Classifications

• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B21/00—Nitrogen; Compounds thereof
  • C01B21/082—Compounds containing nitrogen and non-metals and optionally metals
  • C01B21/087—Compounds containing nitrogen and non-metals and optionally metals containing one or more hydrogen atoms
  • C01B21/093—Compounds containing nitrogen and non-metals and optionally metals containing one or more hydrogen atoms containing also one or more sulfur atoms
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B21/00—Nitrogen; Compounds thereof
  • C01B21/082—Compounds containing nitrogen and non-metals and optionally metals
  • C01B21/086—Compounds containing nitrogen and non-metals and optionally metals containing one or more sulfur atoms
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C303/00—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides
  • C07C303/36—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of amides of sulfonic acids
  • C07C303/40—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of amides of sulfonic acids by reactions not involving the formation of sulfonamide groups
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
  • C07F1/00—Compounds containing elements of Groups 1 or 11 of the Periodic Table
  • C07F1/02—Lithium compounds
• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M10/00—Secondary cells; Manufacture thereof
  • H01M10/05—Accumulators with non-aqueous electrolyte
  • H01M10/052—Li-accumulators
• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M10/00—Secondary cells; Manufacture thereof
  • H01M10/05—Accumulators with non-aqueous electrolyte
  • H01M10/052—Li-accumulators
  • H01M10/0525—Rocking-chair batteries, i.e. batteries with lithium insertion or intercalation in both electrodes; Lithium-ion batteries
• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M10/00—Secondary cells; Manufacture thereof
  • H01M10/05—Accumulators with non-aqueous electrolyte
  • H01M10/056—Accumulators with non-aqueous electrolyte characterised by the materials used as electrolytes, e.g. mixed inorganic/organic electrolytes
  • H01M10/0564—Accumulators with non-aqueous electrolyte characterised by the materials used as electrolytes, e.g. mixed inorganic/organic electrolytes the electrolyte being constituted of organic materials only
  • H01M10/0566—Liquid materials
  • H01M10/0568—Liquid materials characterised by the solutes
• • 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
  • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
  • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
  • Y02E60/10—Energy storage using batteries

Definitions

• the present invention relates to a process for the preparation of imide salts containing a fluorosulfonyl group.
• Anions of sulfonylimide type by their very low basicity, are increasingly used in the field of energy storage in the form of inorganic salts in batteries, or organic salts in supercapacitors or in the field of liquids ionic.
• LiPF 6 LiPF 6
• this salt shows numerous disadvantages such as limited thermal stability, sensitivity to hydrolysis and therefore lower battery safety.
• new salts having the FSO 2 group have been studied and have demonstrated many advantages such as better ionic conductivity and resistance to hydrolysis.
• LiFSI LiN (FSO 2 ) 2
• LiFSI LiN (FSO 2 ) 2
• WO 2015/158979 describes in particular the preparation of LiFSI via a step of chlorination of sulfamic acid, with thionyl chloride and sulfuric acid, at atmospheric pressure (examples). However, after 24 hours at reflux of the thionyl chloride, the conversion of the sulfamic acid is not complete.
• the present invention relates to a process for preparing a compound of formula (IV) below:
• step a) being carried out:
• Step a) advantageously leads to a compound of formula (I):
• the compound (A) is that in which R 0 represents OH.
• the sulfur-containing agent may be selected from the group consisting of chlorosulfonic acid (CIS0 3 H), sulfuric acid, oleum, and mixtures thereof.
• the sulfur-containing agent is sulfuric acid or oleum, preferentially sulfuric acid.
• the chlorinating agent may be selected from the group consisting of thionyl chloride (SOCI 2 ), oxalyl chloride (COCI 2 ), phosphorus pentachloride (PCI 5 ), phosphonyl trichloride (PCI 3 ), phosphoryl trichloride (POCI 3 ), and mixtures thereof.
• the chlorinating agent is thionyl chloride.
• Step a) can be carried out in the presence of a catalyst, such as, for example, chosen from a tertiary amine (such as trimethylamine, triethylamine, or diethylmethylamine); pyridine; and 2,6-lutidine.
