Classifications

• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
  • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
  • C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
  • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
  • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
  • C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P10/00—Technologies related to metal processing
  • Y02P10/20—Recycling
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
  • Y02W30/00—Technologies for solid waste management
  • Y02W30/50—Reuse, recycling or recovery technologies
  • Y02W30/84—Recycling of batteries or fuel cells

Definitions

• the invention relates to the use of a biosourced isoparaffinic fluid as a diluent for the liquid-liquid extraction of metals, in particular implemented in a hydrometallurgical battery recycling process.
• the invention also relates to a hydrometallurgy process comprising at least one liquid-liquid extraction step and at least one step of recovering at least one metal.
• this diluent is a hydrocarbon solvent resulting from refining, often a kerosene or a dearomatized aliphatic product.
• the use of such a diluent in the battery recycling process results in the use of non-renewable material, which is antithetical to the objective of reducing the impact on the environment.
• the hydrocarbon fluid comprises, relative to the total weight of the hydrocarbon fluid: at least 80% by weight of isoparaffins, preferably at least 90% by weight, more preferably at least 95% by weight, and /or at most 20% by weight of normal paraffins, preferably at most 10% by weight, more preferably at most 5% by weight, and/or at most 1% by weight of naphthenes, and/or less than 50 ppm by weight of aromatics.
• the hydrocarbon fluid comprises, relative to the total weight of the hydrocarbon fluid: from 30 to 60% by weight of C15 isoparaffins and from 30 to 60% by weight of C16 isoparaffins, or from 5 15% by weight of C15 isoparaffins, 30 to 60% by weight of C16 isoparaffins, 10 to 30% by weight of C17 isoparaffins, and 10 to 30% by weight of C18 isoparaffins , Or from 10 to 30% by weight of C17 isoparaffins and from 60 to 90% by weight of C18 isoparaffins.
• the hydrocarbon fluid according to the invention has a flash point ranging from 80°C to 95°C (ASTM D93) and comprises, relative to the total weight of the hydrocarbon fluid: from 0.5 to 15% in weight of isoparaffins having less than 13 carbon atoms, from 5 to 25% by weight of C13 isoparaffins, and from 5 to 30% by weight of C14 isoparaffins, and from 5 to 30% by weight of isoparaffins in C15, and from 25 to 50% by weight of C16 isoparaffins, and from 10 to 25% by weight of isoparaffins having more than 16 carbon atoms, relative to the total weight of the hydrocarbon fluid, preferably, said fluid comprises 75 to 90% by weight of isoparaffins and 10 to 25% by weight of n-paraffins, relative to the total weight of the fluid.
• the fluid is used as a diluent in a hydrometallurgical process comprising at least one liquid-liquid extraction of metals using an extraction solution comprising said diluent and at least one extractant.
• the metals come from the recycling of one or more batteries.
• the invention also relates to a hydrometallurgical process for recycling batteries, said process comprising: a step of dissolving the metals present in at least one battery, in particular in the electrodes of said at least one battery, making it possible to obtain a solution of metals M, possibly a clarification step implemented on said solution of metals M making it possible to eliminate residues not dissolved in the metal solution, a liquid-liquid extraction process for metals according to the invention.
• the hydrocarbon fluid according to the invention has a low density, in particular a lower density than hydrocarbon solvents of petroleum (fossil) origin, which makes it particularly efficient for its use as a diluent for the liquid-liquid extraction of metals. .
• hydrocarbon fluid defined in the present invention presented a diluent/extraction couple having good extractability for metals including in particular excellent selectivity towards the metals of interest.
• the invention relates to a use of a hydrocarbon fluid as a diluent for the liquid-liquid extraction of metals in particular in a hydrometallurgical process, said hydrocarbon fluid comprising at least 75% by weight of isoparaffins and less than 100 ppm by weight of aromatics, relative to the total weight of the hydrocarbon fluid, said hydrocarbon fluid having a biodegradability of at least 60% at 28 days, measured according to the OECD 301 B standard.
