hydrometallurgical process to extract gold or silver or both and optionally one or more additional e

专利摘要:
TREATMENT PROCESS FOR EXTRACTION OF PRECIOUS, BASE AND RARE ELEMENTS. The present invention describes a hydrometallurgical process for the recovery and separation of valuable elements, in particular gold and silver, from a feed material comprising a refractory, untreatable or otherwise less responsive to ores, concentrates and other pathway materials. of conventional treatment. In particular, a process is a process integrated into one or more existing value element extraction processes.
公开号:BR102015029540B1
申请号:R102015029540-5
申请日:2015-11-25
公开日:2021-06-08
发明作者:Keith Stuart Liddell；Lisa Anne Smith；Michael David Adams
申请人:Lifezone Limited；
IPC主号:

专利说明:

BACKGROUND OF THE INVENTION
[1] The present invention relates to a hydrometallurgical process for the recovery and separation of valuable elements, in particular gold and silver, from a feed material comprising a refractory, intractable or otherwise responding inferiorly to ores, concentrates and others materials from conventional treatment routes. In particular, the process is a process integrated into one or more existing value element extraction processes.
[2] Polymetallic ore bodies containing multiple valuable metals in lower grades are becoming increasingly attractive to resource companies to assess their potential for exploration, despite the greater metallurgical challenge in recovering and separating such elements into salable products or concentrates . This is generally the case for ores containing precious metals such as gold or silver, platinum group metals (PGMs), and other base and rare metals such as nickel, cobalt, copper, rare earth elements (REE) including yttrium and scandium as well as uranium, thorium, manganese, zinc, cadmium, molybdenum, vanadium, titanium and other smaller elements such as vanadium, germanium and gallium.
[3] Current hydrometallurgical process pathways for extracting valuable metals from polymetallic ore bodies are described in International Patent Publication no. WO 99/60178, known as the "Kell Process" (see Figure 1)1, International patent application WO 2014/009928, and Australian patent application 2013263848 (the contents of each of which are incorporated herein by reference. ). All of these processes require as the starting material an ore or an ore concentrate and produce one or more leachate liquids containing dissolved valuable metals and other elements. The Kell process is typically specifically applied to PGM and base metal containing concentrates.
[4] The core of the Kell Process pathway comprises the steps of:
[5] (i) Leaching an ore or concentrate made from an ore into a pressure oxidation sulfate leach to dissolve base metal sulfides contained in the ore or concentrate and forming a sulfate leach filtrate containing base metals and a residue containing platinum group metals (PGMs);
[6] (ii) Separate the sulfate leach filter from the residue;
[7] (iii) Calcining or heat treating the residue to form a calcination; and
[8] (iv) Leach the calcination in a chloride lye to dissolve the PGMs in solution forming a chloride lye filtrate for PGM recovery and a solid waste residue.
[9] However, a wide range of feed materials, in particular comprising ores containing silver or refractory gold or concentrates containing the precious metals gold or silver are problematic as they return low recoveries of these metals, making conventional process pathways such as cyanidation uneconomical or otherwise technically inadequate for handling these materials2.
[10] These refractory or intractable ores, concentrates and other materials can be classified to fall into several categories, including:
[11] 1. Conventional refractory sulfides (silver or gold particles are smaller than conventional grinding sizes and are encapsulated in various sulfide minerals) - typically treated by bacterial oxidation or pressure, calcination and/or ultra-fine grinding;
[12] 2 Submicroscopic Refractory Sulfides (sometimes referred to as "solid solution") - (gold or silver particles are so much smaller than conventional grinding sizes that they cannot be observed using scanning electron microscopy and are encapsulated in various minerals. sulfide) - typically treated by bacterial oxidation or pressure or calcination;
[13] 3. Preg-robbing materials (carbonaceous matter or other sorbent minerals such as clays are present that can decrease gold and silver recoveries by adsorbing or pregrobbing the gold and silver leached from cyanide leach solutions ) - typically treated by calcining or blinding with kerosene together with the use of stronger cyanide solution and higher carbon addition;
[14] 4. Carbon-blocked materials (carbonaceous matter such as kerogen is present which may decrease silver and gold recoveries by physical encapsulation) - typically treated by calcination;
[15] 5. Double refractory sulfides (gold or silver particles are smaller than conventional crush sizes and are encapsulated in various sulfide minerals; carbonaceous matter or other sorbent minerals are also present that can decrease gold and silver recoveries by physical encapsulation or "preg-robbing" of cyanide leach solutions) - typically treated by calcination or alkaline pressure oxidation;
[16] 6. Residues from calcination (residue after calcination and subsequent cyanide leach from concentrates or ores, containing gold or silver physically encapsulated in the remaining matrix) - typically not treatable using conventional methods;
[17] 7. Materials blocked with aluminate or silicate (silicon material/alumina or phases are present that may decrease gold and silver recoveries by physical encapsulation, coating or adsorption) - typically not treatable using conventional methods;
[18] 8. Refractory material considered to contain microgroups, containing gold or PGMs (eg "nanogold", "nanodimensional gold", "aurids", etc., which may also involve other elements such as Al, Si, Ti, V , Zr, Nb, Hg, Mo, W, Ag, Cu, Cs, La, etc.; at which scale bonds can be stronger than those between bulk atoms and consequently the chemical behavior of precious metals can be altered by termed "glue" effect - typically not treatable using conventional methods;
[19] 9. Slag (residue after melting concentrates or ores, containing gold or silver physically encapsulated in the remaining matrix) - typically not treatable using conventional methods;
[20] 10. Amalgamation waste (waste after mercury amalgamation of concentrates or ores containing gold or silver physically encapsulated in the remaining matrix) - typically treated using calcination along with addition of stronger cyanide; and
[21] 11. Refractory mineral phases in ores containing gold or silver (examples include various inferior or slow cyanide leach minerals such as electrum Au-Ag, acanthite Ag2S, aurostibite AuSb2, calaverite AuTe2, sylvanite (Ag, Au)Te2, among others - typically treated using calcination or lime boiling, along with addition of stronger cyanide;
[22] 12. "e-Waste", used catalysts and other scraps containing precious metals (a variety of such material with a range of metallurgical response characteristics is becoming increasingly available) - typically handled by a wide range of technologies mechanical, pyrometallurgical, hydrometallurgical and biohydrometallurgical separation;
[23] 13. Specific non-refractory concentrates (in particular instances where the concentrates are of a low type, contain elements detrimental to conventional processing, or the resource is too small to warrant an independent treatment facility) - typically not treatable using conventional methods to unless a toll treatment arrangement can be made with a proper installation.
[24] The use of conventional methods would require a separate and distinct flowsheet to be developed in an independent plant to be built for each material type and in some cases the material is not considered economically treatable using current available technology because ores contain a combination of categories of the above types or refractory capacity.
[25] An integrated process for treating and recovering valuable elements including precious, base and rare metals, and particularly gold or silver from any or a combination of these materials is therefore necessary rather than requiring an independent mill be built for each type of material. It would be additionally useful if such a process were able to be integrated into existing processes in power plants, such as the core Kell Process (as claimed in International Patent Publication No. WO 99/60178) or a modified Kell process (as claimed in the Patent Application International No. WO2014/009928, or Australian Patent Application No. 2013263848), or in other precious and base metal extraction processes such as Heap Leach, thereby benefiting from savings in capital, operating costs and infrastructure. A process whereby high grade value metal concentrates or single value metal products are produced on site offers considerable financial benefit by eliminating refinement charges.
[26] In addition, the use of cyanide, a toxic chemical that is conventionally used in silver and gold processing and requires increasingly stringent control measures to address tight environmental and safety concerns from stakeholders and industry. community is problematic. An alternative process that does not require your use would be helpful. In addition, conventional processes generate SO2 and other pollutants that are harmful to the environment and an alternative, environmentally responsible method is needed3. SUMMARY OF THE INVENTION
[27] According to a first embodiment of the invention, a hydrometallurgical process is provided to extract gold or silver or both and optionally one or more additional elements including PGMs, base elements, rare metals and/or rare elements, from a feed material comprising a refractory or intractable material, the process comprising the steps of:
[28] (i) Supply the feed material to a reaction vessel;
[29] (ii) Submitting the feed material to one or more leaching steps comprising:
[30] a) A hot sulfuric acid leaching step under pressure and/or atmospheric conditions to produce a product slurry comprising salable metal sulphates in solution and a solid residue containing salable metals;