• a catalyst such as, for example, chosen from a tertiary amine (such as trimethylamine, triethylamine, or diethylmethylamine); pyridine; and 2,6-lutidine.
• the reaction is carried out in the absence of catalyst.
• the molar ratio between the sulfuric acid and the compound (A) may be between 0.7 and 5, preferably between 0.9 and 5.
• the molar ratio between the chlorinating agent and the compound (A) may be between 2 and 10, preferably between 2 and 5.
• the sulfur-containing agent is chlorosulphonic acid
• the sulfur-containing agent is sulfuric acid (or oleum)
• the molar ratio of sulfuric acid (or oleum) to the compound (A) is between 0.7 and 5.
• the sulfur-containing agent is sulfuric acid (or oleum)
• step a) is carried out at a temperature greater than or equal to 90 ° C, preferably greater than or equal to 100 ° C, preferably greater than or equal to 105 ° C, advantageously greater than or equal to 1 10 ° C C, still more preferably greater than or equal to 1 15 ° C, and in particular greater than or equal to 120 ° C.
• step a) is carried out at a temperature of between 105 ° C. and 130 ° C., preferably between 105 ° C. and 125 ° C., preferably between 10 ° C. and 125 ° C., advantageously between 1 ° C. and 125 ° C. ° C and 125 ° C, and more preferably between 1 18 ° C and 122 ° C, and in particular at 120 ° C.
• step a) is carried out at a pressure greater than or equal to 7.5 bar abs, preferably greater than or equal to 8 bar abs, more preferably greater than or equal to 9 bar abs, preferably greater than or equal to 8 bar abs. or equal to 10 bar abs, advantageously greater than or equal to 1 1 bar abs, even more advantageously greater than or equal to 12 bar abs, preferably greater than or equal to 13 bar abs, for example greater than or equal to 15 bar abs.
• the chlorination step a) may be carried out batchwise or semi-continuously.
• Step a) can be carried out in a reactor made of a material resistant to corrosion.
• Step a) can be carried out in a reactor comprising heating means.
• the reactor of step a) can be heated by means of a double jacket surrounding the reactor in which a heating fluid, for example steam, can circulate.
• a heating fluid for example steam
• hot water or a mixture of benzyltoluene and dibenzyltoluene (for example Jarrytherm BT06).
• the reactor pressure is regulated by a pressure regulating valve.
• a pressure regulating valve advantageously makes it possible to evacuate the gases formed and to maintain the pressure of the reactor at a given pressure.
• the setting of the pressure is advantageously independent of the temperature setting.
• Step a) advantageously makes it possible to provide the compound of formula (I) with a (quasi) total conversion to sulphonamide reagent (A) in a reduced time, preferably in less than 48 hours, advantageously in less than 24 hours. and preferably in less than 22 hours.
• Step a) also makes it possible to reduce the molar ratio between the volatile reactants and the compound (A), and in particular the molar ratio between the chlorinating agent and the compound (A). Indeed, when the pressure is carried out at atmospheric pressure in an open medium, the gas evolution of the reaction products causes a loss of volatile reactants during the reaction. Step a) advantageously makes it possible to limit this loss of reagents, and thus to reduce said molar ratio in the reaction.
• the process according to the invention advantageously makes it possible to prepare the compound of formula (IV) in a shorter time, and to reduce the molar ratio between the volatile reactants and the compound (A).
• step a) leads in particular to a gas evolution comprising HCl and SO 2 .
• the process according to the invention may comprise a step of treating said gas evolution, for example by distillation or by means of a membrane, preferably by distillation, for example in order to recover HCl and / or SO 2 .
• the process according to the invention advantageously makes it possible to facilitate the treatment of said gas evolution by distillation.
• step a) under the reaction conditions indicated above (temperature and pressure), advantageously makes it possible to condense HCl at a higher temperature than at atmospheric pressure in the condenser of the column. distillation.
• the process according to the invention may comprise a step b), subsequent to step a), said step b) comprising the reaction of the compound of formula (I) obtained in the preceding step with at least one fluorinating agent, optionally in the presence of at least one SOI organic solvent.