• the present invention also relates to a process for liquid-liquid extraction of metals comprising at least one step of bringing a solution of metals M into contact with an extraction solvent, said extraction solvent comprising at least one diluent and at least one extractant, said diluent being a hydrocarbon fluid comprising at least 75% by weight of isoparaffins and less than 100 ppm by weight of aromatics, relative to the total weight of the hydrocarbon fluid, said hydrocarbon fluid having a biodegradability of at least 60% at 28 days, measured according to OECD standard 301 B.
• a clarification step implemented on said metal solution M making it possible to eliminate residues not dissolved in the metal solution
• a step of liquid-liquid extraction of metals comprising at least one step of bringing the metal solution M into contact with an extraction solvent, said extraction solvent comprising at least one diluent and at least one extractant, said diluent being a hydrocarbon fluid comprising at least 75% by weight of isoparaffins and less than 100 ppm by weight of aromatics, relative to the total weight of the hydrocarbon fluid, said hydrocarbon fluid having a biodegradability of at least 60% at 28 days, measured according to OECD 301 B standard.
• the hydrocarbon fluid used in the invention is typically of biosourced origin.
• isoparaffins designates non-cyclic branched alkanes.
• the hydrocarbon fluid used according to the invention has an isoparaffin to normal paraffin mass ratio of at least 4:1, preferably at least 9:1, more preferably at least 12:1, preferably at least 15:1, or even at least 19:1.
• the hydrocarbon fluid used according to the invention comprises, relative to the total weight of the hydrocarbon fluid, a content by weight of naphthenic compounds less than or equal to 1%, preferably less than or equal to 0.5% and more preferably less than or equal to 100ppm.
• the hydrocarbon fluid used according to the invention comprises at least 80% by weight of isoparaffins, less than 20% by weight of n-paraffins, less than 1% by weight of naphthenes and less than 100 ppm by weight of aromatics, relative to the total weight of the hydrocarbon fluid and has a biogenic carbon content of at least 90% by weight relative to the total weight of the carbon atoms of the hydrocarbon fluid.
• the hydrocarbon fluid used according to the invention has a flash point ranging from 80°C to 105°C according to the ASTM D93 standard.
• the inventors have in fact observed that this flash point range made it possible to further improve the performance of the diluent in the context of liquid-liquid extraction and in particular for the recycling of batteries.
• the hydrocarbon fluid used according to the invention also preferably has a vapor pressure at 20°C less than or equal to 0.01 kPa.
• the hydrocarbon fluid used according to the invention has a flash point greater than or equal to greater than or equal to 120°C and a vapor pressure at 20°C less than or equal to 0.01 kPa.
• the hydrocarbon fluid used according to the invention has an initial boiling point and a final boiling point in the range from 200 to 400°C, preferably from 240 to 350°C, more preferably from 250 to 340°C.
• Boiling points can be determined according to ASTM D86.
• the difference between the final boiling point and the initial boiling point ranges from 10°C to 80°C, preferably from 20°C to 50°C.
• the hydrocarbon fluid used according to the invention comprises at least 80% by weight of isoparaffins, less than 1% by weight of naphthenes and less than 100 ppm by weight of aromatics, and has a point initial boiling point and a final boiling point in the range from 200 to 400°C.
• the hydrocarbon fluid used according to the invention comprises at least 95% by weight of isoparaffins and less than 100 ppm by weight of aromatics, and has an initial boiling point and a final boiling in the range from 200 to 400°C.
• the hydrocarbon fluid used according to the invention comprises at least 80% by weight of isoparaffins and less than 100 ppm by weight of aromatics, and has an initial boiling point and a final boiling point in the range from 250 to 340°C, the difference between the final boiling point and the initial boiling point ranging from 10°C to 80°C.
• the hydrocarbon fluid used according to the invention comprises at least 95% by weight of isoparaffins and less than 100 ppm by weight of aromatics, and has an initial boiling point and a final boiling point in the range from 250 to 340°C, the difference between the final boiling point and the initial boiling point ranging from 10°C to 80°C.