[31] b) Optionally subjecting the slurry from a) to a conditioning step, in which conditions are selected depending on gangue mineralogy, comprising sulfuric acid of approximately 25 - 300 g/L or alkaline treatment a pH value of 10 - 14 (including, for example, a lime boil);
[32] c) Optionally submit the solid residue from a) or b) to a heat treatment step of approximately 300 - 700°C or approximately 700 - 1000°C, (where conditions are selected depending on gangue mineralogy ) under reducing or oxidizing conditions;
[33] d) Subject feed material or solid waste from step a) or where relevant, b) or c) above to a chloride leach step in a chloride leach medium to produce salable metals soluble in solution of Pregnant Chloride Bleach (PLS);
[34] e) Subject the chloride PLS from step d) above to one or more techniques including ion exchange (IX), chelation, molecular recognition technology (MRT), addition of polymeric or other sorbents, solvent extraction, precipitation using hydroxides, ammonia, carbonates or sulfides, electrolytic extraction, and/or reduction to produce one or more solution products or intermediate solids for the recovery of gold and silver, as well as any associated minor PGMs and other rare or base metals valuable in the chloride PLS;
[35] f) Optionally subjecting the solution product or intermediate solid from step e) above to an additional purification and/or upgrade step comprising one or more techniques including IX, MRT chelation, addition of polymeric sorbents or others; solvent extraction, precipitation using hydroxides, ammonia, carbonates or sulfides, electrolytic extraction and/or reduction;
[36] g) Optionally submit the intermediate solution product from step e) above to the recovery of hydrochloric acid, calcium and residual metals, through one or more steps including pre-boil, rectification, distillation, adsorption, boiling again, and/or pyrohydrolysis, to provide a product slurry comprising a solid residue containing salable metals and salable metal sulfates in solution;
[37] h) Optionally subjecting the solid residue from step g) above to a step of further chloride leaching in a chloride leaching medium to produce salable metals soluble in a purified chloride PLS;
[38] i) Optionally subject the discharge solution from step (e), (g) or (h) to a sorption step whereby salable PMs are adsorbed onto one or more resins or sorbents and base metals are discharged in a solution, or in an additional sulfide precipitation step to produce a second product slurry, followed by solid-liquid separation of a secondary solid residue from the second product slurry for further purification by a method such as that outlined in (e) above, or direct sale to a third party; and
[39] j) Optionally subject the chloride PLS from step h) above to one or more techniques including ion exchange (IX), chelation, molecular recognition technology (MRT), addition of polymeric or other sorbents, solvent extraction, precipitation using hydroxides, ammonia, carbonates or sulfides, electrolytic extraction and/or reduction to produce one or more solution products or intermediate solids for the recovery of gold and silver, as well as any associated minor PGMs and other rare or base metals valuable in the Chloride PLS.
[40] The refractory or intractable material may be selected from the group consisting of ores, concentrates, wastes and other materials from the following categories:
[41] (i) Conventional refractory sulfides where silver or gold particles are smaller than conventional crush sizes and are encapsulated in various sulfide minerals;
[42] (ii) Submicroscopic refractory sulfides, also referred to as "solid solution" refractory sulfides where gold or silver particles are so much smaller than conventional crush sizes that they cannot be observed using scanning electron microscopy and are encapsulated in various sulphide minerals;
[43] (iii) Preg-robbing materials in which carbonaceous matter or other sorbent minerals including clays are present which may decrease silver and gold recoveries by adsorbing or preg-robbing the gold and silver leached from leach solutions of cyanide;
[44] (iv) Carbon-blocked materials in which carbonaceous matter including kerogen is present that may decrease gold and silver recoveries by physical encapsulation;
[45] (v) Double refractory sulfides where gold or silver particles are smaller than conventional crush sizes and are encapsulated in various sulfide minerals and where carbonaceous matter or other sorbent minerals are also present that can decrease gold and silver recoveries by physical encapsulation or "preg-robbing" of cyanide leach solutions;
[46] (vi) Calcination residues which are the residue after calcination and subsequent cyanide leaching from concentrates or ores, containing gold or silver physically encapsulated in the remaining matrix;
[47] (vii) Blocked aluminate or silicate materials where alumina and/or siliceous matter or phases are present that may decrease gold and silver recoveries by physical encapsulation, coating or adsorption;
[48] (viii) Refractory material considered to contain microclusters that contain gold or PGMs, including "nanogold", ''nanodimensional gold", and "aurids", which may also involve other elements including Al, Si, Ti, V, Zr , Nb, Hg, Mo, W, Ag, Cu, Cs, La in which scale bonds can be stronger than those between bulk atoms and consequently the chemical behavior of precious metals can be altered by the so-called "glue" effect;
[49] (ix) slag which is the residue after melting of concentrates or ores, containing gold or silver physically encapsulated in the remaining matrix;
[50] (x) Amalgamation waste, which is the waste after mercury amalgamation of concentrates or ores, containing gold or silver physically encapsulated in the remaining matrix;
[51] (xi) Refractory mineral phases in ores containing gold or silver (including various inferiorly or slow cyanide leach minerals including Au-Ag electrum, acanthite Ag2S, aurostibite AuSb2, calaverite AuTe2, sylvanite (Ag, Au)Te2, among others;
[52] (xii) "e-Waste", used catalysts and other scraps containing precious metals; and
[53] (viii) Specific non-refractory concentrates including where conventional processing is not possible (eg use of cyanide is prohibited), concentrates are of the low type, contain harmful elements for conventional processing, or the resource is too small to ensure a independent treatment facility.
[54] The process may further comprise a step of separating the solid waste containing salable metals from the salable metal sulfides, in solution from the product slurry of steps a) or where relevant, b), f) or g) , and then providing the resulting separated solid residue for any one of steps b), c) or d). The separation step can be carried out by filtration, or by any other liquid/solid separation means known to those skilled in the art.
[55] The process may further comprise a step of separating the solid residue containing salable metals from the salable metal chlorides in solution from the product slurry of step d) and then providing the resulting separated chloride PLS to step e) . The separation step can be carried out by filtration, or by any other liquid/solid separation means known to those skilled in the art.
[56] The process may further comprise a step of recovering salable metals from metal sulfates in solution from the product slurry of steps a) or where relevant, b) and/or from the intermediate product upgrade in the step f), or from the metal sulfate residue produced in step g), through techniques such as solvent extraction, ion exchange, precipitation using hydroxides, ammonia, carbonates or sulfides, electrolytic extraction, reduction, recycling and others techniques known to those skilled in the art based on techno-economic considerations.
[57] The feed material, ore, concentrate, residue or scrap material from (i) may be initially processed by crushing, grinding or may be as extracted. Alternatively, or in addition, the feed material can be subjected to a beneficiation step to produce an intermediate ore product for supply to the reaction vessel. The beneficiation step can be carried out by a combination of crushing, grinding, filtering, separating, sizing, sorting, magnetic separation, electrostatic separation, flotation or gravity separation thereby to concentrate the valuable metals or reject a gangue component, or by another means of beneficiation known to those skilled in the art.
[58] The feed material, ore, intermediate ore product, concentrate or solid residue from step a) or b) may be subjected to a heat treatment to produce a heat-treated calcination before subjecting it to step d ) .
[59] Heat treatment can be carried out at approximately 80 - 750°C for up to 120 minutes, typically approximately 300 - 700°C for 10 to 30 minutes, under oxidizing, neutral or reducing conditions, to remove volatile components from the solid residue and reduce or negate the preg-robbing attributes of the material, while making refractory mineral phases such as silver jarosites suitable for subsequent leach recovery.
[60] Additionally, heat treatment can be carried out at approximately 500 - 1000°C for up to 120 minutes, typically approximately 700 - 1000°C for 30 to 120 minutes, under oxidizing, neutral or reducing conditions, to condition the salable metals to be soluble in chloride leaching medium.
[61] Thermal processes can be performed as individual steps of a sequential heat treatment process, or as a combined step.
[62] The product slurry from step a) can optionally be subjected to an alkaline or hot acid conditioning step or an atmospheric bleach step to effect the removal or conversion of iron such as jarosite or basic ferric sulfate (BFS) to release silver, as well as potentially iron, aluminum and magnesium sulphates, to the solution phase, and then submitted to step c).
[63] In a further embodiment of the invention the chloride PLS of d) and the intermediate solution or solid product of e) in the first embodiment above can be subjected to a sorption step whereby salable metals are adsorbed onto a resin or sorbent and base metals are discharged into a solution.