• Step b) advantageously allows the fluorination of the compound of formula (I) in a compound of formula (II):
• R 2 represents F, CF 3 , CHF 2 , or CH 2 F. It is particularly preferred that R 2 represents F.
• the fluorinating agent is chosen from the group consisting of HF (preferably anhydrous HF), KF, AsF 3 , BiF 3 , ZnF 2 , SnF 2 , PbF 2 , CuF 2 , and mixtures thereof. , the fluorinating agent preferably being HF, and even more preferably anhydrous HF.
• anhydrous HF means THF containing less than 500 ppm water, preferably less than 300 ppm water, preferably less than 200 ppm water.
• Step b) of the process is preferably carried out in at least one SOI organic solvent.
• the organic solvent SOI preferably has a donor number of between 1 and 70 and advantageously of between 5 and 65.
• the donor index of a solvent represents the value -DH, DH being the enthalpy of the interaction between the solvent and antimony pentachloride (according to the method described in Journal of Solution Chemistry, Vol.13, No. 9, 1984).
• organic solvent SOI there may be mentioned in particular esters, nitriles, dinitriles, ethers, diethers, amines, phosphines, and mixtures thereof.
• the organic solvent SOI is selected from the group consisting of methyl acetate, ethyl acetate, butyl acetate, acetonitrile, propionitrile, isobutyronitrile, glutaronitrile , dioxane, tetrahydrofuran, triethylamine, tripropylamine, diethylisopropylamine, pyridine, trimethylphosphine, triethylphosphine, diethylisopropylphosphine, and mixtures thereof.
• the organic solvent SOI is dioxane.
• Step b) can be carried out at a temperature of between 0 ° C. and the boiling temperature of the SOI organic solvent (or of the SOI organic solvent mixture).
• step b) is carried out at a temperature of between 5 ° C. and the boiling temperature of the organic solvent SOI (or the mixture of organic solvents SOI), preferably between 20 ° C. and the boiling temperature of SOI organic solvent (or SOI organic solvent mixture).
• Step b) preferably with anhydrous hydrofluoric acid, can be carried out at a pressure P, preferably between 0 and 16 bar abs.
• This step b) is preferably carried out by dissolving the compound of formula (I) in the organic solvent SOI, or the mixture of organic solvents SOI, prior to the reaction step with the fluorinating agent, preferably with Anhydrous GI-IF.
• the weight ratio between the compound of formula (I) and the organic solvent SOI, or the mixture of organic solvents SOI, is preferably between 0.001 and 10, and advantageously between 0.005 and 5.
• anhydrous GI-IF is introduced into the reaction medium, preferably in gaseous form.
• the molar ratio x between the fluorinating agent, preferably the anhydrous IFF, and the compound of formula (I) used is preferably between 1 and 10, and advantageously between 1 and 5.
• reaction step with the fluorinating agent preferably anhydrous HF
• step b) is carried out in an open medium, in particular with the release of HCl in the form of gas.
• the fluorination reaction typically leads to the formation of HCl, the majority of which can be degassed from the reaction medium (just like the excess HF if the fluorination agent is HF), for example by stripping with a neutral gas. (such as nitrogen, helium or argon).
• a neutral gas such as nitrogen, helium or argon.
• composition obtained at the end of step b) can be stored in an HF-resistant container.
• the composition obtained in step b) may comprise HF (it is in particular unreacted HF), the compound of formula (II) mentioned above, the SOI solvent (such as, for example, dioxane), and optionally HCl, and / or possibly heavy compounds.
• the process according to the invention may optionally comprise a step of distilling the composition obtained in step b).
• the process according to the invention may comprise a step c), subsequent to step b), of reaction of the compound of formula (II) obtained in the preceding step (step b)), with a composition comprising at least one salt of alkali metal or alkaline earth metal.
• the alkali or alkaline earth metal salt may be an alkali or alkaline earth metal carbonate, or an alkali or alkaline earth metal hydroxide, or an alkali or alkaline earth metal chloride, or an alkali metal fluoride or alkaline earth metal.
