, non-oxidative, and non-reductive agglomeration conditions, but always in the presence of a) an inhydrated chloride salt, b) an hydrated chloride salt, or c) a mixture of both salts. Water may or may not be added in this stage. In the case of the hydrated chloride salt, the wetting provided by the water molecules of the salt itself upon mixing with the mineral is sufficient, without the addition of water or with a minimal dose. However, when using an inhydrated chloride salt (for example, sodium chloride), the addition of a solution is necessary. The addition of liquid in this stage generates the solvation process of the salts, which allows the ions to become active, react, and migrate through the mineral's joints.All these conditions create variable pH levels and minimal oxygen presence, achieving optimal conditions for the second stage of the process. The second stage, called the Drying and Supersaturation Stage, corresponds to a drying process that promotes supersaturation, crystallization, recrystallization and precipitation of salts, both QQhcnn / 1 znz / E / YiAi both inside and outside the ore or concentrate. Drying can begin on the conveyor belt and continue in the stockpile, or it can be carried out directly in the stockpile by injecting dry or hot air, increasing the temperature, and / or promoting low relative humidity. At this stage, physical and chemical weathering is promoted by the use of chloride salts under supersaturation conditions. Furthermore, the dissolution of primary and / or secondary copper sulfide, mainly chalcopyrite, is governed by supersaturation and precipitation, which causes non-stoichiometric decomposition of the sulfide. Therefore, the process is independent of redox potential, pH, the presence of oxygen, or reducing or oxidizing agents. The drying time is variable and concludes with the start of the ore or concentrate washing stage. The third stage, called the Washing and Rewetting Stage, involves washing with an acidified or unsaturated acidified chloride solution to remove soluble chlorinated species from the target metal (e.g., copper) generated in the second stage, as well as restoring the salt concentrations and moisture content of the ore. Once washing is complete, a new Drying and Supersaturation stage begins, where the ore is dried again to promote evaporation and salt supersaturation for varying periods. The wash can be acid-chloride and / or simply seawater and is intended to remove the copper precipitated in the second stage of the process. The repeated application of the Wetting, Drying and Rewetting stages enhances the supersaturation condition and the crystallization phenomena of the salts, increasing the physical damage to the mineral or concentrate. The reactions and mechanisms involved in the steps of the method described in this application can occur in any sulfide mineral containing copper, iron, sulfur, and arsenic, even in minor quantities. It is obvious that they will affect the dissolution of any other base metal as a metallic sulfide. This applies to minerals containing nickel, zinc, cobalt, molybdenum, etc. QQhCOn / 1 7Π7 / E / YILI BRIEF DESCRIPTION OF THE FIGURES Figure 1: Graph of Copper Extraction in relation to the acid concentration in the Wetting stage using Mineral 1. Figure 2: Graph of Copper Extraction in relation to the moisture percentage in the Wetting stage using Mineral 1. Figure 3: Graph of Copper Extraction in relation to the salt concentration using Mineral 1. Figure 4: Graph of Copper Extraction in relation to the drying time in the Drying and Supersaturation 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 Extended Curing Times, using Mineral 1. Figure 7: Graph of Copper Extraction in relation to two cycles of the Solid-Liquid-Solid method versus Extended Curing 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 9: Graph of copper extraction in relation to the Solid-Liquid-Solid method versus prolonged curing times, using 1 m columns. Figure 10: Graph of irrigation ratio in relation to the Solid-Liquid-Solid method versus prolonged curing times, using 1 m columns. Figure 11: Graph of copper extraction in relation to the Solid-Liquid-Solid method versus prolonged curing times, using Mineral 2. Figure 12: Graph of copper extraction in relation to the Solid-Liquid-Solid (SLS) method versus bioleaching and chloride leaching, using Mineral 3. QQfrcnn / Lznz / E / γΐΛΐ Figure 13: Graph of water contribution by use of bischofite in the wetting stage to reach a humidity of 6% and 10%. Figure 14: Graph of copper extraction, using the solid-liquid-solid method in Mineral 4. Figure 15: Graph of copper extraction in a chalcopyrite concentrate, using the Solid-Liquid-Solid method versus chloride leaching, ferric leaching and prolonged curing time. Figure 16: SEM microscopy images of Concentrate 1, after being subjected to the Wetting and Drying stage. DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a solid-liquid-solid hydrometallurgical method in the presence of a non-hydrated chloride salt and / or a hydrated chloride salt, under supersaturation conditions. This supersaturation is achieved through the intentional and repeated application of drying and wetting stages, enhancing the chemical and physical phenomena on the ore or concentrates. This results in the crystallization, recrystallization, and release of copper through a non-stoichiometric decomposition of the sulfide, followed by precipitation of the sulfide with chloride. The method operates at temperatures of 20 to 40°C, independent of the redox potential, with minimal water and acid consumption and without the need for oxygen addition. The method reduces acid and water consumption because the sulfide transformation can be achieved using only hydrated salts and / or minimal acid and water addition.Furthermore, the method of the present invention allows for a reduction in the use of water in the agglomeration and / or agglomeration-curing stage, because when the hydrated salt is mixed with the mineral, the water molecules of the hydrated chloride salt moisten the mineral, reducing the volume of water that must be added in the agglomeration and / or curing stages. The present invention relates to a solid-liquid-solid hydrometallurgical method in a chloride medium, governed by physical and chemical weathering processes for the solubilization of sulfide minerals, through supersaturation and crystallization of salts, using the addition of: QQhCnn / 1 7Π7 / E / YILI a) an inhydrated chloride salt, b) a hydrated chloride salt, c) a mixture of both salts, in a supersaturated condition, which is achieved through repeated and intentional drying stages. This generates rapid evaporation kinetics and, consequently, supersaturation of the salts, promoting the solubilization of sulfide minerals, particularly chalcopyrite. This method consists of three stages: 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, whether in the ore or concentrate, thus achieving greater extraction of the desired metal. To carry out the Solid-Liquid-Solid hydrometallurgical method of the present invention, an inhydrated chloride salt may be selected from the group consisting of sodium chloride, potassium chloride, magnesium chloride, anhydrous ferrous chloride, anhydrous ferric chloride, and calcium chloride, and the hydrated chloride salt may be selected from the group consisting of magnesium chloride hexahydrate (bischofite), ferrous chloride heptahydrate, ferric chloride hexahydrate, among others. These three overlapping or sequential stages are governed by solid-liquid-solid physical and chemical phenomena, independent of the redox potential and over a wide pH range. This is achieved by using non-hydrated and / or hydrated chloride salts, resulting in phenomena of supersaturation and crystallization of salts and consequently the selective and non-stoichiometric solubilization of copper sulfide of primary and / or secondary origin. The process for copper minerals comprises the following stages detailed below: I. Humidification Stage This stage begins with exposing the crushed ore to an agglomeration or agglomeration and curing step in an agglomeration drum or on a conveyor belt, in order to moisten it, form agglomerates, and dissolve the sodium chloride, or bischofite, using conventional methods and procedures. This stage can be carried out in the following ways: The first difference is that the water and acid are added together. In contrast, in a classic agglomeration and curing process, the acid and water are added separately. QQhcnn / ιζηζ / E / γίΛΐ The second is that