• the hydrocarbon fluid used according to the invention comprises at least 95% by weight of isoparaffins and less than 100 ppm by weight of aromatics, and has an initial boiling point and a final boiling point in the range from 250 to 340°C, the difference between the final boiling point and the initial boiling point ranging from 20°C to 50°C.
• the hydrocarbon fluid used according to the invention comprises, relative to the total weight of the hydrocarbon fluid: from 20 to 80% by weight of C15 isoparaffins and from 20 to 80% by weight of isoparaffins in C16, said fluid then being able to comprise isoparaffins comprising 14 carbon atoms or less and/or isoparaffins comprising 17 carbon atoms or more; or from 3 to 20% by weight of C15 isoparaffins, from 20 to 70% by weight of C16 isoparaffins, from 5 to 40% by weight of C17 isoparaffins, and from 5 to 40% by weight of C18 isoparaffins, said fluid possibly comprising isoparaffins comprising 14 carbon atoms or less and/or isoparaffins comprising 19 carbon atoms or more; or from 5 to 40% by weight of C17 isoparaffins and from 60 to 95% by weight of C18 isoparaffins, said fluid possibly comprising isoparaffins comprising 16 carbon atoms or less and/or iso
• the hydrocarbon fluid used according to the invention has an initial boiling point and a final boiling point in the range from 240 to 300°C and comprises from 5 to 15% by weight of C15 isoparaffins, from 30 to 60% by weight of C16 isoparaffins, from 10 to 30% by weight of C17 isoparaffins, and from 10 to 30% by weight of C18 isoparaffins and has an aromatic content less than 100 ppm by weight, relative to the total weight of the hydrocarbon fluid.
• the hydrocarbon fluid used according to the invention has a biodegradability of at least 60% at 28 days, measured according to the OECD 301 B standard.
• the hydrocarbon fluid according to the invention will be said to be “easily biodegradable” or " readily biodegradable” in English.
• the hydrocarbon fluid used according to the invention has a biodegradability of at least 60% at 28 days, measured according to OECD standard 306.
• OECD standard 306 is more restrictive than OECD standard 301 B.
• the hydrocarbon fluid used according to the invention comprises at least 80% by weight of isoparaffins and less than 100 ppm by weight of aromatics, and has an initial boiling point and a final boiling point in the range from 200 to 400°C, said hydrocarbon fluid having a biodegradability of at least 60% at 28 days, measured according to the OECD 301 B standard.
• the hydrocarbon fluid used according to the invention comprises at least 95% by weight of isoparaffins and less than 100 ppm by weight of aromatics, and has an initial boiling point and a final boiling point in the range from 200 to 400°C, said hydrocarbon fluid having a biodegradability of at least 60% at 28 days, measured according to the OECD 301 B standard.
• the hydrocarbon fluid used according to the invention comprises at least 95% by weight of isoparaffins and less than 100 ppm by weight of aromatics, and has an initial boiling point and a final boiling point in the range from 250 to 340°C, said hydrocarbon fluid having a biodegradability of at least 60% at 28 days, measured according to the OECD 301 B standard.
• the hydrocarbon fluid used according to the invention comprises at least 95% by weight of isoparaffins and less than 100 ppm by weight of aromatics, and has an initial boiling point and a final boiling point in the range from 250 to 340°C, the difference between the final boiling point and the initial boiling point ranging from 20°C to 50°C, said hydrocarbon fluid having a biodegradability of at minus 60% at 28 days, measured according to OECD standard 301 B.
• the hydrocarbon fluid used according to the invention comprises from 5 to 15% by weight of C15 isoparaffins, from 30 to 60% by weight of C16 isoparaffins, from 10 to 30% by weight of C17 isoparaffins, and from 10 to 30% by weight of C18 isoparaffins and has an aromatic content of less than 100 ppm by weight, relative to the total weight of the hydrocarbon fluid, said hydrocarbon fluid having a biodegradability of at minus 60% at 28 days, measured according to OECD standard 301 B.