[64] In a further embodiment of the invention the chloride PLS of d) and the intermediate solution or solid product of e) in the first embodiment above may be subjected to precipitation and purification comprising any one or more of the following steps:
[65] (i) Subject the chloride PLS from d) of the solution product or intermediate solid from e) above, or both to a sulfide precipitation and reduction step by adding a solution containing one or a combination of salts or sulfide acids, hydrogen sulfide, thiosulfate, metabisulfite or sulfite or a gas including sulfur dioxide or hydrogen sulfide, thereby to produce a product slurry comprising a solid residue containing elemental sulfur, metal sulfides and/or alloys and a flushing solution;
[66] (ii) Separation of liquid-solid from solid residue from step (i) from the discharge solution, for example, by filtration or other suitable liquid-solid separation device, at temperatures between approximately 10 and 130°C;
[67] (iii) Subjecting the solid residue from step (ii) to a series of purification and recovery steps comprising:
[68] a) A sulfur removal step comprising sublimating the solid residue at temperatures between approximately 200 and 500°C (typically in an oven or other suitable heat treatment device) to produce a solid residue and a sulfur product by sublimation, adsorption or scrubbing;
[69] b) Optionally subjecting the solid residue from step a) above to a sulfur removal step comprising dissolving the solid residue (eg, in an agitated container or other suitable contactor) in a suitable sulfur solvent, including , but not limited to: aromatic hydrocarbons (eg, xylene and/or its isomers or mixtures (such as xylol), toluene, ethyl benzene, etc.); chlorinated or sulphide hydrocarbons (eg carbon tetrachloride, chloroform, carbon disulfide, etc.); or sulfur-containing ligands (e.g., sulfite, sulfide, etc.), at temperatures between approximately 10 and 130°C, to provide a solid residue and a sulfur product by sublimation, adsorption, or scrubbing;
[70] c) Subjecting the solid residue from step a) and b), where relevant, above, to a pressure oxidation liquor at temperatures between approximately 110 and 230°C;
[71] d) Subjecting the solid residue from step c) above to an atmospheric sulfuric acid leach at temperatures between approximately 10 and 110°C to provide a slurry comprising a solid residue that includes salable metals and a sulfate leach solution;
[72] e) Solid-liquid separation of solid residue comprising salable metals from step d) above from the sulfate leachate solution, for example, by filtration or by means of another suitable solid-liquid separation device , at temperatures between approximately 10 and 130°C;
[73] f) Optionally subjecting the sulfate leachate solution from e) above to a sorption step whereby salable metals are adsorbed to a resin or sorbent and base metals are discharged into a solution;
[74] g) Subject the sulphate leachate solution from e) and, where relevant, the discharge solution from f) to aging, evaporation, precipitation and/or recycling in a primary base metal recovery circuit from the Kell process as claimed in any one of WO99/60178, W02014/009928, or Australian Patent Application No. 2013263848; and
[75] (iv) Optionally subject the discharge solution from step (ii) to a sorption step whereby salable metals are adsorbed to a resin or sorbent and base metals are discharged into a solution, or to a step of further sulfide precipitation to produce a second product slurry, followed by liquid-solid separation of a secondary solid residue from the second product slurry for further purification by a method such as that outlined in (iii) above, or direct sale to a third.
[76] In a further embodiment of the invention, the discharge solution from step (ii) above and/or intermediate solution product from step e) of the first embodiment of the invention may be subjected to hydrochloric acid, calcium and recovery of residual base metal and separation step comprising:
[77] a) feed the discharge solution and/or the intermediate solution product into a pre-boil evaporator together with seed gypsum in this way to generate a hydrochloric acid gas and gypsum precipitate, followed by liquid-solid separation to provide precipitated gypsum for recovery and a treated flush solution;
[78] b) feed the discharge solution from step a) above to a sulfuric acid rectification column or reboiler together with sulfuric acid thereby to generate a hydrochloric acid gas and a sulfuric acid solution comprising base and/ or salable and/or recoverable rare metals;
[79] c) alternatively, feed the discharge solution from step a) above to a pyrohydrolysis reactor to provide a slurry comprising a solid iron oxide residue for recovery and a solution of base and/or rare metals, followed by liquid-solid separation;
[80] d) subjecting the sulfuric acid solution generated in step b) above and/or the base metal and/or rare metals solution from step c) above to a cooling and aging step, whereby the salts of metal sulphate crystallize or undergo a sorption step and are recovered, for example, by evaporation or precipitation and/or are recycled back to a Kell Process primary base metal recovery loop as claimed in any one of WO99/60178, WO2014/009928, or Australian patent application no. 2013263848;
[81] e) subjecting the hydrochloric acid gas from step a) or step b) above to distillation and sorption, thereby to recover a hydrochloric acid solution.
[82] The recovered hydrochloric acid can be recycled back to the chloride leach step d) of the first embodiment of the invention. The recovered hydrochloric acid solution can be recycled back to a chloride leach step or a chlorination step of a Kell Process primary precious metal recovery loop as claimed in WO99/60178, WO2014/009928, or Patent Application Australia No. 2013263848.
[83] For example, sulfuric acid comprising salable or recoverable base and/or rare metals from step b) above may comprise metal sulfate salts such as copper, nickel, cobalt, rhodium, ruthenium, iridium, vanadium, germanium, gallium or scandium.
[84] The feed material may comprise an individual material or a mixture of materials of a different nature.
[85] The process of the invention may optionally further comprise an initial step of subjecting the chloride PLS of step d) in the first embodiment of the invention to an aging step for crystallizing silica, comprising:
[86] (i) Feed the chloride PLS into a containment vessel;
[87] (ii) Add silica seed solids to chloride PLS;
[88] (iii) Allow the chloride PLS to remain at room temperature to precipitate out a solid residue comprising silica;
[89] (iv) Separating the precipitated solid residue comprising silica from the solution of (iii) to produce exhausted silica solution; and
[90] (v) Feed the spent silica solution from (iv) to step (i) of the process.
[91] The process of the invention may optionally comprise an initial step of subjecting the chloride PLS of step d) in the first embodiment of the invention to a concentration step to produce a concentrated PLS by any one or more of:
[92] a) Evaporation with HCl condensation recovery; and/or
[93] b) Reverse osmosis (RO), nanofiltration (NF), filtration or other membrane-based separation method.
[94] Process sorption steps can comprise any one or more of the following steps:
[95] a) Contacting the solution with an ion exchange resin (IX) or other suitable sorbent whereby salable metals, including gold, silver and PGMs if present, are adsorbed onto the resin or sorbent and base metals are discharged into a solution; and/or
[96] b) Elute the adsorbed salable metals, including gold, silver and PGMs if present, from resin IX or sorbent and precipitate the gold, silver and PGMs if present, from the eluate using a reducing medium or, if PGMs are present, using a caustic, ammoniacal or reducing solution to form a high grade metal concentrate or single value metal products; and/or
[97] c) Directly incinerate the loaded resin or sorbent to produce a high-grade metal concentrate or single-value metal products, and/or
[98] d) Optionally, further process salable metals produced by any of steps (a) to (c) above.
[99] Elution step (b) can be carried out using a solution comprising acidic thiourea, sulfite or hydrosulfite or chloride salts, or other eluents known to those skilled in the art.
[100] In an additional embodiment of the invention, the techniques described in international patent application no. WO2014/009928 (incorporated herein by reference) can be applied to the process of the invention, thereby to recover sulfuric acid and precipitate a storable or potentially salable iron product. Specifically, the process can be as follows: 1) subjecting the concentrate to a pressure-modified oxidation step to selectively separate base metals from the precious metals in sulfate medium, wherein the pressure-modified oxidation step is partial or fully oxidize base metal sulphide minerals in a mixture of sulphate and elemental sulphur, to produce a product slurry containing a base metal sulphate in solution and a solid residue containing precious metals together with a mixture of sulphate and elemental sulphur ; 2) the product slurry from the pressure modified oxidation step 1) is optionally subjected to a hot acid etching (or atmospheric leach) step to effect the removal of additional iron as well as potentially magnesium and aluminum sulfates to the solution phase; 3) the product slurry from the pressure modified oxidation step 1) and/or atmospheric leach step 2) is filtered to provide a solid residue containing precious metals together with a mixture of sulfate and elemental sulfur, and a filtrate containing base metal sulfates; 4) the solid residue from step 3) is subjected to a heat treatment: a. to remove sulfate and elemental sulfur from the solid residue as disulfide, sulfur dioxide and/or hydrogen sulfide gas, and b. to condition the precious metals to be soluble in chloride medium; and 5) the solid residue treated from step 4) is subjected to precious metal recovery by leaching in chloride leaching medium to recover the precious metals. In addition, the chloride PLS is optionally subjected to solvent extraction to remove additional iron.