bischofite and / or sodium chloride can be added in solid form, depending on the characteristics of the mineral and the concentration of salts needed for the dissolution of the mineral, which range between 20 and 80 kg / t. The third is that this stage can be carried out only 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. The fourth is that this stage can be carried out with the addition of a mixture of salts and water or with water and acid; if only water is used, the curing stage would not be carried out. In a continuous operation, circulating or recirculating solutions will be used for the wetting and / or agglomeration-curing process, as well as for replenishing the salt concentration retained in the tailings of the treated ore. Bischofite and / or sodium chloride will be replenished by adding them in solid form at a rate 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 ore, with a final moisture content of the agglomerated ore varying between 8 and 15%, depending on the characteristics of the gangue, hygroscopicity, and particle size distribution of the ore. In this wetting stage, only bischofite and / or sodium chloride, water, or acid and water are required. The addition of cupric ions or oxygen is not necessary. Once the ore is moistened, agglomerated, and / or cured, it is transported to the stockpiling yards. After the ore is piled, the wetting stage ends, and the second stage, drying and supersaturation, begins. Humidification Stage Conditions: a) Bischofite concentrations between 20 and 80 kg / t. b) Sodium chloride concentrations between 20 and 80 kg / t. c) Mixture of both salts 20 and 80 kg / t. d) Target humidity between 6 and 15%. e) Acid concentration between 0 and 30 kg / t. QQhcnn / 1 ζηζ / E / γίΛΐ II. Drying Stage vs. Supersaturation This second stage occurs in a solid-liquid-solid (SLS) condition and consists of promoting supersaturation of the salts by drying the ore through vaporization and / or evaporation methods, including the injection of dry and / or hot air, and low temperatures or relative humidity. This stage can begin on the conveyor belt by partially reducing the surface moisture of the ore and / or directly in the stockpile, using drying methods that generate and enhance a constant drying rate while promoting supersaturation and physical phenomena in the ore, such as crystallization, precipitation, and halodesty. During this stage, no solutions are added (watering), and the stockpile is covered or sealed during each drying cycle, which lasts from 15 to 90 days, to increase temperature and evaporation, prevent salt erosion by wind, and protect the stockpiles from rain, snow, or low temperatures.The first cycle of the method ends when copper extraction decreases significantly because the vaporization or evaporation kinetics stop. This occurs because the mineral surface is covered by precipitated copper-chloride complexes and salt crystals, since in the case of sodium chloride, the crystallization process takes place primarily on the solid surface. Once the first cycle is complete, the first wash begins to remove the extracted copper. After the first wash, a second cycle of drying and supersaturation begins to achieve maximum supersaturation and copper extraction. This stage requires bischofite and / or sodium chloride, water, or acid and water. The addition of oxidizing agents such as cupric ions is not necessary, nor is the addition of oxygen through constant irrigation. This Drying and Supersaturation Stage ends with the start of continuous or intermittent irrigation of varying duration, using an unsaturated acidic solution of bischofite and / or sodium chloride. Drying Conditions vs. Supersaturation: QQhcnn / ιζηζ / E / γίΛΐ a) Sodium chloride concentrations, between 20 and 80 kg / t. b) Bischofite concentrations, between 20 and 80 kg / t. c) Drying time of 15 to 90 days, or more, depending on the reactivity of the surface of the mineral or concentrate. d) Humidity between 6 and 10%. e) Temperature between 20 to 35°C. III. Washing and Re-wetting Stage Once the drying period is complete, the third stage, Washing and Re-wetting, begins with irrigation using an unsaturated acidic chloride solution. The purpose of washing is to remove copper and soluble species, replenish salts, clean the mineral surface, and re-wet the bed. After the Washing and Re-wetting stage is finished, a second drying cycle begins. Washing and Re-wetting Conditions: a) Bischofite concentrations between 120 and 200 g / L. b) Sodium chloride concentrations between 120 and 200 g / L. c) Concentration of sodium chloride and bischofite 120 to 200 g / L d) Net irrigation rate between 5-10 L / h / m2. e) pH of the solution 0.5 to 6. The three stages, Wetting, Drying and Supersaturation and Washing, can be repeated as many times as necessary, as long as it is possible to promote wetting and chloride concentrations again, to achieve maximum solubilization of the copper contained in the primary or secondary ore. Procedure for solubilizing concentrates The procedure for concentrates comprises the following stages detailed below: I. Humidification Stage This stage begins with mixing the concentrate with bischofite and / or sodium chloride, and afterwards, water or water and acid are added, in order to achieve optimal wetting of the concentrate QQhcnn / 1 ζηζ / E / γίΛΐ and solvation. The concentration of bischofite and / or sodium chloride used ranges from 20 to 120 kg / t in a solid-liquid-solid condition. However, the concentration of fresh and / or circulating sulfuric acid will be that necessary to achieve a pH between 0.5 and 3. The final moisture content varies between 8 and 20%, depending on the hygroscopic characteristics of the salt and the concentrate. At this stage, only bischofite and / or sodium chloride, water, or acid and water to moisten the concentrate are required. Oxidizing agents, temperature, and oxygen are not necessary. Furthermore, for concentrates with the required moisture content for the process, only the sodium chloride and / or bischofite should be added in solid form. Once the concentrate is mixed with salts and has been given an optimum moisture content, which corresponds to the maximum moisture that the concentrate can withstand before forming a paste, it is transported to concentrate accumulation yards, to begin the second stage of Drying and Supersaturation. Wetting Conditions (solid-liquid-solid): a) Concentrations of sodium chloride and / or bischofite between 20 and 120 kg / t. b) Humidity between 9 and 20%. c) pH between 0.5 and 7. d) Particle size 100% below 150 microns. II. Drying and Supersaturation Stage This second stage of Drying and Supersaturation consists of drying the moistened concentrate for a variable amount of time to generate chloride supersaturation and selectively transform the concentrate into soluble chlorinated copper species, precipitating these soluble species. Furthermore, as the drying time increases, the moisture content decreases, and the supersaturation condition intensifies due to water vaporization and / or evaporation. Additionally, the prolonged drying period promotes salt crystallization and the phenomenon of cryptoefflorescence on the concentrate particles. QQhCnn / 1 7Π7 / E / YILI 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, which allows for a constant evaporation rate in the piles or heaps of concentrates, to promote supersaturation and extraction of copper. This stage requires only bischofite and / or sodium chloride, water, or acid and water. The addition of oxidizing agents such as cupric ions, or oxygen, is not required. This Drying and Supersaturation Stage ends when the concentrate is transferred to the washing ponds to remove the extracted copper. Drying Conditions vs. Supersaturation (solid-liquid-solid): a) Bischofite and sodium chloride in supersaturation. b) Drying time of 15 to 90 days or more, depending on the reactivity of the surface of the concentrate. c) Humidity between 8 and 15%. d) Temperature 25 to 40°C. e) Acidic pH. III. Washing and Re-wetting Stage The concentrate that has undergone the drying and supersaturation stage is transported to washing tanks, where it is washed with an acidified solution or a chloride and acid solution to obtain soluble copper. The concentrate is then filtered and dried to begin a new cycle of the process 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 go directly to the newer electrowinning plants, which can produce a cathode without a prior solvent extraction stage and directly process copper-rich solutions. Chlorinated Washing Conditions: a) Concentrations of sodium chloride and / or bischofite between 0 and 200 g / L. QQhcnn / ιζηζ / E / γίΛΐ b) pH between 0.5 and 3. c) Washing time between 2 and 45 minutes. The stages of 1) Wetting, 2) Drying and Supersaturation and 3) Washing can be repeated as many times as necessary, as long as wetting is promoted again in the presence of chloride, to achieve maximum solubilization of the copper contained in the concentrate. MODALITIES OF THE INVENTION The present invention relates specifically to a Solid-Liquid-Solid hydrometallurgical method for the solubilization of metals from primary and / or secondary sulfide minerals and / or mineral concentrates containing them, comprising the following sequential and / or overlapping steps: I. Wetting, where the mineral or concentrate is moistened by the addition of water or water-acid and hydrated and / or non-hydrated chloride salts; II. Drying and Supersaturation, where the moistened mineral is dried by vaporization and / or evaporation, which drying can be carried out both in the pile, as well as on the conveyor belt, generating conditions of supersaturation, crystallization and recrystallization of the salts, favoring chemical and physical weathering on the mineral or concentrate, of the acid concentration; and III. Washing and Re-wetting, where an acidified solution with or without chloride is added to remove the target metal species precipitated in the second stage of the process, also allowing the mineral or concentrate to be re-wetted in order to restore the optimum chloride and moisture concentration to the bed. Where, when the method is in continuous regime, in stage I the contact of the mineral or concentrate is carried out with recirculating solutions from the same process that may contain chloride, iron and copper ions, in a non-saturated environment, and where the three stages are carried out independently of the REDOX potential of the medium. QQhcnn / 1 ζηζ / E / γΐΛ In a preferred embodiment, the hydrated chloride salt is selected from the group consisting of magnesium chloride hexahydrate (bischofite), ferrous chloride heptahydrate, ferric chloride hexahydrate, among others. In another preferred embodiment, 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. In one embodiment of the invention, in step I the non-hydrated and / or hydrated chloride salt is sodium chloride and / or bischofite added in solid or solution, preferably in an amount of sodium chloride and / or bischofite added ranging from 20 to 80 kg per ton of material, preferably between 30 and 60 kg / t. In another embodiment of the invention, steps I and II can be performed only with the addition of bischofite and / or bischofite and water and / or process solutions. Even in another modality, in stages I, II and III, the addition of chloride salts may include a mixture of hydrated and / or non-hydrated salts. In another preferred embodiment of the method, the addition of water and acid in stage I is carried out separately or together, preferably together. The addition of sulfuric acid ranges from 0 to 30 kg per ton of material, preferably between 5 and 15 kg / t. In a preferred embodiment of the invention in stage I the final moisture content of the agglomerated mineral can be between 6 and 20%, preferably between 8 and 10%. In another embodiment of the invention, step I can be performed on an agglomerating drum or directly on the conveyor belt. In a preferred modality, in stage II the drying of the ore is carried out with the pile covered and protected to generate the temperature increase. In an even more preferred embodiment of the invention, in stage II the condition of supersaturation of species and salts is achieved by intentional and repetitive drying cycles and / or by drying the mineral by air injection and / or temperature increase and / or by periods without QQhcnn / ιζηζ / E / γίΛΐ addition of solutions and, where in stage II the pile may be covered or capped during the drying cycles. In another modality of the method in stage I, the concentrations of salts to be replenished in the continuous regime system range between 5 and 20 kg / t. In a preferred modality, stages I, II and III of the method can be repeated one or more successive times until the maximum extraction of the desired metal is achieved. In another embodiment of the invention, after stage I, the sulfide minerals and / or mineral concentrates are subjected to drying cycles ranging from 15 to 90 days, where the supersaturation condition is generated and the crystallization of salts and precipitation of soluble chlorinated metal species occurs. In a preferred modality of the method, the sulfide mineral, which can be of primary origin, mainly chalcopyrite, is subjected to 2 or 3 drying cycles ranging from 30 to 90 days, preferably 60-day cycles. In another preferred method after stage I, the sulfide mineral, which can be of secondary origin, mainly chalcocite and covellite, is subjected to 2 or 3 drying cycles ranging from 15 to 45 days, preferably 15-day cycles. In one version of the method, in stage III the ore is washed by continuous or intermittent irrigation with a solution containing acidified water, or acid and chloride. In a preferred embodiment of the invention, the metals to be solubilized are selected from the group that includes copper, zinc, nickel, molybdenum, cobalt, lead, among others. In another embodiment of the invention, in stage III, washing is carried out by means of a limited or prolonged irrigation, promoting the presence of Cu (I) or Cu (II), respectively. In one version of the method, the solubilization of the target metal can be carried out in the same way from sulfide minerals with arsenical contents and / or concentrates of arsenical sulfide minerals that contain it. QQhcnn / 1 ζηζ / E / γίΛΐ In another preferred embodiment, stages I, II and III can be applied to copper ores and / or concentrates, preferably chalcopyrite, bornite, tennantite, enargite, chalcocite and covellite. In a preferred embodiment of the invention, step II can be applied in a drying chamber or greenhouse, which allows for the generation of a constant evaporation kinetics of the liquid. In another preferred embodiment of the invention, chloride ions can be incorporated into the method in the form of bischofite, 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. In another preferred embodiment of the invention, the metal to be solubilized is copper and the sulfide mineral is a secondary copper sulfide mineral. In a preferred embodiment of the invention, step II is carried out in a solid-liquid-solid condition. In a preferred embodiment of the method, stages I of wetting and II of drying and supersaturation can be carried out at pH between 0.5 and 5. In another embodiment of the invention, stages I of wetting, II of drying and supersaturation, and III of washing can be performed independently of the potential, under 700 mV or above 700 mV (Eh). In a preferred embodiment of the invention, washing stage III can be performed with a reused solution containing chloride and iron ions. In an even more preferred modality, stages I and II can use chloride salts, which can come from seawater, desalination plant brines, halite, bischofite, and commercial sodium chloride. In another embodiment of the invention, steps I, II and III can be performed at room temperature, preferably between 20 and 40°C. In an even more preferred embodiment of the invention, the solution obtained from step II can follow the traditional steps of solvent extraction and electrowinning or go directly to electrowinning. QQhcnn / ιζηζ / E / γίΛΐ APPLICATION EXAMPLES Example 1: Mineralogy of three copper minerals Table 1 shows the quantitative mineralogical analysis obtained for four copper sulfide ore heads, designated as Mineral 1, 2, 3, and 4. Optical microscopy and modal analysis were used for the analysis, supported by sequential copper chemical analysis. The point-counting statistical method was used to determine the mineralogical composition. The mineralogical analysis for total copper indicated the presence of both low- and high-grade ores; however, the analysis by copper species showed that for Minerals 1, 2, 3, and 4, the percentage of chalcopyrite was 99.8%, 81.7%, 45%, and 11.7%, respectively. Table 1: Quantitative mineralogical analysis obtained for four copper sulfide mineral head samples, named Mineral 1, 2, 3 and 4 QQhcnn / ιζηζ / E / γίΛΐ Mineral Species 1% Mineral 2% Mineral 3% Mineral 4% Total Copper Grade 0.24 0.68 0.36 0.67 Chalcopyrite 99.8 81.7 45 11.7 Bornite 0.13 12.3 - 12.0 Tennantite 0.08 1 - 0.1 