• the alkali metal or alkaline earth metal is chosen from: lithium, potassium, sodium, magnesium and calcium, the alkali metal being preferably potassium or lithium, and advantageously potassium.
• the alkali metal or alkaline earth metal salt is selected from the group consisting of: LiOH, UOH, H 2 O, LiHCO 3, U 2 CO 3 , LiCl, LiF, KOH, KOH, H 2 O, KHCO 3, K 2 CO 3 , KOI, Ca (OH) 2 , Ca (OH) 2 , H 2 O, Ca (HCO 3 ) 2 , CaCO 3 , CaCl 2 , CaF 2 , Mg (OH) 2 , Mg (OH) ) 2 , H 2 O, Mg (HCO 3 ) 2 , MgCO 3 , MgCl 2 , MgF 2 and mixtures thereof.
• the alkali metal or alkaline earth metal salt is K 2 CO 3
• the compound of formula (III) is a compound of formula (IV) mentioned above.
• composition comprising at least one alkali metal or alkaline earth metal salt may be an aqueous composition.
• composition comprising at least one alkali metal or alkaline earth metal salt may be a solid alkali metal or alkaline earth metal salt.
• Step c) may comprise adding the composition obtained in the preceding step to the composition comprising at least one alkali metal or alkaline earth metal salt, or the reverse, namely adding the composition comprising at least an alkali metal or alkaline earth metal salt in the composition obtained in the preceding step.
• an analysis of the total acidity of the mixture to be neutralized may typically be carried out.
• step c) is such that:
• the molar ratio of the alkali or alkaline-earth salt divided by the number of basicities of said salt relative to the compound of formula (II) is greater than or equal to 1, preferably less than 5, preferably less than 3, preferably between 1 and 2; and or
• the mass ratio of the alkaline or alkaline-earth salt to the mass of water in the aqueous composition is between 0.1 and 2, preferably between 0.2 and 1, preferably between 0.3 and 0.7.
• the salt K 2 CO 3 has a number of basicities equal to 2.
• Step c) of the process according to the invention may be carried out at a temperature of less than or equal to 40 ° C, preferably less than or equal to 30 ° C, preferably less than or equal to 20 ° C, and in particular less than or equal to 15 ° C.
• the method according to the invention comprises an additional step of filtering the composition obtained in step c), resulting in a filtrate F and a cake G.
• the compound of formula (III) prepared may be contained in the filtrate F and / or in the cake G.
• the filtrate F may be subjected to at least one extraction step with a SO 2 organic solvent which is typically poorly soluble in water, in order to extract the above-mentioned compound of formula (III) in an organic phase.
• the extraction step typically leads to the separation of an aqueous phase and an organic phase.
• “poorly soluble in water” means a solvent whose solubility in water is less than 5% by weight.
• the above-mentioned organic solvent SO 2 is in particular chosen from the following families: esters, nitriles, ethers, chlorinated solvents, aromatic solvents, and mixtures thereof.
• the organic solvent SO 2 is chosen from dichloromethane, ethyl acetate, butyl acetate, tetrahydrofuran and diethyl ether, and mixtures thereof.
• the organic solvent S0 2 is butyl acetate.
• the mass quantity of organic solvent used can vary between 1/6 and 1 times the weight of the filtrate F.
• the number of extractions can be between 2 and 10.
• the organic phase resulting from the extraction (s) has a mass content of compound of formula (III) ranging from 5% to 40% by weight.
• the separated organic phase (obtained after the extraction) can then be concentrated to reach a concentration of compound of formula (III) of between 30% and 60%, preferably between 40% and 50% by weight, concentration that can be achieved by any means of evaporation known to those skilled in the art.
• the aforementioned cake G can be washed with an organic solvent SO 3 selected from the following families: esters, nitriles, ethers, chlorinated solvents, aromatic solvents, and mixtures thereof.
• the organic solvent SO 3 is chosen from dichloromethane, ethyl acetate, butyl acetate, tetrahydrofuran, acetonitrile, diethyl ether, and mixtures thereof.
• the organic solvent SO 3 is butyl acetate.
• the mass quantity of organic solvent S03 used may vary between 1 and 10 times the weight of the cake.