[101] In addition, technologies such as precipitation or crystallization can be employed in the process, including PLS or copper sulfate solutions, to produce a potentially salable or storable ferrous or ferric sulfate or hydroxide product while recovering sulfuric acid in a suitable flow. for recycling.
[102] In an alternative embodiment of the invention, a conventional low-pressure or atmospheric lye using sulfuric acid can be applied directly to the product slurry comprising the sulfate PLS and solid residue from step a) of the first embodiment of the invention, thereby to removing excess iron sulphates from the solid residue in the sulphate PLS. The sulfate PLS can then be subjected to precipitation of ferric hydroxide sprayed with oxygen or air under pressurized or atmospheric conditions to remove excess iron sulfate.
[103] Alternatively, or in addition to conventional low pressure or atmospheric lye using sulfuric acid applied directly to the product slurry comprising the sulfate PLS and solid residue from step a) of the first embodiment of the invention, where the solid residue is subjected to treatment thermal, excess soluble iron can be removed from heat-treated calcination.
[104] The chloride leaching medium of step e) of the first embodiment of the invention may contain iron chloride and may be treated by pressure, precipitation or crystallization, concentrated by evaporation, reverse osmosis, nanofiltration or other membrane technology, or treated by sparging/rectifying, pyrohydrolysis or other technique known to those skilled in the art to produce an iron-containing product.
[105] The chloride leaching medium of step d) of the first embodiment of the invention may comprise hydrochloric acid or saline brine in combination with an oxidizing agent such as chlorine, hypochlorite, nitric compounds, hydrogen peroxide or other oxidizing agents known to those skilled in the art, and the refractory material from step (i) or solid residue from step a) of the first embodiment of the invention can be leached under oxidizing conditions, thereby to generate a chloride PLS comprising one or more salable elements including Au , Ag, PGMs, as well as Ni, Co, Cu, REE, Y, Sc, U, Th, Zn, Mn, Cd, Mo, V and Ti.
[106] A chloride PLS comprising one or more salable elements including Au, Ag, PGMs, as well as Ni, Co, Cu, REE, Y, Sc, U, Th, Zn, Mn, Cd, Mo, V, and Ti can be subjected to the separation and/or recovery of one or more salable elements through techniques such as solvent extraction, IX, precipitation using hydroxides, carbonates or sulfides, electrolytic extraction, reduction and other techniques known to those skilled in the art based on considerations technical-economical.
[107] Thermal processes can be performed as individual steps of a sequential heat treatment process, or as a combined step. The oxidation chloride leach medium set out above, or the chloride leach medium of step d) of the first embodiment of the invention may contain iron chloride and may be treated by pressure, precipitation or crystallization, concentrated by evaporation, reverse osmosis, nanofiltration or other membrane technology, or treated by sparging/rectification, pyrohydrolysis or other technology known to those skilled in the art to produce an iron-containing product.
[108] In a further specific embodiment, the chloride leaching step d) of the first embodiment of the invention may comprise a less acidic chloride leaching medium having a pH between approximately 2.5 and 7.5 maintained at a temperature in the range 50 - 150 °C.
[109] In a further specific embodiment, the chloride leaching step d) of the first embodiment of the invention may comprise a chloride leaching medium with a free acidity between approximately 50 to 300 g/L HCl maintained at a temperature in the range of 50-150°C.
[110] According to a further specific embodiment, the chloride leaching step d) of the first embodiment of the invention can be carried out by pressure or atmospheric autoclave leaching with saline brine under oxidizing conditions.
[111] Any one or more of the processes of the invention may be integrated into an existing process including, for example, a "Kell Process" as claimed in WO99/60178 or a modified Kell Process as claimed in WO2014/009928 or Australian patent application 2013263848, or a conventional pile leach process for base metal recovery. BRIEF DESCRIPTION OF THE DRAWINGS
[112] Figure 1 is a simplified block flow diagram of the Kell process;
[113] Figure 2 is a simplified block flow diagram showing the modified Kell process of the present invention (KellGold);
[114] Figure 3 is a simplified block flow diagram illustrating the integration of the KellGold process of the present invention with the Kell process for PGM recovery, and other conventional processes;
[115] Figure 4 is a simplified block flow diagram illustrating the integration of the KellGold process of the present invention with a conventional pile leach process for base metal recovery, as an illustration. DETAILED DESCRIPTION OF THE INVENTION
[116] The present invention provides a hydrometallurgical process for the recovery and separation of valuable elements, in particular gold and silver, from a feed material comprising refractory, intractable or otherwise less responsive to conventional treatment route ores, concentrates and other materials. In particular, the process is a process integrated into one or more existing value element extraction processes.
[117] Furthermore, the process of the invention does not require the use of cyanide or mercury, toxic chemicals that are conventionally used in gold and silver processing that require stringent environmental and safety controls. Furthermore, the process of the invention provides an environmentally responsible, alternative method for extracting precious metals such as gold and silver that does not generate SO2 and other pollutants that are harmful to the environment.
[118] The terms "element", "mineral" and "metal" are used interchangeably in this specification.
[119] "Refractory" is typically taken to mean a material that provides less than 90% recovery of gold and/or silver when subjected to cyanide leaching, even under highly excessive cyanide additions.
[120] For the purpose of this application, the phrase "refractory or intractable material" means ores, concentrates, residues and other materials that are selected from the following categories:
[121] 1. Conventional refractory sulfides (silver or gold particles are smaller than conventional grinding sizes and are encapsulated in various sulfide minerals) - typically treated by bacterial oxidation or pressure, calcination and/or ultra-fine grinding;
[122] 2. Submicroscopic refractory sulfides (sometimes referred to as "solid solution") - (gold or silver particles are so much smaller than conventional grinding sizes that they cannot be observed using scanning electron microscopy and are encapsulated in various minerals of sulfide) - typically treated by bacterial oxidation or pressure or calcination;
[123] 3. Preg-robbing materials (carbonaceous matter or other sorbent minerals such as clays are present that can decrease gold and silver recoveries by adsorbing or preg-robbing gold and silver leached from cyanide bleach solutions ) - typically treated by calcining or blinding with kerosene together with the use of stronger cyanide solution and higher carbon addition;
[124] 4. Carbon-blocked materials (carbonaceous matter such as kerogen is present that may decrease silver and gold recoveries by physical encapsulation) typically treated by calcination;
[125] 5. Double refractory sulfides (gold or silver particles are smaller than conventional crush sizes and are encapsulated in various sulfide minerals; carbonaceous matter or other sorbent minerals are also present that can decrease gold and silver recoveries by physical encapsulation or "preg-robbing" of cyanide bleach solutions) - typically treated by calcination or alkaline pressure oxidation;
[126] 6. Residues from calcination (waste after calcination and subsequent cyanide leach from concentrates or ores, containing gold or silver physically encapsulated in the remaining matrix) - typically not treatable using conventional methods;
[127] 7. Materials blocked with aluminate or silicate (silicon material/alumina or phases are present which may decrease gold and silver recoveries by physical encapsulation, coating or adsorption) - typically not treatable using conventional methods;
[128] 8. Refractory material considered to contain microgroups, containing gold or PGMs (eg "nanogold", "nanodimensional gold", "aurids", etc., which may also involve other elements such as Al, Si, Ti, V , Zr, Nb, Hg, Mo, W, Ag, Cu, Cs, La, etc.; in which scale bonds can be stronger than those between bulk atoms and consequently the chemical behavior of precious metals can be altered by termed "glue" effect - typically not treatable using conventional methods;
[129] 9. Slag (residue after melting concentrates or ores, containing gold or silver physically encapsulated in the remaining matrix) - typically not treatable using conventional methods;
[130] 10. Amalgamation waste (waste after mercury amalgamation of concentrates or ores containing gold or silver physically encapsulated in the remaining matrix) - typically treated using calcination along with addition of stronger cyanide; and
[131] 11. Refractory mineral phases in ores containing gold or silver (examples include various inferiorly or slow cyanide leach minerals such as Au-Ag electrum, Ag2S acanthite, AuSb2 aurostibite, AuTe2 calaverite, silvanite (Ag, Au)Te2, among others - typically treated using calcination or lime boiling, along with addition of stronger cyanide;
[132] 12. "e-Waste", used catalysts and other scraps containing precious metals (a variety of such material with a range of metallurgical response characteristics is becoming increasingly available) - typically handled by a wide range of technologies mechanical, pyrometallurgical, hydrometallurgical and biohydrometallurgical separation; or
[133] 13. Specific non-refractory concentrates (in particular instances where the concentrates are of a low type, contain elements detrimental to conventional processing or the resource is too small to warrant an independent treatment facility) - typically not treatable using conventional methods to unless a toll treatment arrangement can be made with a proper installation.