Chalcocite - 3.9 21 76.2 Covellite - 1.1 14 - Atacamite - - 4 - Malachite - - 16 - Example 2: Copper extraction in relation to acid concentration in the Wetting stage using Mineral 1. The results in Figure 1 were obtained from column tests, using Mineral 1, which has a total copper grade of 0.24% and a copper species percentage of 99.8% chalcopyrite (see Table 1). Mineral 1 underwent traditional crushing until a particle size of 100% below 2 inches was achieved. Subsequently, six batches of this mineral were prepared. All batches were then subjected to a wetting stage, where agglomeration and curing occurred with the addition of water, and water and acid together. The addition of bischofite and sodium chloride in solid form directly onto the mineral was carried out at the following concentrations and conditions: a) Addition of 60 kg / t sodium chloride. b) Addition of 60 kg / t bischofite. c) Addition of 0.15 and 30 kg / t of sulfuric acid. d) Humidity of 10%. e) Temperature of 30°C. Once the wetting stage was completed, the thermal drying stage began directly in the column for a period of 45 days. After the stipulated time for the second stage was completed, the third stage, washing, began with an irrigation rate of 5 L / h / m² for 12 hours, using a sodium chloride solution of 180 g / L at pH 1. The results are shown in Figure 1, which indicates that increasing the acid concentration during the Wetting stage does not significantly affect copper extraction during the Drying and Supersaturation stages. Furthermore, the test conducted with only water confirms that the method is independent of the acid concentration and, therefore, of the curing process. This differs from the prior art, where the method described in this application depends on the salt concentration and evaporation kinetics. Example 3: Copper extraction in relation to the percentage of moisture in the Wetting stage using Mineral 1 The results in Figure 2 were obtained from column tests using Mineral 1. The minerals were subjected to a conventional crushing process until a particle size of 100% below W inch was achieved. Subsequently, four batches of this mineral were prepared. Each batch was then agglomerated and cured with the addition of water and acid together, imposing a different moisture content on each test. The addition of bischofite and sodium chloride in solid form directly onto the mineral was carried out under the following conditions: a) Humidity percentages 6 and 10%. QQhcnn / ιζηζ / E / γίΛΐ b) Addition of 15 kg / t of sulfuric acid. c) Addition of 60 kg / t bischofite. d) Addition of 60 kg / t sodium chloride. e) Drying and Supersaturation Time was 60 days. f) Temperature of 30°C. Once the stipulated time of the second stage was completed, the third stage of Washing was initiated with an irrigation rate of 5 L / h / m2 for 24 hours, using an artificial refining solution containing 180 g / L sodium chloride, 5 g / L ferric chloride, 2 g / L ferrous chloride and 10 g / L acid. The results are shown in Figure 2, where it can be observed that the moisture percentage applied during the Wetting stage for the sodium chloride tests has a significant effect on the performance of the Drying and Supersaturation stage, achieving greater copper extraction with a moisture content of 10%. However, for the bischofite tests, the difference was smaller, probably due to the deliquescence of this salt, which does not occur with sodium chloride. Example 4: Copper extraction in relation to salt concentration using Mineral 1. The results in Figure 3 were obtained in column tests, using Mineral 1. The ore was subjected to a traditional crushing process until a particle size of 100% less than one inch was achieved. Subsequently, twelve batches of this ore were prepared, and then the ore batches were subjected to the wetting stage, with the addition of water and acid together. The addition of bischofite and sodium chloride in solid form directly onto the ore was carried out at the following concentrations and conditions: a) 0, 20, 40, 60, 80 kg / t of NaCl. b) 0, 20, 40, 60, 80 kg / t of bischofite. c) Addition of acid at 15 kg / t. d) Humidity of 10%. QQhCnn / 1 7Π7 / E / YILI e) Temperature of 25-30°C. Once the Wetting stage was completed, the Drying and Supersaturation stage began, lasting for 45 days. During this time, there was no irrigation, and the columns were covered to maintain a temperature of 25-30°C. After the second stage was completed, the third stage, Washing, began at an irrigation rate of 7 L / h / m2 for 12 hours, using an artificial refining solution containing 180 g / L sodium chloride, 5 g / L ferric chloride, 2 g / L ferrous chloride, and 10 g / L acid. The results can be seen in Figure 3, where it is observed that an increase in salt concentration leads to greater copper extraction. However, this phenomenon or trend for both salts is only maintained up to 60 kg / t, possibly because the excess salts quickly cause supersaturation of the mineral surface, resulting in minimal evaporation. In the case of bischofite, the results show that only 40 kg / t are required to achieve high copper extraction; however, for sodium chloride, 60 kg / t are needed. It appears that the use of hydrated salts performs better than non-hydrated salts in the Solid-Liquid-Solid method. Example 5: Copper extraction in relation to drying time in the Drying and Supersaturation stage, using Mineral 1. The results in Figure 4 were obtained in column tests, using Mineral 1. The minerals underwent a traditional crushing process until a particle size of 100% less than 1 / 2 inch was achieved. Subsequently, twelve batches of Mineral 1 were prepared. All batches of mineral were then subjected to the Wetting stage, where agglomeration and curing occurred with the addition of water and acid. The addition of bischofite and sodium chloride in solid form directly onto the mineral was carried out at the following concentrations and conditions: a) Addition of 60 kg / t of NaCl. b) Addition of 60 kg / t of bischofite. c) Addition of acid at 15 kg / t. QQhcnn / 1 znz / E / YiAi d) Humidity of 10%. e) Temperature of 25-30°C. Once the Wetting stage was completed, the Drying and Supersaturation stage began for different periods of time (5, 15, 30, 45, 60, and 90 days). After the stipulated time period of the second stage was completed, the third stage, Washing, began with an irrigation rate of 5 L / h / m² for 24 hours using an artificial refining solution containing 180 g / L sodium chloride, 5 g / L ferric chloride, 2 g / L ferrous chloride, and 10 g / L acid. The results can be seen in Figure 4, where it can be observed that there is an increase in copper extraction as the Drying and Supersaturation time increases, which confirms that the Solid-Liquid-Solid method is governed by evaporation kinetics, which allows reaching supersaturation and a high ionic charge, which ultimately allows the extraction of copper. Example 6: Copper extraction in relation to the simulation of a continuous regime, using Mineral 1. The results in Figure 5 were obtained in column tests, using Mineral 1. The minerals underwent a traditional crushing process until a particle size of 100% under 1 / 2 inch was achieved. Subsequently, six batches of Mineral 1 were prepared. All batches of mineral were then subjected to the Wetting stage, where a continuous regime was simulated, carrying out the agglomeration and curing process with the addition of water and acid together; in addition to the addition of an artificial refining solution in which the chloride was in solution. The addition of bischofite and sodium chloride in solid form directly onto the mineral was carried out with the following concentrations and conditions: a) Addition of 5, 10 and 15 kg / t of NaCl. b) Addition of 5, 10 and 15 kg / t of bischofite. c) Artificial refining: 80-120 g / L chloride, 5 g / L ferric, 2 g / L ferrous and 10 g / L acid. d) Humidity of 10%. QQhcnn / ιζηζ / E / γίΛΐ e) Temperature of 25-30°C. f) Drying time 45 days. Once the second stage was completed, the third stage of washing was started at an irrigation rate of 7 L / h / m2 for 12 hours, using an artificial refining solution containing 180 g / L sodium chloride, 5 g / L ferric chloride, 2 g / L ferrous chloride and 10 g / L acid. The results are shown in Figure 5, where it can be observed that adding the salts in solution and in solid form is effective, achieving extractions similar to those obtained when the salts are added as a solid to the ore. The results demonstrate that salt replenishment in a continuous operation can be achieved by adding 5, 10, or 15 kg / t of salts. This test indicates that the Solid-Liquid-Solid method is feasible to apply in a mining operation, since the amount of salt to be replenished in the circuit is technically and economically viable. 