• the hydrocarbon fluid used according to the invention comprises from 10 to 30% by weight of C17 isoparaffins and from 60 to 90% by weight of C18 isoparaffins and has an aromatic content of less than 100 ppm by weight, relative to the total weight of the hydrocarbon fluid, said hydrocarbon fluid having a biodegradability of at least 60% at 28 days, measured according to the OECD 301 B standard.
• the hydrocarbon fluid used according to the invention comprises from 10 to 30% by weight of C17 isoparaffins and from 60 to 90% by weight of C18 isoparaffins and has an aromatic content of less than 50 ppm by weight, relative to the total weight of the hydrocarbon fluid, said hydrocarbon fluid having a biodegradability of at least 60% at 28 days, measured according to the OECD 301 B standard.
• biomass conversion we mean a hydrocarbon cut produced from raw materials of biological origin.
• Raw materials of organic origin can be chosen from vegetable oils, animal fats, fish oils and their mixtures.
• the raw material of biological origin is an ester or a triglyceride derivative.
• This material is first subjected to a hydrodeoxygenation (H DO) step to decompose the structure of the constituent esters or triglycerides and eliminate the oxygenated, phosphorous and sulfur compounds concomitantly with the hydrogenation of the olefinic bonds.
• HDO hydrodeoxygenation
• the hydrogen and the raw material of biological origin are passed through a catalytic hydrodeoxygenation bed simultaneously or against the current.
• the pressure and temperature are between 20 and 150 bars and between 200 and 500°C respectively.
• Conventional and known hydrodeoxygenation catalysts are used during this step.
• the raw material of biological origin can be subjected to pre-hydrogenation under mild conditions to avoid secondary reactions of double bonds before the HDO step.
• the product resulting from the reaction is subjected to an isomerization step (ISO) where the hydrogen and the product, and optionally a mixture of n-paraffins, are passed over catalytic isomerization beds of simultaneously or against the flow.
• ISO isomerization step
• the pressure and temperature are between 20 and 150 bars and between 200 and 500°C respectively.
• Conventional and known isomerization catalysts are used during this step.
• the product resulting from the HDO/ISO steps can possibly be split in order to obtain the cuts of interest.
• Patent application EP2084245 describes a process for producing a hydrocarbon mixture which can be used as diesel or in a diesel composition by hydrodeoxygenation of a mixture of biological origin containing esters of fatty acids optionally mixed with free fatty acids, for example vegetable oils such as sunflower oil, rapeseed oil, oil canola, palm oil or pine oil, followed by hydroisomerization on specific catalysts.
• Patent application EP2368967 describes such a process and the product obtained by this process.
• the deoxygenated and isomerized feedstock resulting from the HDO/ISO process is then hydrogenated, after having possibly been fractionated in order to obtain a desired boiling range.
• the hydrogen used in the hydrogenation unit is typically highly purified hydrogen.
• highly purified we mean hydrogen with a purity, for example, greater than 99%, although other grades can also be used.
• a preferred catalyst is a nickel-based catalyst on an alumina support whose specific surface area preferably varies from 100 to 200 m 2 /g of catalyst or a nickel-based mass catalyst.
• the hydrogenation conditions are typically as follows:
• Pressure 50 to 160 bars, preferably 80 to 150 bars and more preferably 90 to 120 bars;
• WH Hourly volume velocity
• - Hydrogen treatment rate adapted to the conditions mentioned above and up to 200 Nm3/tons of load to be treated.
• the temperature in the reactors is typically between 150 and 160°C with a pressure of approximately 100 bars while the hourly volume velocity is approximately 0.6 hr-1 with a treatment rate adapted according to the quality of the feed. to be processed and the parameters of the first hydrogenation reactor.
• Hydrogenation can take place in one or more reactors in series.
• the reactors may include one or more catalytic beds.
• Catalytic beds are generally fixed catalytic beds.
• the hydrogenation process preferably comprises two or three reactors, preferably three reactors and is more preferably carried out in three reactors in series.