• the total quantity of organic solvent S03 intended for washing can be used in one go or in several times, in particular in order to optimize the dissolution of the compound of formula (III).
• the organic phase, resulting from washing (s) cake G has a mass content of compound of formula (III) ranging from 5% to 20% by weight.
• the separated organic phase resulting from the washing (s) of the cake G can then be concentrated to reach a concentration of compound of formula (III) of between 30% and 60%, preferably between 40% and 50% by weight. said concentration can be achieved by any means of evaporation known to those skilled in the art.
• the organic phases resulting from the extraction (s) of the filtrate F and the washing (s) of the cake G can be collected together, before the concentration step.
• the process according to the invention may comprise a possible step d), subsequent to step c), of cation exchange between a compound of formula (III) obtained in the preceding step (step c)), and at least one lithium salt.
• the process according to the invention comprises this step d) when the salt obtained in step c) is not a lithium salt.
• Step d) is in particular a cation exchange reaction for converting a compound of formula (III) mentioned above into a compound of formula (IV):
• the lithium salt is a salt of formula LiX, X representing a fluoride, a chloride, a carbonate, a tetrafluoroborate, a hydroxide, a sulfate, a chlorate, a perchlorate, a nitrile or a nitrate.
• LiX is LiCl.
• the aforementioned lithium salt may be dissolved in a polar organic solvent, preferably selected from the following families: alcohols, nitriles and carbonates.
• a polar organic solvent preferably selected from the following families: alcohols, nitriles and carbonates.
• alcohols preferably selected from the following families: alcohols, nitriles and carbonates.
• methanol preferably ethanol
• ethanol preferably acetonitrile
• dimethylcarbonate dimethylcarbonate
• ethylmethylcarbonate ethylmethylcarbonate
• mixtures thereof preferably methanol.
• the molar ratio of the compound of formula (III) relative to the lithium salt may vary: it may be at least 1 and less than 5.
• the molar ratio of compound of formula (III) / lithium salt is between 1, 2 and 2.
• the reaction medium may be stirred for 1 to 24 hours, and / or at a temperature of, for example, 0 ° C to 50 ° C.
• the reaction medium can be filtered and then optionally concentrated.
• the concentration step can optionally be carried out by a thin-film evaporator, an atomizer, an evaporator, or any other apparatus for solvent evaporation.
• the method according to the invention may further comprise a purification step of the compound of formula (IV) mentioned above.
• Step d) of purifying the compound of formula (IV) can be carried out by any known conventional method. This may be for example an extraction method, a washing method with solvents, a reprecipitation method, a recrystallization method, or their combination.
• the compound of formula (IV) may be in the form of a solid, or a composition comprising from 1% to 99.9% by weight of compound of formula (IV).
• step e) is a crystallization step of the compound of formula (IV).
• the compound of formula (IV) is crystallized in the cold, in particular at a temperature of less than or equal to 25 ° C.
• the crystallization of the compound of formula (IV) is carried out in an organic solvent (“crystallization solvent") chosen from chlorinated solvents, such as, for example, dichloromethane, and aromatic solvents , such as for example toluene, and alkanes such as pentane, hexane, cyclohexane, heptane, in particular at a temperature of less than or equal to 25 ° C.
• the compound of formula (IV) crystallized at the end of step (e) is recovered by filtration.
• step e) comprises the following steps: i) optionally dissolving the compound of formula (IV) in an organic solvent S'1; ii) liquid-liquid extraction of the compound of formula (IV) with deionized water, and recovery of an aqueous solution of said compound of formula (IV);
• Step e) may not comprise step i) mentioned above, if the compound of formula (IV) obtained in step d) already comprises an organic solvent (such as for example SO 2 and / or SO 3).
• an organic solvent such as for example SO 2 and / or SO 3.
• step ii) comprises in particular the addition of deionized water to the solution of the compound of formula (IV) in the abovementioned organic solvent S'1, to allow the dissolution of said compound of formula (IV), and the extraction said compound of formula (IV) in water (aqueous phase).
• the extraction can be carried out by any known extraction means.