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 in Figure 6 were obtained in column tests, using Mineral 1. The minerals underwent a traditional crushing process until a particle size of 100% less than 1 / 2 inch was achieved. Subsequently, six batches of this mineral were prepared. These batches were then subjected to a wetting stage, followed by agglomeration and curing with the addition of water and acid together for the SLS method and separately for the extended curing test. The four extended curing tests were loads, 2 for a 60-day curing period and 2 for a 120-day period, as shown in Example 8. The addition of bischofite and sodium chloride in solid form directly onto the ore was carried out with the following concentrations and conditions: Solid-Liquid-Solid Method (cycle No. 1) a) Addition of 60 kg / t of NaCl. b) Addition of 40 kg / t of bischofite. QQhCnn / 1 7Π7 / E / YILI c) Humidity of 10%. d) Acid 15 kg / t. e) Thermal drying 25-30°C. f) Drying time 60 days. Prolonged curing time a) Addition of 60 kg / t of NaCl. b) Addition of 60 kg / t of bischofite. c) Humidity of 10%. d) Acid 40 kg / t. e) Room temperature without drying. f) Curing time 60 days. Once the second stage and the extended curing time were completed, the third stage of washing was initiated for the tests that had 60 days of testing, at an irrigation rate of 7 L / h / m2 for 12 hours, using an artificial refining solution containing 180 g / L sodium chloride, 5 g / L ferric, 2 g / L ferrous and 10 g / L acid. The results can be seen in Figure 6, which shows that the SLS method is capable of achieving a significantly higher extraction rate than a prolonged curing process. Even when higher acid concentrations were used than those employed in the method, and the same salt concentrations as the solid-liquid-solid method were used, the extraction rate was still more than double that of the prolonged curing process. Example 8: Copper extraction in relation to two cycles of the Solid-Liquid method versus Extended Curing Times of 120 days, using Mineral 1. The results in Figure 7 for the SLS method tests were obtained from the continuation of the tests in Example 7. For this purpose, a second cycle of Drying and Supersaturation was performed for a QQhcnn / ιζηζ / E / γίΛΐ 60-day period. For the case of prolonged curing tests, the tests that had a curing period of 120 days were continued. Once the second stage and the extended curing time were completed, the third stage of washing and watering was started for all tests, at a watering rate of 10 L / h / m2 for 12 hours, using an artificial refining solution containing 180 g / L sodium chloride, 5 g / L ferric chloride, 2 g / L ferrous chloride and 10 g / L acid. The results can be seen in Figure 7, where the SLS method again allowed for a significantly higher extraction rate than that achieved with prolonged curing periods. During two SLS cycles, extraction rates of 72.1% and 74.7% were achieved for bischofite and sodium chloride, respectively. However, for tests with prolonged resting periods, the extraction rates were only 37.9% and 36.9%, respectively. Example 9: Copper extraction in relation to a first cycle of the Solid-Liquid-Solid method, using a mixture of salts and Mineral 1. The results in Figure 8 were obtained in column tests, using Mineral 1. The minerals underwent a traditional crushing process until a particle size of 100% less than 1 / 2 inch was achieved. Subsequently, two batches of this mineral were prepared. All batches were then subjected to a wetting stage, where agglomeration and curing occurred with the addition of water and acid. The addition of bischofite and sodium chloride in solid form directly onto the mineral was carried out at the following concentrations and conditions: a) Addition of 40 kg / t of salts (20 kg / t of NaCl and 20 kg / t of bischofite). b) Addition of 60 kg / t of salts (30 kg / t of NaCl and 30 kg / t of bischofite). c) Addition of acid at 15 kg / t. d) Humidity of 10%. e) Drying Temperature 25-30°C. f) 45 days of drying. QQhcnn / 1 ζηζ / E / γίΛΐ Once the drying time of the second stage was completed, the third stage of Washing was started with an irrigation rate of 5 L / h / m2 for 24 hours with an artificial refining solution containing 180 g / L sodium chloride, 5 g / L ferric, 2 g / L ferrous and 10 g / L acid. The results can be seen in Figure 8, which shows that, during 45 days of drying, extractions similar to those obtained using the salts separately were achieved. This indicates that a mixture of the salts can be used for both 40 and 60 kg / t of salts. Example 10: Copper extraction in relation to the Solid-Liquid-Solid method versus prolonged curing times, using 1 m columns. The results in Figure 9 were obtained in tests on 1 m columns, using Mineral 1 (see Table 1). The ore was subjected to a traditional crushing stage until a particle size of 100% less than 1 / 2 inch was achieved. Subsequently, four 30 kg batches of this ore were prepared. All batches were then subjected to the Wetting stage, where agglomeration and curing were carried out with the addition of water and acid together for the SLS method and separately for the extended curing test. The addition of bischofite and sodium chloride in solid form directly onto the ore was carried out with the following concentrations and conditions: Solid-Liquid-Solid Method (cycle No. 1) a) Addition of 60 kg / t of NaCl. b) Addition of 40 kg / t of bischofite. c) Humidity of 10%. d) Acid 15 kg / t. e) Thermal drying 25-30°C. f) Drying time, two 60-day cycles. Prolonged curing time a) Addition of 60 kg / t of NaCl. b) Addition of 60 kg / t of bischofite. QQhcnn / 1 ζηζ / E / γίΛΐ c) Humidity of 10%. d) Acid 40 kg / t. e) Ambient temperature. f) Curing time 60 days and watering for 60 days. Once the first drying cycle was completed, the washing stage began with an irrigation rate of 5 L / h / m² for 24 hours using an artificial refining solution containing 200 g / L sodium chloride, 5 g / L ferric chloride, 2 g / L ferrous chloride, and 10 g / L acid, and 240 g / L bischofite, 5 g / L ferric chloride, 2 g / L ferrous chloride, and 10 g / L acid. After the washing stage was finished, a second drying cycle of 60 days began. For the extended curing tests, after 60 days of curing, irrigation began at a rate of 5 L / h / m² for 24 hours with an artificial refining solution of 150 g / L sodium chloride, 5 g / L ferric chloride, 2 g / L ferrous chloride, and 10 g / L acid. Following the initial irrigation, watering-rest periods were implemented every 5 days at a rate of 5 L / h / m² for 12 hours, until the 120-day test period was completed. The results are shown in Figure 9, which confirms that the SLS method is more effective for extraction from ore containing copper primarily in the form of chalcopyrite, even though the SLS tests were performed with a lower concentration of bischofite and acid than the extended curing tests. The SLS method achieved an extraction rate of over 70% for both salts; however, for the extended curing tests, it was less than 33%. This example also includes the redox potential and chemical analysis results of the solutions obtained from the first wetting and drying cycle, as well as the effluent from the extended curing test (see Table 2). QQhCnn / 1 7Π7 / E / YILI Table 2. Chemical analysis of the solutions from the first wash and irrigation CONDITIONS CuT g / L FeT g / L Fe2+ g / i Fe3+ g / L REDOX POTENTIAL Eh SLS METHOD (NaCI) 19.1 3.6 ND 3.6 655 SLS METHOD (BISCHOPHITE) 22.9 2.3 0.5 1.8 724.9 PROLONGED CURING (NaCI) 10.1 9.6 6.1 3.5 641 PROLONGED CURING (BISCHOPHITE) 10.9 9.1 5.2 3.9 711.8 QQhcnn / ιζηζ / E / γίΛΐ As can be seen in Table 2, the SLS method results in a higher concentration of copper relative to total iron, with a copper-to-iron ratio of approximately 5:1 for sodium chloride and almost 10:1 for bischofite. Conversely, in prolonged curing, the copper-to-iron ratio is approximately 1:1 for both salts. It can also be observed that the redox potentials are similar, with no significant differences indicating that the potential difference might affect copper solubilization. Example 11: Irrigation Ratio in relation to the Solid-Liquid-Solid method versus Prolonged Curing Times, using 1 m columns. The results in Figure 10 for the SLS method tests were obtained from the tests in Example 10. To this end, a