[134] "PGMs" stand for ruthenium (Ru), rhodium (Rh), palladium (Pd), osmium (Os), iridium (Ir) and platinum (Pt).
[135] "Precious metals" means gold, (Au), silver (Ag), and PGMs in the few cases where ores containing precious metals also contain associated minor PGMs.
[136] As used herein, "base metals" means industrial non-ferrous metals excluding precious metals such as aluminum, copper, lead, nickel, tin, tungsten, zinc, cadmium and manganese. "Rare earth elements" means a group of chemically similar metallic elements comprising the lanthanide series (fifteen elements), scandium and yttrium. "Rare metals" means a group of metals including the rare earths, germanium, gallium, indium, scandium and other valuable nominal metals that may be worth recovering, including uranium, thorium, molybdenum and vanadium.
[137] "KellGold" indicates the process described in this application. "Kell" indicates the core process described in international patent publication WO 99/60178 and associated modified process patents W02014/009928 or Australian patent application 2013263848 (all incorporated herein by reference) for recovery of PGMs and base metals from concentrates.
[138] For purposes of this application the terms "pressure and/or atmospheric conditions" and "hot sulfuric acid leach step" mean a sulfuric acid leach step comprising any one or a combination of a temperature and atmospheric pressure leach (20-100°C), low (100-130°C), medium (130-220°C) or high (220-260°C), conventional using sulfuric acid.
[139] The term "hot acid conditioning step" means a conventional atmospheric (20-100°C) or low (100-130°C) pressure and temperature leach using sulfuric acid.
[140] A "hot alkaline conditioning step" means a boil of lime at a pH value of 10-14.
[141] An "atmospheric leach stage" means a conventional (20-100°C) atmospheric pressure and temperature leach using sulfuric acid.
[142] A "chloride leach step" means a conventional atmospheric (20-100°C) or low (100-130°C) pressure and temperature leach under oxidizing conditions using hydrochloric acid or brine in combination with a oxidizing agent such as chlorine, hypochlorite, nitric compounds, hydrogen peroxide or others known to those skilled in the art.
[143] The term "cooling and aging" in the context of this application means allowing PLS or other process liquid to remain for a period of time, optionally with addition of seed solids from a subsequent liquid-solid separation step and optionally with applied external cooling.
[144] The term "saleable elements" or "saleable metals" means any element or metal that is capable of generating a revenue by selling the element or metal in metallic form or as a salt or precipitate of the metal or element.
[145] There is a considerable range of materials that are not treatable using current conventional technologies, or that respond inferiorly, or that may require the development of specific flowchart design and construction, of a custom built plant that may be too expensive to justify the capital expense given the size of the specific resource. Applicants have developed a process as described here that accepts a wide variety of types of refractory or non-refractory material as feed, without modification or with minimal circuit modifications from one feed type to the next, and does not require the use of mercury-containing reagents or toxic cyanide.
[146] As provided in more detail in the steps below, an important aspect of the invention that allows for higher recovery of base metals and precious metals is the ability to recycle any sulfate stream that is produced in the chloride leach loop, including metal sulphate slurry from the HCl recovery circuit, and the atmospheric leach/PM sulphide pressure oxidation solution back to the sulphate leach circuit for base metal recovery, with the proviso that chloride has been removed from the solution. The solutions can be recycled back into the pressure oxidation feed or atmospheric leach feed, depending on the remaining acid and water for the specific application. The enhanced recovery is achieved by a) the secondary leaching of base metals in the chloride leach loop and b) the way in which the HCl is regenerated by distillation from sulfuric acid.
[147] For reference purposes, the "Kell Core Process" for recovering PGMs and base metals from concentrates is shown schematically in Figure 1.
[148] As illustrated in Figure 2, the main embodiment of the invention is a hydrometallurgical process for extracting salable elements including valuable metal, particularly gold and silver, from a range of very different feed materials comprising refractory or intractable material types. Key to the process lies in its ability to achieve high recoveries of Au and Ag along with by-products such as Cu, Ni, Co, Zn, Mn, Sc, H2SO4, S, PGMs and others by treating separate feed materials. or blended comprising various sulfides refractory, non-refractory and carbonaceous silicates from calcinations and other materials by a multi-step but unique process. Removing most of the sulfur and base metals in the first stage of the process facilitates immediate removal of the remaining precious metals and base metals in the second stage of the process. This process completely avoids the use of toxic substances such as cyanide or mercury in the recovery process, and also avoids the emission of sulfur dioxide and other environmentally sensitive elements into the atmosphere.
[149] The feed materials (10) entered into the process can be as extracted, as received or can be ground to a finer grain size. The input feed materials (10) may also have undergone a previous beneficiation step such as filtration, sizing, classification, magnetic separation, electrostatic separation, dense media separation, radiometric separation, optical separation, or gravity separation to condense the valuable metals or reject a denim component. However, the need and type of crushing or processing at this stage would be determined by the characteristics of the specific material.
[150] The process may comprise a first step where a feed material (10) is subjected to a hot sulfuric acid leach step (12) under pressure and/or atmospheric conditions to produce a product slurry comprising metal sulfates valuable in solution and a solid residue containing valuable metals. The solid residue would then be separated from the metal sulfates in solution by a solid/liquid separation means (14a), such as by filtration or other means known to those skilled in the art.
[151] The sulfuric acid leach product slurry comprising the sulfate PLS and solid residue can be further treated by a conventional low or atmospheric pressure leach using sulfuric acid (16), allowing removal or conversion of excess iron sulfates and/or jarosites from the solid residue in the sulfate PLS for removal by precipitation of ferric hydroxide sprayed with air or oxygen under atmospheric or pressurized conditions.
[152] If required for specific ore types, subject the sulfuric acid lye product slurry to a conditioning step comprising treatment with acid or alkali.
[153] Salable metals can be recovered by a base metal recovery step (18) from any of the solutions comprising metal sulfates, including, the sulfuric acid leach product slurry by techniques such as solvent extraction , ion exchange, precipitation using hydroxides, ammonia, carbonates or sulfides, electrolytic extraction, reduction, recycling and other techniques known to those skilled in the art based on techno-economic considerations.
[154] Optionally, techniques described in international patent publication no. WO2014/009928 (the content of which is incorporated herein by reference) can also be applied, allowing sulfuric acid recovery and precipitation of a potentially salable or storable iron product. Specifically, the solid waste can first be subjected to heat treatment (20a) to produce off-gases comprising sulfur and the off-gases can then be subjected to a process of recovering sulfur:
[155] a. By condensation as an intermediate elemental sulfur product;
[156] b. In an intermediate product of sulfuric acid; or
[157] c. From drier exhaust gases into a thiosulfate, polythionate, polysulfide, sulfide or similar intermediate product.
[158] Typically, heat treatment would be carried out at approximately 80 - 750°C for up to 120 minutes, preferably at approximately 300 - 700°C for 10 to 30 minutes, under oxidizing, neutral or reducing conditions, to remove volatile components from the solid residue and reduce or negate the preg-robbing properties of the material.
[159] An additional heat treatment (20b) may be carried out if necessary at approximately 500 - 1000°C for up to 120 minutes, preferably at approximately 700 - 1000°C for 30 to 120 minutes, under oxidizing, neutral or reducing conditions, to condition the valuable metals to be soluble in chloride leaching medium. Additionally, this step can negate or modify preg-robbing and encapsulation or coating properties of clay minerals, thereby unlocking precious metals for leaching. For example, silver jarosite present in the material would decompose at 400-700°C in the heat treatment step, making the silver available for chlorination leach. However, if an economically sufficient proportion of the gold and silver is already soluble and the material does not exhibit preg-robbing characteristics without requiring additional heat treatment, then this step can be omitted. Thermal processes can be carried out as individual steps of a sequential heat treatment process, or as a combined step.
[160] The chloride leaching step (22) can be optimized for effective recovery and/or separation of some of the salable elements that may be present in the multi-composition feed. Specifically, the chloride leaching step (22) can be performed under oxidizing conditions using hydrochloric acid or saline brine in combination with an oxidizing agent such as chloride, hypochlorite, nitric compounds, hydrogen peroxide or others known to those skilled in the art . Value elements such as Au, Ag, as well as Pt, Pd, Rh, Ru, Ir, Os (ie PGMs), Ni, Co, Cu, REE, Y, Sc, U, Th, Zn, Mn, Cd, Mo, V, Ti, Ge, Ga are leached into the chloride-pregnant bleach (PLS) solution.