• the first reactor allows the trapping of sulfur compounds and the hydrogenation of essentially all unsaturated compounds and up to approximately 90% by weight of aromatic compounds.
• the product from the first reactor does not contain substantially any sulfur compounds.
• the hydrogenation of the aromatics continues and up to 99% by weight of the aromatics are therefore hydrogenated.
• the third stage in the third reactor is a finishing stage making it possible to obtain aromatic contents of less than 100 ppm, preferably less than 50 ppm, preferably less than 20 ppm.
• the catalysts may be present in varying or essentially equal amounts in each reactor; for three reactors, the quantities according to weight can for example be 0.05-0.5/0.10-0.70/0.25-0.85, preferably 0.07-0.25/0 .15-0.35/0.4-0.78 and more preferably 0.10-0.20/0.20-0.32/0.48-0.70.
• the first reactor is composed of twin reactors implemented in alternative ways. This mode of operability allows in particular easier loading and unloading of the catalysts: when the first reactor includes the saturated catalyst first (substantially all the sulfur is trapped on and/or in the catalyst) it must be changed often.
• a single reactor can also be used in which two, three or more catalyst beds are installed.
• the hydrocarbon fluid used according to the invention ideally comes from the treatment of raw materials of biological origin.
• biogenic carbon or “bio-carbon” indicates that the carbon is of natural origin and comes from a biomaterial, as indicated below.
• Bio-carbon content, biogenic carbon content and biomaterial content are expressions indicating the same value.
• a material of renewable origin or biomaterial is an organic material in which the carbon comes from CO2 recently fixed (on a human scale) by photosynthesis from the atmosphere.
• a biomaterial (100% natural carbon) has a 14 C/ 12 C isotopic ratio greater than 10'12 , typically around 1.2 x 10 -12 , while a fossil material has a zero ratio.
• Antioxidant additives act in particular as free radical inhibitors or hydroperoxide destroyers.
• antioxidant additives we can cite phenolic-type antioxidant additives, amine-type antioxidant additives, phosphosulfur-containing antioxidant additives. Some of these antioxidant additives, for example phosphosulfur antioxidant additives, can generate ash. Phenolic antioxidant additives can be ash-free or in the form of neutral or basic metal salts.
• the antioxidant additives may in particular be chosen from sterically hindered phenols, sterically hindered phenol esters and sterically hindered phenols comprising a thioether bridge, diphenylamines, diphenylamines substituted by at least one C1-C12 alkyl group, and their mixture.
• the sterically hindered phenols are chosen from compounds comprising a phenol group of which at least one vicinal carbon of the carbon carrying the alcohol function is substituted by at least one alkyl group in C-CIO, preferably an alkyl group in C1-C6, preferably a C4 alkyl group, preferably the tert-butyl group.
• Amino compounds are another class of antioxidant additives that can be used, possibly in combination with phenolic antioxidant additives.
• Examples of amino compounds are aromatic amines, for example aromatic amines of formula NR4R5R6 in which R4 represents an aliphatic group or an aromatic group, optionally substituted, R5 represents an aromatic group, optionally substituted, R6 represents a hydrogen atom, an alkyl group, an aryl group or a group of formula R7S(O)zR8 in which R7 represents an alkylene group or an alkenylene group, R8 represents an alkyl group, an alkenyl group or an aryl group and z represents 0, 1 or 2 .
• Sulfurized alkyl phenols or their alkali and alkaline earth metal salts can also be used as antioxidant additives.
• antioxidant additives are that of copper compounds, for example copper thio- or dithio-phosphates, copper salts and carboxylic acids, dithiocarbamates, sulphonates, phenates, copper acetylacetonates. Copper I and II salts, succinic acid or anhydride salts can also be used.
• copper compounds for example copper thio- or dithio-phosphates, copper salts and carboxylic acids, dithiocarbamates, sulphonates, phenates, copper acetylacetonates.
• Copper I and II salts, succinic acid or anhydride salts can also be used.
• the antioxidant(s) preferably represent 0.01 to 3% by weight of the weight of the composition, preferably 0.05 to 2% by weight of the weight of the diluent.