graph was created to identify the irrigation ratio for both processes. As can be seen in Figure 10, the Solid-Liquid-Solid method exhibits a lower irrigation ratio compared to the tests with prolonged curing and irrigation-rest. Furthermore, it should be noted that in both cases, the tests with bischofite have a lower irrigation ratio due to its greater deliquescence; therefore, the amount of solution used in each washing stage was less. Example 12: Copper extraction in relation to the Solid-Liquid-Solid method versus Prolonged Curing Times, using Mineral 2. The results in Figure 11 were obtained in tests on 1 m columns, using Mineral 2, which has a total copper grade of 0.68% and a copper species percentage of 81.7% in the form of chalcopyrite (see Table 1). The minerals were subjected to a traditional crushing process until a particle size of 100% less than 1 / 2 inch was achieved. Subsequently, four 30 kg batches of this mineral were prepared. All batches were then subjected to the Wetting stage, where agglomeration and curing were carried out with the addition of water and acid together for the SLS method and separately for the extended curing test. The addition of bischofite and sodium chloride in solid form directly onto the mineral was carried out with the following concentrations and conditions: Solid-Liquid-Solid Method (cycle No. 1) a) Addition of 60 kg / t of NaCl. b) Addition of 40 kg / t of bischofite. c) Humidity of 10%. d) Acid 15 kg / t. e) Air injection drying. f) Drying time, two 60-day cycles. Prolonged curing time a) Addition of 60 kg / t of NaCl. b) Addition of 40 kg / t of bischofite. c) Humidity of 10%. d) Acid 40 kg / t. e) Ambient temperature. f) Curing time 60 days and watering for 60 days. Once the first drying cycle was completed, the washing stage began with an irrigation rate of 5 L / h / m² for 24 hours using an artificial refining solution containing 200 g / L sodium chloride, 5 g / L ferric chloride, 2 g / L ferrous chloride, and 10 g / L acid, and 240 g / L bischofite, 5 g / L ferric chloride, 2 g / L ferrous chloride, and 10 g / L acid. After the washing stage ended, a second drying cycle began for another 60 days. QQhcnn / 1 znz / E / YiAi For the extended curing tests, once 60 days of curing were reached, irrigation began at a rate of 5 L / h / m² for 24 hours with an artificial refining solution of 150 g / L sodium chloride, 5 g / L ferric chloride, 2 g / L ferrous chloride, and 10 g / L acid. After the first irrigation, watering followed by rest periods were carried out every 5 days at a rate of 5 L / h / m² for 12 hours, until 120 days of testing were completed. The results are shown in Figure 11, which confirms that the SLS method is more effective at extracting copper from the primary sulfide than the prolonged curing followed by irrigation and resting. Extraction rates for both methods were above 80% and below 44%, respectively. It can also be concluded that the effect of the prolonged curing process is enhanced by the mineralogy, as Mineral 2 contains only 70% chalcopyrite, with the remaining 30% consisting of less refractory and soluble mineral species. This is because approximately 30% of the copper was extracted during the first irrigation. Example 13: Copper extraction in relation to the solid-liquid-solid (SLS) method versus Bioleaching and Chloride Leaching, using Mineral 3 The results in Figure 12 were obtained in tests on 1 m columns, using Mineral 3, which has a total copper grade of 0.36% and a copper species percentage of 45% chalcopyrite (see Table 1). The minerals were subjected to a traditional crushing process until a particle size of 100% less than 1 / 2 inch was achieved. Subsequently, three batches of this mineral were prepared. The mineral batches were then subjected to the wetting stage, followed by agglomeration and curing with the addition of water and acid together for the SLS method and separately for the chloride leaching and bioleaching tests. The addition of sodium chloride in solid form directly onto the mineral was carried out with the following concentrations and conditions: Solid-Liquid-Solid Method (cycle No. 1) a) Addition of 60 kg / t of NaCl. b) Humidity of 10%. QQhcnn / ιζηζ / E / γίΛΐ c) Acid 15 kg / t. d) Thermal drying 25-30°C. e) Drying time 60 days. Chloride leaching and bioleaching tests were performed in 1000 lm columns by a metallurgical laboratory specializing in this type of testing. Classical secondary sulfide leaching methods were used on Mineral 3. Chloride leaching was carried out with a concentration of 150 g / L of sodium chloride, 30 kg / t of acid, and 10% moisture. The process lasted 90 days, with irrigation and settling periods. For the bioleaching test, a bacterial consortium composed of iron and sulfur oxidizing microorganisms was used, with 10% moisture and 50 kg / t of acid. The process lasted 90 days, using irrigation-resting stages. The results are shown in Figure 12, where it can be seen that, when using a mixed mineral of primary and secondary sulfides, the SLS method is more efficient in copper extraction than traditional methods, since it allows the extraction of copper from both chalcopyrite and soluble sulfides such as chalcocite, covellite, and malachite. Example 14: Water input by using Bischofite in the wetting stage to achieve a humidity of 6% and 10%. The results in Figure 13 were obtained from column tests described in Example 3, using Mineral 1, which has a total copper grade of 0.24% and a copper species percentage of 99.8% chalcopyrite (see Table 1). To graph the data obtained, the amount of water provided by the mass of bischofite used to moisten the mineral and reach a humidity of 6 and 10% was determined. The results can be seen in Figures 13A and 13B, where it was determined that at a humidity of 6%, bischofite provides 47% of the water required for wetting. However, to reach a humidity of 10%, the water contribution from bischofite is 27%. QQhCnn / 1 7Π7 / E / YILI Example 15: Copper extraction using the solid-liquid-solid method in Mineral 4. The results in Figure 14 were obtained from column tests, using Mineral 4, which has a total copper grade of 0.67% and a copper species percentage of 76.24% chalcocite and 11.7% chalcopyrite (see Table 1). The minerals underwent a traditional crushing stage until a particle size of 100% less than 1 / 2 inch was achieved. Subsequently, two batches of this mineral were prepared, and then the mineral batches were subjected to the SLS method, beginning with the Wetting stage, where agglomeration was achieved by the addition of water and acid together, according to the conditions described below: Solid-Liquid-Solid Method (cycle No. 1) a) Addition of 40 kg / t of NaCl. b) Humidity of 10%. c) Acid 15 kg / t. d) Thermal drying 25-30°C. e) Drying time 15 days. Once the first drying cycle was completed, the washing and re-wetting stage began with an irrigation rate of 5 L / h / m² for 24 hours using an artificial refining solution containing 200 g / L sodium chloride, 5 g / L ferric chloride, 2 g / L ferrous chloride, and 10 g / L acid. A second drying cycle then began for another 15 days. After the second drying cycle, a second wash was performed with an acidified solution at pH 1 at an irrigation rate of 5 L / h / m² for 24 hours. Finally, the test was concluded. The extraction results can be seen in Figure 14, which shows that under the first cycle of the Solid-Liquid-Solid method, Mineral 4 is solubilized to a high degree in just 15 days QQhcnn / 1 znz / E / YiAi of drying. However, during the second drying cycle, the remaining copper was extracted, achieving an extraction rate of over 80%. High copper extraction is expected during testing on an ore containing more than 70% total copper in the form of chalcocite. However, under the solid-liquid method according to the invention, the maximum copper concentration is achieved in just two 15-day cycles. Example 16: Concentrate Mineralogy 1. The results in Table 3 were obtained through quantitative mineralogical analysis of a representative sample of primary copper concentrates, called Conc. 1. Optical microscopy was used for the analysis, supported by sequential copper chemical analysis. The statistical method of point counting was used to determine the mineralogical composition. The mineralogical analysis indicated that the total copper grade for Conc. 1 is 25.57%; however, the analysis by copper species showed that Conc. 1 mainly contains 80.03% chalcopyrite and 12.14% tennantite. Table 3: Quantitative mineralogical analysis of a representative sample of primary copper concentrates