• step ii) can be repeated at least once, for example three times.
• a quantity of deionized water corresponding to half of the mass of the initial solution can be added, then an amount equal to about 1/3 of the mass of the initial solution during the second extraction, then a amount equal to about 1/4 of the mass of the initial solution during the third extraction.
• step ii) is such that the mass of deionized water is greater than or equal to one third, preferably greater than or equal to half, of the mass of the initial solution of the compound of formula (III) in the organic solvent S'1 (in the case of a single extraction, or for the first extraction only if step ii) is repeated at least once).
• step ii the extracted aqueous phases are combined together to form a single aqueous solution.
• step ii) an aqueous solution of compound of formula (IV) is obtained in particular.
• the mass content of compound of formula (IV) in the aqueous solution is between 5% and 35%, preferably between 10% and 25%, relative to the total mass of the solution.
• step e) comprises a step of concentration iii) between step ii) and step iv), preferably to obtain an aqueous solution of the compound of formula (IV) comprising a mass content of compound of formula (IV) of between 20% and 80%, in particular between 25% and 80%, preferably between 25% and 70%, and advantageously between 30% and 65% relative to the mass total of the solution.
• the concentration step can be carried out by an evaporator under reduced pressure, at a pressure of less than 50 mbar abs (preferably less than 30 mbar abs), and in particular at a temperature of between 25 ° C and 60 ° C, of preferably between 25 ° C and 50 ° C, preferably between 25 ° C and 40 ° C, for example at 40 ° C.
• the compound of formula (IV), contained in the aqueous solution obtained at the end of step ii), and of a possible concentration step iii) or of any other intermediate step, can then be recovered by extraction. with an organic solvent S'2, said solvent S'2 (step iv).
• Stage iv) advantageously makes it possible to obtain an aqueous phase and an organic phase, which are separated.
• the organic solvent S'2 is selected from the group consisting of esters, nitriles, ethers, chlorinated solvents, aromatic solvents, and mixtures thereof.
• the solvent S'2 is chosen from ethers, esters, and mixtures thereof.
• the solvent S'2 is selected from methyl-t-butyl ether, cyclopentylmethyl ether, ethyl acetate, propyl acetate, butyl acetate, and mixtures thereof.
• the organic solvent S'2 is butyl acetate.
• the extraction step iv) is repeated at least once, preferably from one to ten times, and in particular four times.
• the organic phases can then be combined into one before step v).
• the mass quantity of organic solvent used can vary between 1/6 and 1 times the mass of the aqueous phase.
• the mass ratio organic solvent S'2 / water, during an extraction of step iv) varies from 1/6 to 1/1, the number of extractions varying in particular from 2 to 10.
• the organic solvent S'2 is added to the aqueous solution resulting from step ii) (and from possible step iii).
• Step e) may comprise a pre-concentration step between step iv) and step v), preferably to obtain a solution of the compound of formula (IV) in the organic solvent S'2 comprising a mass content of compound of formula (IV) of between 20% and 60%, and preferably between 30% and 50% by weight relative to the total mass of the solution.
• the pre-concentration stage can be carried out at a temperature ranging from 25 ° C to 60 ° C, preferably from 25 ° C to 45 ° C, optionally under reduced pressure, for example at a pressure of less than 50 mbar abs, in particular at a pressure of less than 30 mbar abs.
• the pre-concentration step is preferably carried out by an evaporator under reduced pressure, in particular at 40 ° C. and at a pressure of less than 30 mbar abs.
• the concentration step v) can be carried out at a pressure of between 10 -2 mbar abs and 5 mbar abs, preferably between 5.10 -2 mbar abs and 2 mbar abs, preferably between 5.10 1 and 2 mbar abs, even more preferably between 0.1 and 1 mbar abs, and in particular between 0.4 and 0.6 mbar abs.
• step v) is carried out at 0.5 mbar abs or at 0.1 mbar.
• step v) is carried out at a temperature between 30 ° C and 95 ° C, preferably between 30 ° C and 90 ° C, preferably between 40 ° C and 85 ° C, and in particular between 50 ° C and 70 ° C.