[161] Precious metals including gold and silver are separated and recovered (24) from chloride PLS using conventional methods known to those skilled in the art, and may include techniques such as solvent extraction, ion exchange, precipitation using hydroxides, carbonates or sulfides, electrolytic extraction, reduction and others. The selection of unit-specific processes for separation and/or recovery of elements of by-product value is made based on considerations of product requirements and techno-economics, such as the production of pure metals in the form of powder "sponge", bars end-product precursors, such as catalyst form solutions. In some cases, a less pure product may be preferable. Techniques such as solvent extraction, ion exchange, precipitation using hydroxides, carbonates or sulfides, electrolytic extraction, reduction and others can be used to obtain separation and/or recovery of these elements from chloride PLS. In particular, certain silver-containing or equally gold-containing ores that provide low recoveries using conventional treatment methods are expected to provide high recoveries using the KellGold process technique.
[162] The salable elements would include, in particular, gold and silver, but may additionally include other valuable metals such as platinum group metals (PGMs) and rare metals. These metals are separated through the process from other valuable metals such as nickel, cobalt and copper, and additionally rare earth elements, including yttrium and scandium, and uranium, thorium, vanadium, titanium, manganese, zinc and cadmium, while Iron components can also be extracted as potentially salable products.
[163] The chloride and/or sulfate acids from the process can be recycled to reduce operating costs and additional amounts of metals can be recovered during this recycling process. For example, base metals such as nickel, copper and cobalt can be recovered as sulphates in wash water from final wastes and can be recycled along with sulfuric acid to sulphate streams earlier in the process. The recovered sulfate acid solutions can be recycled back to sulfate streams from a Kell Process primary base metal recovery loop as claimed in any one of WO99/60178, WO2014/009928, or Australian patent application 2013263848.
[164] Any gold, silver, PGMs or other minor fugitive value metals, if present, can similarly be recovered as chlorides in wash water from final wastes and can be recycled along with hydrochloric acid to previously untreated chloride streams. process or retrieved directly. For example, recovered hydrochloric acid solution can be recycled back to a chloride leach step or a chlorination step of a Process primary precious metal recovery loop as claimed in WO99/60178, WO2014/009928, or application Australian patent 2013263848.
[165] IX, chelation sorbent resins (eg, thiol, thiouronium, polyamide or others) fibers, carbons, biological materials or other materials are capable of recovering small amounts of gold, silver, PGMs or other minor fugitive value metals if present, from sterile sulfide precipitation, intermediate product upgrade liquids, or base metal PLS.
[166] Chlorination leaching requires the use of hydrochloric acid, which would benefit from recovery and recycling. Several results are obtained by a specific process of subjecting the sterile chloride flow from the chlorination bleach step to a pre-boil-rectify-boil again treatment (26) allowing recovery of strong hydrochloric acid, calcium removal and recovery of residual metal sulfate salts, such as copper, nickel, cobalt, rhodium, ruthenium, vanadium iridium, germanium, gallium or scandium, for recycling or recovery. Sterile chloride solution (after recovery of primary and absorbed precious metals and other fugitive elements) is subjected to metal and acid recovery by exploiting differences in solubility of metal sulfates under selected conditions. The sterile chloride solution is contacted with 70% sulfuric acid and is preheated in a pre-boil stage in which the volume of hydrochloric acid is boiled for recovery. Calcium is removed by precipitation of gypsum at this stage, with subsequent solid-liquid separation by thickening and filtration, generating residual solids for disposal. Part of the thickener underflow is recycled to the contactor as seed material.
[167] The low calcium solution is introduced part way down a distillation column while additional 60-80% sulfuric acid is introduced to the top of the column at a rate determined by the strength of recovered hydrochloric acid required. A steam heated reboiler or other means is used to heat the liquid at the bottom of the column to ~110-160°C, while the tops of the column are at ~95-1250°C. water remains largely unvolatilized, while remaining hydrochloric acid is almost completely volatilized.
[168] Vapors from the column and pre-boiler pass through a water-cooled absorber column where the hydrochloric acid is recovered by absorption into chlorination filter wash water, producing 25-40% hydrochloric acid suitable for use in primary chlorination bleach while directly reusing wash water.
[169] Dilute sulfuric acid (-35-65%) discharges from the bottom of the column and is passed into an evaporator to recover absorbed water for reuse, producing a -60-80% sulfuric acid which is subjected to a step of cooling and aging in storage tanks, where supersaturated metal sulfates crystallize and are harvested. The sulfuric acid and metals contained therein are recovered or reused by recycling them to the base metals recovery loop of the KellGold process for the pre-leach, pressure oxidation and/or atmospheric acid steps. The acid content is used in the primary base metal leach circuit, while the metal sulfates dissolve in that step and are recovered in the base metal circuit, thereby increasing the overall base metal recovery of the process by high values.
[170] Vapors from the evaporator pass into a water-cooled condenser where they are condensed into a liquid suitable for use as a second stage chlorination filter wash water. The concentrated sulfuric acid (•“60-80%) that is recovered is recycled to a sulfuric acid compounding tank where 98% sulfuric acid is added to make up the sulfate which is removed to filter cake and recycled to the base metal of the process. The composite sulfuric acid is then available for reuse in the pre-boil and pre-heater sections of the circuit.
[171] In an additional specific innovation described here the KellGold Process accumulates significant techno-economic benefits by integrating with a separate Kell Process plant for the recovery of PGMs and base stocks from concentrates. As illustrated in Figure 3, the use of common reagents, preparation, base metal recovery, precious metal recovery and HCI recycling units or parts thereof, considerably reduces the specific operating costs of both plants. In addition, the KellGold mill's key ability to accept and "toll" feeds from multiple sources of a variety of very different refractory, non-refractory and other problematic feed material types is considered a significant innovation. Locating such a toll treatment facility alongside another similar facility has clear benefits.
[172] A further example of the potential synergies through joint localization and integration is shown in Figure 4. Heap leaching of low grade copper ores in particular, as well as nickel/cobalt and other metals, is now considered relatively common. The acid produced in the KellGold process is used to drive the sulfate PLS into the heap leach and associated base metal recovery circuit, achieving lower capital and operating costs than as a stand-alone facility.
[173] Higher grade copper concentrates and ores typically contain gold, which is obtained as a smelter credit. Terms paid by smelter can be unfavorable for producers in remote locations and particularly smaller operations. The KellGold process can easily handle toll treatment of gold-copper concentrates, thereby providing a potentially attractive option for such operations to achieve higher metal recoveries and financial returns. Extraction of precious, basic and rare elements from refractory or intractable materials of different types.
[174] The following examples are provided to demonstrate the effectiveness of the process described here, which have been brought to bear on the recovery and separation of precious metals such as gold and silver, as well as base and/or rare metals from a variety of refractory materials or otherwise intractable or conventionally untreatable, resulting in potentially economical recovery and/or separation of multiple valuable elements and possible reuse or regeneration of reagents, and where removal of most sulfur and base metals in the first stage of the process facilitates immediate removal of remaining precious and base metals in the second stage of the process.
[175] These examples, however, are not to be interpreted as limiting the spirit or scope of the invention in any way. EXAMPLES
[176] In the first of the following examples, tests are performed on a range of material types to primarily demonstrate the superior extractability of valuable elements using the chlorination leach medium as preferred in the process described, compared to the ability of lower extraction of value elements using the cyanidation leach medium as typically used conventionally. In all these cases a conventional cyanide bleach bottle roll (BLEG) test was performed using conditions considered standard in the industry.
[177] In the following examples, a complete KellGold test was performed on a ground sample of each material, covering pressure oxidation for base metal extraction, and chlorination liquor for precious metal extraction such as Au and Ag. EXAMPLE 1 Extraction of precious and base metals from various feed stocks
[178] In this example, seven samples of concentrates containing selected refractory gold and process products were obtained for testing, covering a range of precious metal types, copper, sulfur and organic carbon contents as well as degree of refractive capacity for leaching of conventional cyanidation. The main tests are summarized in table 1, while the cyanide and chloride extraction capacities are summarized in table 2. Table 1 - main tests for refractory carbonaceous sulphide ore, concentrates and residues