QQhcnn / ιζηζ / E / γίΛΐ Species Concentrate 1% Total copper grade 25.57 Chalcopyrite 80.03 Bomite 5.66 Tennantite 12.14 Enargite 0.53 Chalcocite 0.11 Covellite 1.53 Example 17: Copper extraction from a chalcopyrite concentrate, using the Solid-Liquid-Solid method versus chloride leaching. Ferric and prolonged curing time. The results in Figure 15 were obtained using a chalcopyrite-rich concentrate with a particle size distribution of 100% between 75 and 106 microns and a total copper content of 25.57% (see Table 3). Subsequently, the masses of concentrates were weighed for testing under three types of reaction, as described below: A. Solid-liquid-solid reaction (water vs. acid) For the tests, 200 grams of the concentrate were weighed for each salt. Subsequently, the sample was subjected to the Humidification stage, which consisted of the addition in solid form of 100 kg / t of NaCl, 100 kg / t of bischofite and 100 kg / t of FeCbx 6H2O to the concentrate. Then, a solution composed of water and acid with 2 g / L of ferrous and 3 g / L of ferric was added, reaching a final moisture content of 12%. Once the concentrate was moistened, the second stage of the process began, in which the concentrates were stored in a drying chamber at 30°C for 25 days. Subsequently, the third stage of the process began, in which the concentrate was transferred to the washing tanks and washed with a pH 1 solution for 30 minutes. After washing, the concentrate was filtered and then dried to begin a second moistening and drying cycle. B. Solid-Liquid-Solid Reaction (water) For the tests, 200 grams of the concentrate were weighed for each salt. Subsequently, the sample underwent a wetting stage, in which 100 kg / t of NaCl, 100 kg / t of bischofite, and 100 kg / t of FeCbx 6H2O were added in solid form to the concentrate. Then, for the sodium chloride test, a solution composed of water with 2 g / L of ferrous and 3 g / L of ferric was added until a final moisture content of 13% was reached. However, for the bischofite and FeCbx 6H2O tests, only the salt was added. Once the concentrate was humidified, the second stage of the process began, in which the concentrates were stored in a QQhcnn / 1 ζηζ / E / νίΛΐ drying chamber at 30°C for 25 days. After the drying and supersaturation period, the third stage of the process began, in which the concentrate was transferred to the washing tanks, where it was washed with a pH 1 solution for 30 minutes. Once the washing was completed, the concentrate was filtered and then dried to begin a second wetting and drying cycle. C. Solid-Liquid-Solid Reaction (Ferric Sulfate) For these tests, 200 grams of the concentrate were weighed. The sample was then subjected to the Wetting stage, which consisted of adding 100 kg / t of ferric sulfate to the concentrate. A solution of water and acid containing 2 g / L of ferrous and 3 g / L of ferric was then added until a final moisture content of 12% was reached. Once the concentrate was humidified, the second stage of the process began, in which the concentrates were stored in a drying chamber at 30°C for 25 days. After the drying and supersaturation period, the third stage of the process began, in which the concentrate was transferred to the washing tanks and washed with a pH 1 solution for 30 minutes. After washing, the concentrate was filtered and then dried to begin a second Wetting and Drying cycle. D. Solid-liquid reaction Chloride leaching For the tests, 50 grams of each concentrate were weighed. The concentrate was then transferred to a 1000 mL Erlenmeyer flask, and 500 mL of acidified solution (pH 1, with a sodium chloride concentration of 200 g / L) was added. Each test was performed in duplicate, and the mixture was stirred at 120 rpm for 45 days at room temperature. During this period, the pH was not adjusted, and the solution was not replenished, as it was lost through evaporation. Once the test time was completed, the solution was filtered and the solid was separated from the liquid, in order to perform the corresponding chemical analyses and determine the copper extraction, as shown in Figure 15. QQhCnn / 1 7Π7 / E / YILI E. Prolonged curing in the presence of salts For the tests, 200 grams of the concentrate were weighed for each salt. Subsequently, the sample was subjected to the curing stage, which consisted of the addition of a solution at pH 0.5 containing 150 g / L of sodium chloride, 2 g / L of ferrous and 3 g / L of ferric. The same condition was used for the test with bischofite, reaching a final moisture content of 13%. Once the concentrate was cured, it was left to rest for 50 days. After the curing period, the concentrate was washed using a pH 1 solution for 30 minutes. The resulting solution was then analyzed to determine the amount of copper obtained. The extraction results can be seen in Figure 15, where it can be observed that under the Solid-Liquid-Solid conditions, a high extraction rate was achieved for both salts in as little as 25 days; in contrast, the prolonged curing condition did not exceed 30% extraction in days. However, for the chloride leaching and ferric sulfate tests, the extraction did not exceed 37% and 26%, respectively. Table 4 shows the ion concentration, pH and redox potential of the first washes of the SLS and ferric sulfate tests; for the other tests it corresponds to the effluent obtained from their 15 washes only. Table 4: Ion concentration, pH and redox potential of the first washes of the tests QQhCnn / 1 7Π7 / E / YILI SLS Type of reaction CuT g / i FeT g / i Fe2+ g / i Fe3+ g / i pH Eh mV SLS Method Water and acid (Bischofite) 19.86 6.26 0.56 5.7 1.2 731.8 SLS Method Water and acid (NaCl) 22.17 3.36 0.85 2.5 1.0 689.0 SLS Method Water and acid (FeCl3 x H2O) 29.57 16.2 13.8 2.5 1.1 613.0 SLS Method Water (Bischofite) 26.24 7.58 1.97 5.6 0.7 659.8 SLS Method Water (NaCl) 18.63 3.30 1.13 2.2 1.2 642.3 SLS Method Water (FeCl3 x H2O) 26.24 16.85 6.45 10.36 0.9 742 Ferric Sulfide Leaching 9.77 30.04 11.10 18.9 0.8 741.0 Chloride Leaching (Solid-Liquid) 9.53 8.92 4.36 4.6 0.5 651.0 Extended Curing (Bischofite) 10.92 7.62 1.06 6.6 1.6 646.9 Extended Curing (NaCl) 11.64 8.69 1.18 7.5 1.8 697.2 Tests using the SLS method with sodium chloride and bischofite show that the copper-to-iron ratio is higher for copper. However, in tests involving chloride leaching and prolonged curing, the copper-to-iron ratio is similar. Regarding redox potential, there is no trend indicating that above or below 700 mV results in greater or lesser copper extraction. Example 18: SEM microscopy images of Concentrate 1 after the Wetting and Drying stage. The results in Figure 16 were obtained from a test using the Solid-Liquid-Solid method in the presence of sodium chloride. The test consisted of weighing 200 grams of the concentrate. The sample was then subjected to a wetting stage, which involved the addition of 100 kg / t of NaCl. This was followed by the addition of a solution of water and acid containing 2 g / L of ferrous chloride and 3 g / L of ferric chloride, achieving a final moisture content of 12%. Once the concentrate was moistened, the second stage of the process began, in which the concentrate was stored in a drying chamber at 30°C for 25 days. After the drying and supersaturation period was completed, a representative sample of the concentrate was taken for microscopy analysis, using a TESCAN Vega 3 Scanning Electron Microscope, with a Bruker Quantax 400 series EDS probe detector, in order to visualize the crystallization and precipitation processes. Image A: General image of the concentrate sample, where the precipitates that were generated during the second stage of the method can be identified throughout the sample. Image B: Specific area of ​​the general image A (white circle), where the shape of the precipitates and crystals can be seen in detail, which correspond to copper and chlorine complexes, presenting a shape defined by the loss of moisture during the drying and supersaturation stage. QQhCnn / 1 7Π7 / E / YIL Image C: Specific area of ​​the general image A (black circle), where the shape of the precipitates and crystals can be seen in detail, which correspond to copper and chlorine complexes, presenting a shape defined by the loss of moisture during the drying and supersaturation stage. The preceding section is considered to be merely illustrative of the principles of the invention. The scope of the claims should not be limited by the illustrative embodiments set forth in the preceding section, but should be given the broadest interpretation consistent with the description as a whole.