• step v) is carried out with a residence time of less than or equal to 15 minutes, preferably less than 10 minutes, and preferably less than or equal to 5 minutes and advantageously less than or equal to 3 minutes.
• the term “residence time” means the time that elapses between the entry of the solution of the compound of formula (III) (in particular obtained at the end of of step iv) above) in the evaporator and the outlet of the first drop of the solution.
• the temperature of the condenser of the short-path thin-film evaporator is between -55 ° C. and 10 ° C., preferably between -50 ° C. and 5 ° C., more preferably between -45 ° C. ° C and -10 ° C, and advantageously between -40 ° C and -15 ° C.
• the aforementioned short-path thin-film evaporators are also known as "Wiped film short path” (WFSP). They are typically so called because the vapors generated during evaporation make a “short trip" (short distance) before being condensed to the condenser.
• WFSP Wiped film short path
• evaporators marketed by the companies Buss SMS Ganzler ex Luwa AG, UIC Gmbh or VTA Process.
• short-path thin-film evaporators may include a solvent vapor condenser positioned within the apparatus itself (particularly in the center of the apparatus), unlike other types of film evaporators. thin (which are not short path) in which the condenser is located outside the device.
• the formation of a thin film of product to be distilled on the internal hot wall of the evaporator can typically be provided by continuously spreading on the evaporation surface by mechanical means. specified below.
• the evaporator may in particular be provided at its center, an axial rotor on which are mounted the mechanical means that allow the formation of the film on the wall.
• They may be rotors equipped with fixed blades: three-blade or four-blade lobed rotors in flexible or rigid materials, distributed over the entire height of the rotor or rotors equipped with moving blades, pallets, scrapers, guided rubbers.
• the rotor may be constituted by a succession of articulated pallets on pivot mounted on a shaft or axis via radial supports.
• Other rotors may be equipped with mobile rollers mounted on secondary axes and said rollers are pressed on the wall by centrifugation.
• the rotational speed of the rotor which depends on the size of the apparatus can be readily determined by those skilled in the art.
• the various mobiles can be made of various materials, for example metal, steel, alloy steel (stainless steel), aluminum, or polymers, for example polytetrafluoroethylene PTFE or glass materials (enamel); metallic materials coated with polymeric materials.
• the process according to the present invention is particularly advantageous for producing the following compounds of formula (IV): LiN (SO 2 F) 2 , UNSO 2 CF 3 SO 2 F, UNSO 2 C 2 F 5 SO 2 F, UNSO 2 CF 2 OCF 3 SO 2 F, UNSO 2 C 3 HF 6 SO 2 F, UNSO 2 C 4 F 9 SO 2 F, UNSO 2 C 5 F 11 SO 2 F, L 1 SO 2 C 6 F 13 SO 2 F, L 1 NO 2 C 7 F 15 SO 2 F, L 1 NSO 2 C 8 F 17 SO 2 F and L 1 NO 2 C 9 F 19 SO 2 F.
• the process according to the invention is a process for the preparation of LiN (SO 2 F) 2 (LiFSI).
• lithium salt of bis (fluorosulfonyl) imide lithium salt of bis (fluorosulfonyl) imide
• lithium bis (sulfonyl) imide lithium bis (fluorosulfonyl) imide
• LiFSI lithium bis (sulfonyl) imide
• LiN (SO 2 F) 2 lithium bis (fluorosulfonyl) imide
• between x and y" or “ranging from x to y” means an interval in which the terminals x and y are included.
• the temperature "between -20 and 80 ° C” includes in particular the values -20 ° C and 80 ° C.
• a stirred one-liter glass reactor is charged with sulfamic acid (1 eq, 1, 24mol, 120g) and 95% sulfuric acid (1 eq, 1, 24mol, 127.5g). ).
• the thionyl chloride (4 eq, 4.9 mol, 583 g) is gradually added to the reactor with the aid of a dropping funnel.
• the temperature of the reaction medium is maintained at 35 ° C. for 2 hours and then is gradually increased to 75 ° C.
• the réadion is maintained at a temperature of 75 ° C for 64 hours to obtain a total convection sulfamic acid.