[17 9] Indicative percentages of cyanide extractable and chloride extractable Au, Ag and Cu for the seven feed stocks under consideration are summarized in table 2. This example provides a preliminary level of testing, where the results are indicative only of suitability potential of the material for processing with KellGold. The cyanide soluble results are from single standard small scale cyanide leach (BLEG) tests under excess cyanide and lime conditions that were not subjected to balanced and monitored leaching and collection of kinetic data and reagent consumption. Chloride extractable results are from single standard small scale aqua regia leach tests under excess reagent conditions that were not subjected to balanced leaching and monitored with kinetic data collection. Table 2 - summary of KellGold recoveries from refractory sulfide ore, concentrates and residues
*anomalous main test (-0.2 g/t Ag); #anomalous main test (suspected Hg interference); X - unrehearsed
[1801 The samples show a range of cyanide extraction capacities, with all seven samples being classified as refractory using the La Brooy3 definition of <90% gold extraction capacity by cyanidation (ranging from 3-28%). Silver and copper extraction capacities by cyanidation are also generally low and by chlorination they are generally high. EXAMPLE 2 Recovery of Precious and Base Metals from Refractory Gold Arsenopyrite Concentrate
[181] In this example, a refractory gold arsenopyrite concentrate was studied, and the main test is summarized in table 3. Approximately 2 kg of mixed concentrate without additional grinding or other pretreatment was loaded into a 15 L autoclave and subjected to to pressure oxidation with oxygen injection for 60 minutes. Pressure was then released using a letdown flash system with slurry subsequently held in a further stirred tank prior to solid-liquid separation by pressure filtration. The filter cake was dried and divided for analysis and a portion (-0.5 kg) was slurried with a hydrochloric acid solution and subjected to chlorination in two stages with interstage filtration. The final residue was again subjected to chemical analysis to determine leach efficiencies of value elements. KellGold recoveries are summarized in Table 4, showing recoveries in excess of 98% for Au, Ag and Cu. Copper is typically recoverable from solution by conventional means such as solvent extraction, electrolytic extraction, ion exchange or precipitation. From the solid residue, from which reagent-consuming species are largely removed, Au and Ag can be obtained in the high recoveries demonstrated in the chlorination stage, along with remaining Cu.
EXAMPLE 3 Recovery of Precious and Base Metals from Refractory Gold Pyrite Concentrate
[182] In this example, a refractory gold concentrate was studied, and the main test is summarized in table 5. Approximately 2 kg of mixed concentrate without additional grinding or other pretreatment was loaded into a 15 L autoclave and subjected to oxidation by pressure with oxygen injection for 60 minutes. Pressure was then released using a letdown flash system with slurry subsequently held in a further stirred tank prior to solid-liquid separation by pressure filtration. The filter cake was dried and divided for analysis and a portion (~0.5 kg) was slurried with a hydrochloric acid solution and subjected to chlorination in two stages with interstage filtration. The final residue was again subjected to chemical analysis to determine leach efficiencies of value elements. KellGold recoveries are summarized in table 6, showing recoveries in excess of 95% for Au, Ni, Cu and Co. Base metals Ni, Cu and Co are typically recoverable from solution by conventional means such as solvent extraction, extraction electrolytics, ion exchange or precipitation. From the solid residue, from which reagent-consuming species are largely removed, Au and Ag are obtained in the high recoveries demonstrated in the chlorination stage, along with remaining Ni, Cu and Co. Table 5 - main tests of refractory gold pyrite concentrate
EXAMPLE 4 Recovery of Precious and Base Metals from Refractory Polymetallic Sulphide Concentrate
[183] In this example, a refractory polymetallic Au-Ag-Cu-Zn-Pb concentrate was studied, and the main test is summarized in table 7. Approximately 2 kg of mixed concentrate without further grinding or other pretreatment was loaded into a 15 L autoclave and subjected to pressure oxidation with oxygen injection for 60 minutes. Pressure was then released using a letdown flash system with slurry subsequently held in a further stirred tank prior to solid-liquid separation by pressure filtration. The filter cake was dried and divided for analysis and a portion (-0.5 kg) was slurried with a hydrochloric acid solution and subjected to chlorination in two stages with interstage filtration. The final residue was again subjected to chemical analysis to determine leach efficiencies of value elements. KellGold recoveries are summarized in table 8, showing recoveries in excess of 98% for Au, Ag, Cu, Zn and Pb. Base metals Cu and Zn are typically recoverable from solution by conventional means such as solvent extraction, extraction electrolytics, ion exchange or precipitation. From the solid residue, from which reagent-consuming species are largely removed, Au and Ag as well as Pb are obtained in the high recoveries in the chlorination stage, along with the remaining Cu and Zn.