Claims

NOVELTY OF THE INVENTION CLAIMS 1. A Solid-Liquid-Solid hydrometallurgical method for the solubilization of metals from minerals and / or concentrates of sulfide minerals of primary and / or secondary origin that contain them, characterized in that it comprises the following sequential and / or overlapping stages: I. Wetting, in which the mineral or concentrate is wetted by the addition of water or water-acid and hydrated and / or non-hydrated chloride salts; II. Drying and Supersaturation, in which the wetted mineral is dried by vaporization and / or evaporation, which can be carried out both in the pile, as well as on the conveyor belt, generating conditions of supersaturation, crystallization and recrystallization of the salts, favoring the phenomena of chemical and physical weathering and haloclasty on the mineral or concentrate; and III.Washing and re-wetting, where an acidified solution with or without chloride is added to remove the target metal species precipitated in the second stage of the process, also allowing the mineral or concentrate to be re-wetted in order to restore the optimum chloride and moisture concentration to the bed, where if the method is in continuous regime, in stage I the mineral or concentrate is contacted with recirculating solutions from the same process that may contain chloride, iron and copper ions, in a non-saturated environment, and where the three stages are carried out independently of the REDOX potential of the medium.

2. The method according to claim 1, characterized in that the hydrated chloride salt is selected from the group consisting of magnesium chloride hexahydrate (bischofite), ferrous chloride heptahydrate, ferric chloride hexahydrate, among others. QQhCnn / 1 7P7 / E / YILI 3. The method according to claim 1, characterized in that 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.

4. The method according to claims 1-3, characterized in that in step I the non-hydrated and / or hydrated chloride salt is sodium chloride and / or bischofite which is added in solid or solution form.

5. The method according to claim 4, characterized in that in step I the amount of sodium chloride and / or bischofite added is between 20 and 80 kg per ton of material, preferably between 30 and 60 kg / t.

6. The method according to claim 1, characterized in that steps I and II can be performed only with the addition of bischofite and / or bischofite and water and / or process solutions.

7. The method according to claim 1, characterized in that in steps I, II and III, the addition of chloride salts may include a mixture of hydrated and / or non-hydrated salts.

8. The method according to claim 1, characterized in that the addition of water and acid in step I is carried out separately or together, preferably together.

9. The method according to claim 1, characterized in that in step I the addition of sulfuric acid ranges from 0 to 40 kg per tonne of material, preferably between 10 and 20 kg / t. QQhCnn / 1 7P7 / E / YIL 10. The method according to claim 1, characterized in that in stage I the final moisture content of the agglomerated mineral can be between 6 and 20%, preferably between 8 and 10%.

11. The method according to claim 1, characterized in that step I can be performed on an agglomerating drum or directly on the conveyor belt.

12. The method according to claim 1, characterized in that in stage II the drying of the mineral is carried out with the pile covered and protected to generate the increase in temperature and maintain the evaporation kinetics.

13. The method according to claim 1, characterized in that in stage II the condition of supersaturation of species and salts is achieved by intentional and repetitive drying cycles.

14. The method according to claim 1, characterized in that in stage II the condition of supersaturation of species and salts is achieved by drying the mineral by injection of air and / or increase of temperature.

15. The method according to claim 1, characterized in that in stage II the supersaturation condition of species and salts is achieved by periods without addition of solutions.

16. The method according to claim 1, characterized in that in stage II, the pile is covered or capped during the drying cycles.

17. The method according to claim 1, characterized in that in stage I, the concentrations of salts to be replenished in the continuous-flow system range from 5 to 20 kg / t. QQhcnn / ιζηζ / E / γίΛΐ 18. The method according to claim 1, characterized in that steps I, II and III can be repeated one or more successive times until the maximum extraction of the desired metal is achieved.

19. The method according to claim 1, characterized in that after stage I, the sulfide minerals and / or mineral concentrates are subjected to drying cycles ranging from 15 to 90 days, where the supersaturation condition is generated and the crystallization of salts and precipitation of soluble chlorinated metal species occurs.

20. The method according to claim 19, characterized in that after stage I, the sulfide mineral, which may be of primary origin, mainly chalcopyrite, is subjected to 2 or 3 drying cycles ranging from 30 to 90 days, preferably 60-day cycles.

21. The method according to claim 19, characterized in that after stage I, the sulfide mineral, which may be of secondary origin, mainly chalcocite and covellite, is subjected to 2 or 3 drying cycles ranging from 15 to 45 days, preferably 15-day cycles.

22. The method according to claim 1, characterized in that in stage III the ore is washed by continuous or intermittent irrigation with a solution containing acidified water, or acid and chloride.

23. The method according to claim 1, characterized in that the metals to be solubilized are selected from the group that includes copper, zinc, nickel, molybdenum, cobalt, lead, among others. QQhcnn / ιζηζ / E / γΐΛ 24. The method according to claims 1 and 23, characterized in that in stage III, washing is carried out by means of a limited or prolonged irrigation, promoting the presence of Cu (I) or Cu (II), respectively.

25. The method according to the preceding claims, characterized in that the solubilization of the target metal can be carried out in the same way from sulfide minerals with arsenical contents and / or concentrates of arsenical sulfide minerals containing it.

26. The method according to any of the preceding claims, characterized in that steps I, II and III can be applied to copper minerals and / or concentrates, preferably chalcopyrite, bornite, tennantite, enargite, chalcocite and covellite.

27. The method according to claim 1, characterized in that step II can be applied in a drying chamber or greenhouse, which allows for the generation of a constant evaporation kinetics of the liquid.

28. The method according to any of the preceding claims, characterized in that chloride ions can be incorporated into the method in the form of bischofite, sodium chloride, potassium chloride, magnesium chloride, anhydrous ferrous chloride, anhydrous ferric chloride, calcium chloride or through the use of recirculating solutions of the same method containing chloride, iron and copper ions.

29. The method according to claim 1, characterized in that the metal to be solubilized is copper and the sulfide mineral is a primary and / or secondary copper mineral. QQhcnn / 1 ζηζ / E / γίΛΐ 30. The method according to claim 1, characterized in that step II is carried out in a solid-liquid-solid condition.

31. The method according to any of the claims, characterized in that steps I of wetting and II of drying and supersaturation can be carried out at pH between 0.5 and 5.

32. The method according to claim 1, characterized in that steps I of wetting, II of drying and supersaturation and III of washing can be carried out independently of the potential, under 700 mV or above 700 mV (Eh).

33. The method according to any of the preceding claims, characterized in that washing step III can be performed with a reused solution containing chloride and iron ions.

34. The method according to claim 1, characterized in that in steps I and II chloride salts can be used, which can be derived from seawater, brines from desalination plants, halite, bischofite and commercial sodium chloride.

35. The method according to any of the preceding claims, characterized in that steps I, II and III can be carried out at room temperature, preferably between 20 and 40°C.

36. The method according to claim 1, characterized in that the solution obtained from step II can undergo the traditional steps of solvent extraction and electrowinning or proceed directly to electrowinning. QQhcnn / 1 ζηζ / E / γίΛΐ 37. The method according to claim 1, characterized in that the Solid-Liquid-Solid method can be used in in-situ leaching.