• a condenser operating with cold water is placed on the reactor vent line so as to condense the vaporized thionyl chloride and reflux it into the reaction medium.
• the gases generated by the reaction (HCl and SO 2 ) and not condensed by the condenser are directed to a bubbler containing water where they are absorbed.
• a glass reactor is charged with sulfamic acid (1 eq, 0.41 mole, 40 g) and thionyl chloride (3.25 eq, 1.34 mole, 159.3 g). 20% oleum (1 eq, 0.41 mol, 38.9 g) is gradually added to the reactor.
• the reaction medium is stirred and is heated until a temperature of 120 ° C is obtained.
• the pressure of the reactor is set at 8 bar absolute by means of an overflow located on the outlet of the reactor vent. Downstream of the discharge, this vent is directed to a bubbler containing 1 kg of water to absorb the gases.
• the reaction time is 20 hours to obtain a total conversion to sulfamic acid.
• the final bis (chlorosulfonyl) imide is light yellow in appearance.
• 136.4 g of liquid containing bis (chlorosulfonyl) imide, residual thionyl chloride and solubilized S0 2 are recovered.
• a stirred one-liter glass reactor was charged with sulfamic acid (1 eq, 1, 24 mol, 120 g) and 95% sulfuric acid (1 eq, 1, 24 mol, 127.5 g).
• Thionyl chloride (4 eq, 4.9 mol, 583 g) is gradually added to the reactor using a dropping funnel.
• the temperature of the reaction medium is gradually increased to 90 ° C.
• the reaction is carried out at atmospheric pressure.
• the total conversion to sulfamic acid is obtained after 52 hours.
• a condenser operating with cold water is placed on the reactor vent line so as to condense the vaporized thionyl chloride and reflux it into the reaction medium.
• the gases generated by the reaction (HCl and SO2) and those not condensed by the condenser are directed to a bubbler containing water where they are absorbed.
• a stirred one-liter glass reactor was charged with sulfamic acid (1 eq, 1, 24 mol, 120 g) and 95% sulfuric acid (1 eq, 1, 24 mol, 127.5 g).
• the thionyl chloride (4 eq, 4.9 mol, 583 g) is gradually added to the reactor with the aid of a dropping funnel.
• the temperature of the reaction medium is gradually increased to 90 ° C.
• the pressure of the reactor is set at 8 bar absolute by means of an overflow located on the outlet of the reactor vent. Downstream of the discharge, this vent is directed to a bubbler containing water to absorb the gases.
• the total conversion to sulfamic acid is obtained in less than 52 hours. 323 g of liquid containing bis (chlorosulfonyl) imide and residual thionyl chloride are obtained.
• a stirred one-liter glass reactor was charged with sulfamic acid (1 eq, 1, 24 mol, 120 g) and 95% sulfuric acid (1 eq, 1, 24 mol, 127.5 g).
• the thionyl chloride (3.5 eq, 4.9 mol, 583 g) is gradually added to the reactor using a dropping funnel.
• the temperature of the reaction medium is gradually increased to 90 ° C.
• the pressure of the reactor is set at 8 bar absolute by means of an overflow located on the outlet of the reactor vent. Downstream of the discharge, this vent is directed to a bubbler containing water to absorb the gases.
• the total conversion to sulfamic acid is obtained in less than 52 hours.
• 320.5 g of liquid containing bis (chlorosulfonyl) imide and residual thionyl chloride are obtained.
• Example 4 shows that the implementation of the chlorination reaction under a pressure of 8 bar (Example 4) advantageously makes it possible to obtain the conversion total sulfamic acid in a reduced time compared to the implementation at atmospheric pressure (Example 3).
• the chlorination reaction carried out under a pressure of 8 bar advantageously makes it possible to reduce the time to obtain a total conversion to sulphamic acid while decreasing the molar amount of thionyl chloride (example 5) relative to the reaction under atmospheric pressure. (Example 3)
• LiFSI was prepared from each of the bis (chlorosulfonyl) imides obtained in Examples 1 to 5, according to the procedure described in Example 3 of WO2014 / 080120.

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