REFERENCES 1. Liddell, KS and Adams, MD Kell hydrometallurgical process for extraction of platinum group metals and base metals from flotation concentrates, JS Afr. Inst. Min. Metall. Trans., vol. 112, January 2012, p. 31-36. 2. La Brooy, SR, Linge, HG and Walker, GS 1994. Review of gold extraction from ores. Minerals Engineering, vol. 7, no. 10, p. 1213-1241. 3. Liddell, KS, Newton, T., Adams, MD and Muller, B. Energy consumptions in Kell hydrometallurgical refining versus conventional pyrometallurgical smelting of PGM concentrates, JS Afr. Inst. Min. Metall. Trans., vol. Ill, February 2011, p. 127-132.

权利要求:
Claims (5)
[0001]
1. Hydrometallurgical process to extract gold or silver or both and optionally one or more additional elements, such as base elements, rare metals and/or rare elements, from a refractory or intractable feed material, the process being characterized by the fact that it consists of the steps of: (i) supplying the feed material to a reaction vessel; and (ii) subjecting the feed material to one or more of the following and associated leaching steps: a) a hot sulfuric acid leaching step under pressure and/or atmospheric conditions to produce a product slurry comprising salable metal sulfates in solution and a solid residue containing salable metals; b) subjecting the pulp from a) to a conditioning step comprising sulfuric acid of 25 - 300 g/l, or alkaline treatment at a pH value of 10 - 14; c) separating the solid residue containing salable metals from the salable metal sulphates in solution from the product slurry of step b) to generate a separated solid residue; d) subjecting the solid residue separated from step c) above to a step of chloride leaching in a chloride leaching medium to produce salable metals soluble in a chlorine-filled lye solution (PLS) of chloride and an intermediate solid residue, and when the chloride leach medium contains iron chloride, the chloride PLS is treated with an additional step of pressure, precipitation or crystallization, concentration by evaporation, reverse osmosis, nanofiltration or other membrane technology, solvent extraction, or treatment by washing/rectifying, and/or pyrolysis to produce an iron-bearing product; e) subjecting the chloride PLS from step d) above to one or more techniques such as ion exchange (IX), chelation, molecular recognition technology (MRT), addition of polymeric or other sorbents, solvent extraction, precipitation using hydroxides , ammonia, carbonates or sulfides, electrolytic extraction and/or reduction to produce one or more solution products or intermediate solids for the recovery of gold and silver, as well as any rare or base metals salable in the chloride PLS. f) subjecting the intermediate solution product of step e) above to the recovery of hydrochloric acid, calcium and residual metals, by means of one or more steps such as pre-boiling, rectification, distillation, adsorption, reflashing, and/or pyrohydrolysis , to provide a product slurry comprising a solid residue containing salable metals and salable metal sulfates in solution, and when the chloride leach medium contains iron chloride, the chloride PLS is treated with an additional step of pressure, precipitation or crystallization, concentration by evaporation, reverse osmosis, nanofiltration or other membrane technology, solvent extraction, or washing/rectification treatment, and/or pyrolysis to produce an iron-bearing product; g) subjecting the solid residue from step f) above to a step of chloride releaching in a chloride leach medium to produce salable metals soluble in a purified chloride PLS, and when the chloride leaching medium contains chloride iron, chloride PLS is treated with an additional step of pressure, precipitation or crystallization, concentration by evaporation, reverse osmosis, nanofiltration or other membrane technology, solvent extraction, or washing/rectification, and/or pyrolysis treatment for produce a product bearing iron; h) recovering the gold and silver, as well as any other rare or base metals from the intermediate solid or solution products of steps e), f) or g) above, wherein the process optionally includes subjecting the feed material to any one or more of the following optional or associated additional leaching steps: i) subjecting the intermediate solid or solution product of step e) to an additional purification and/or upgrade step comprising one or more techniques such as IX, chelator, MRT , addition of polymeric or other sorbents; solvent extraction, precipitation using hydroxides, ammonia, carbonates or sulfides, electroforming and/or reduction; j) subjecting the discharge solution from step e), f) or g) to a sorption step in which salable PMs, such as gold and silver, are adsorbed onto one or more resins, such as an IX resin, or a sorbent and metals Bases are discharged into a solution, followed by eluting the adsorbed salable metals, such as gold and silver, from resin IX or sorbent and precipitating the gold and silver from the eluate using a reductant or directly incinerating the loaded resin or sorbent to produce a concentrate of high-grade metal or single-value metal products, or whereby salable gold and/or silver are subjected to an additional sulfide precipitation step to produce a second product slurry, followed by solid-liquid separation from a residue secondary solid from the second product slurry for further purification by a method as described in step e) or direct sale to third parties; k) subjecting the chloride PLS from step g) to one or more techniques such as IX, chelating, MRT, addition of polymeric or other sorbents, solvent extraction, precipitation using hydroxides, ammonia, carbonates or sulfides, electroforming and/or reduction to produce one or more intermediate solids or solution products for the recovery of gold and silver, as well as any other valuable rare or base metals in the chloride PLS; l) separate the solid residue containing salable metals from the salable metal sulphates in slurry solution of the product of steps f), g), i), j) or k) and then supply the resulting separated solid residue to step b) or d); m) recover salable metals from metal sulfates in solution from the intermediate product upgrade in step i) through techniques such as solvent extraction, IX, precipitation using hydroxides, ammonia, carbonates or sulfides, electroforming, reduction and/or recycling.
[0002]
2. Process according to claim 1, characterized in that step f) of separation and recovery of hydrochloric acid, calcium and residual base metal comprises: A) feeding the discharge solution of step e) into an evaporator pre-boiling together with seed gypsum to generate a precipitate of gaseous hydrochloric acid and gypsum, followed by solid-liquid separation to produce precipitated gypsum for recovery and a treated discharge solution; B) (aa) feed the discharge solution from step A) to a sulfuric acid rectification column or reboiler together with sulfuric acid to generate a hydrochloric acid gas and a sulfuric acid solution comprising salable base and/or rare metals and/or recoverables such as copper, nickel, cobalt, rhodium, ruthenium, iridium, vanadium, germanium, gallium or scandium; or (bb) feed the discharge solution from step A) to a pyrohydrolysis reactor to produce a slurry comprising a solid iron oxide residue for recovery and a base and/or rare metals solution, followed by solid-liquid separation ; C) subjecting the sulfuric acid solution generated in step B)(aa) or the base metal and/or rare metals solution from step B(bb) to a cooling and aging step, in which the metal sulfate salts are crystallized or subjected to a sorption step and are recovered, such as by evaporation or precipitation and/or are recycled back into a Kell Core Process primary base metal recovery loop; and D) subjecting the hydrochloric acid gas from step A) or step B(bb) to distillation and absorption, thereby recovering a hydrochloric acid solution.
[0003]
3. Process according to any one of claims 1 or 2, characterized in that the chloride leaching medium has a pH between 2.5 and 7.5, maintained at a temperature in the range of 50-150 oC or a free acidity between 50 to 300 g/L of HCl maintained at a temperature in the range of 50-150 oC.
[0004]
4. Process according to any one of claims 1 to 3, characterized in that the chloride leaching step is carried out by leaching in an atmospheric autoclave or under pressure with saline brine under oxidizing conditions.
[0005]
5. Process according to any one of claims 1 to 4, characterized in that the process is integrated into an existing process, such as a Kell core process or a conventional leaching process for base metal recovery.

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EA034848B1|2020-03-27|

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US20160145714A1|2016-05-26|

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法律状态:
2017-02-14| B03A| Publication of a patent application or of a certificate of addition of invention [chapter 3.1 patent gazette]|

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2018-10-30| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|

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2019-08-06| B06U| Preliminary requirement: requests with searches performed by other patent offices: procedure suspended [chapter 6.21 patent gazette]|

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2021-04-27| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|

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2021-06-08| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 25/11/2015, OBSERVADAS AS CONDICOES LEGAIS. |

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2022-01-25| B16C| Correction of notification of the grant [chapter 16.3 patent gazette]|Free format text: REF. RPI 2631 DE 08/06/2021 QUANTO AO ENDERECO. |

优先权:

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申请号 | 申请日 | 专利标题

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ZA2014/08682|2014-11-26|

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ZA201408682|2014-11-26|

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