• the hydrocarbon fluid is used as a diluent for the liquid-liquid extraction of metals.
• the fluid hydrocarbon defined in the invention can be used as a diluent in a hydrometallurgical process comprising at least one step of liquid-liquid extraction of metals.
• the metal solution M typically comprises at least two different metals and the liquid-liquid extraction of metals will make it possible to recover at least one metal from the metal solution M, preferably at least two metals separately.
• Said metals can for example be chosen from nickel, copper, cadmium, cobalt, manganese, lithium, zinc, their mixtures including alloys of these metals.
• the metals in solution M may be in the form of metal oxide and/or metal hydroxide.
• the extractant can be chosen by those skilled in the art depending on the metals present in the metal solution M.
• alkyl groups the alkyls preferably having from 1 to 24 carbon atoms, preferably from 4 to 18 carbon atoms.
• the metal solution M can for example come from a step of dissolving metals from electric batteries, in particular from the electrodes of electric batteries.
• the present invention also relates to a hydrometallurgical process for recycling one or more batteries, said process comprising: a step of dissolving the metals present in at least one battery, in particular in the electrodes of said at least one battery, making it possible to obtain a solution of metals M, possibly a clarification step implemented on said solution of metals M making it possible to eliminate the residues not dissolved in the solution of metals, a step of liquid-liquid extraction of metals comprising at at least one step of bringing the metal solution M, optionally clarified, into contact with an extraction solvent, said extraction solvent comprising at least one diluent and at least one extractant, said diluent being a hydrocarbon fluid comprising at least 75 % by weight of isoparaffins and less than 100 ppm by weight of aromatics, relative to the total weight of the hydrocarbon fluid, said hydrocarbon fluid having a biodegradability of at least 60% at 28 days, measured according to the OECD 301 B standard.
• the process is implemented on Lithium-ion batteries.
• the solution of metals M will generally include at least two metals of different nature.
• the process hydrometallurgy will then make it possible to separately recover said at least two metals of different nature.
• the metals present in the metal solution M can for example be chosen from nickel, copper, cadmium, cobalt, manganese, lithium, zinc, their mixtures including alloys of these metals.
• a solution L making it possible to dissolve the metals present, in particular the metals intended to be recovered, will be chosen.
• the solution L for dissolution could for example be chosen from acids, bases, oxidants or reducing agents.
• the hydrometallurgy process according to the invention may possibly include a clarification step making it possible to eliminate the solid residues which would be present in the solution of metals M.
• This possible clarification step can possibly be implemented by decantation and/or centrifugation and/or filtration.
• the hydrometallurgy process according to the invention comprises a step of liquid-liquid extraction of metals comprising at least one step of bringing the metal solution M into contact, after a possible clarification step, with an extraction solvent.
• the extraction solvent comprises at least one diluent and at least one extractant.
• Said diluent is the hydrocarbon fluid defined in the present invention.
• the extractant can be chosen by those skilled in the art depending on the metals present in the metal solution M.
• the extractant will be miscible with the hydrocarbon fluid.
• the extractant is chosen from oximes comprising one or two alkyl groups and phosphorous acids optionally comprising one or more alkyl groups, the alkyls preferably having from 1 to 24 carbon atoms, preferably from 4 to 18 carbon atoms, preferably from ketoximes having an alkyl group, phosphinite acids optionally comprising one or more alkyl groups, the alkyls preferably having from 1 to 24 carbon atoms, preferably from 4 to 18 carbon atoms.
• the extractants we can cite the extractants from the Cyanex® range from Solvay or the extractants from the LIX® range from BASF.
• the process according to the invention may comprise at least one subsequent step of recovering at least one metal, preferably at least two metals of different nature.

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• 2022
  • 2022-09-07 FR FR2208962A patent/FR3139346A1/fr active Pending
• 2023
  • 2023-09-06 EP EP23767866.9A patent/EP4584404A1/de active Pending
  • 2023-09-06 KR KR1020257010632A patent/KR20250069567A/ko active Pending
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