METHOD OF SALT EXTRACTION AND THERMALLY REGENERATED EXTRACTING COMPOSITION.

Abstract

A thermally regenerated hydrophobic liquid composition comprising an extractant molecule of a non-alkali cationic species, a solvating molecule of a complementary anionic species, and a fluidifier, said composition being characterized in that the extractant molecule of a non-alkali cationic species is a macrocycle whose ring is formed by 24 to 32 carbon atoms and of the following formula (I) or (II): (see Formulas) (I) (II) where -n is an integer from 5 to 8, -p is 1 or 2, -m is 3 or 4, -qyt, identical or different, are 0, 1 or 2, -R is a tert-butyl, tert-octyl, O-methyl, O-ethyl, O-propyl, O-isopropyl, O-butyl, O-isobutyl, O-pentyl, O-hexyl, O-heptyl, O-octyl, or OCH2phenyl group or a hydrogen atom, - R' and R", identical or different, are chosen from the group consisting of methyl, ethyl, propyl, isopropyl, butyl, isobutyl, heptyl and octyl groups or R' and R" together form a pyrrolidine, piperidine or morpholine ring.

Description

Method of salt extraction and thermally regenerated extractant composition Technical field of the invention The technical field of the invention is the ionic extraction of salts, especially hydrophilic salts, applied to the treatment of industrial or natural saline waters. State of the art Mining, oil, and industrial activities can generate highly saline, fouling, and / or toxic metal-contaminated wastewater that requires treatment before release into the environment, or even before recycling in an industrial process. In any of these cases, manufacturers currently only offer very expensive solutions that are poorly suited, or not at all, to their specific environments. There are also cases, especially for highly scale-forming saline waters rich in alkaline earth metal cations and / or containing trace metals, where there is currently no sustainable and / or economical processing technology for this water, forcing the storage of these waters in settling tanks while awaiting a solution. In the case of mixtures of water from different or highly scale-producing sources, it is common for equipment to become scaled by precipitation of salts with low water solubility, such as certain carbonate salts (MgCCh, CaCOa, SrCOa, BaCCh, CdCCh, CO3, MnCOa, PbCO3, N1CO3, FeCO3, ZnCO3), sulfate salts (CaSO4, SrSCU, BaSO4, PbSCh...), fluoride salts (MgF2, CaF2, SrF2, BaF2, CdF2, FeF21 PbFa...), metallic hydroxide salts (Mg(OH)a, Ca(OH)2, Cd(OH)2, Co(OH)2, Fe(OH)2, Ni(OH)2, Zn(OH)2...), and others that may be present in a considerable quantity.Furthermore, if the technology used is associated with thermal vaporization of this water, the temperature of use, which usually exceeds 80°C, then generates a decrease in the precipitation threshold of certain salts (for example, carbonate salts such as CaCO3 by evaporation of carbon dioxide) and salts of inverted solubility (such as CaSO4), which can further limit the maximum level of water extraction from the seawater or generate an even larger volume of solid waste to be managed. To extract an ion or salt dissolved in industrial or natural water, the current approach is chemical, for example, by ensuring precipitation through the addition of a reagent such as a base (NaOH, etc.). This allows the precipitation of water-insoluble metal hydroxides. This method is not selective for the precipitated metals and involves an exchange of cations (Na+ against the metal in this case) or anions. It also presents other drawbacks, such as the addition of new contaminants that require further treatment and a decrease in efficiency due to a reduction in the concentration of the desired compounds. Another solvent extraction method, known as hydrometallurgy, can also be used to extract metals such as nickel and cobalt at higher concentrations through Mn+ / nH+ cation exchange. These processes employ cationic extractants dissolved in a solvent, using acid-base chemistry, or the extraction and solvent regeneration are performed at pH levels that differ by several orders of magnitude. This method, therefore, consumes expensive bases (NaOH, etc.) and acids (H2SO4, etc.), resulting in the addition of new pollutants associated with the co-production of salts (Na2SO4, etc.) that require further management. Another method, also used for over 50 years, involves employing selective electrodialysis membranes, namely permeable to cations or anions and impermeable to water and neutral molecules in general. In this case, the electrical energy consumed is proportional to the salt displaced, which limits its use to high-value-added applications in brine treatment. This technology is not selective for ions of the same charge and, therefore, is not selective for metals or anions to be extracted, and it also carries a risk of membrane clogging. There are other methods, such as ion exchange, where selectivity depends on the charge of the ion, limited by the concentration of the ion being treated, and in that case they also generate a contribution of new contaminants from the chemical regeneration of the resins. More recently, the applicant described in application WO2010 / 086575 the use of fluorinated compounds in a direct contact exchanger comprising a liquid, hydrophobic fluorinated phase associated with ion exchangers. However, the liquid organic fluorinated phase described in this application involves the use of ionic and non-ionic organofluorinated compounds in a process poorly suited to achieving high water desalination rates or selective salt desalination, and in particular, descaling as a result of an unsuitable regeneration process. US patent application 2008 / 179568A1 describes a liquid-liquid extraction process for low-concentration cesium and strontium using two types of cationic extractant molecules: crown ethers at medium concentrations and calixarenes at very low concentrations (0.0025 to 0.025 mol / L), and at least one modifier dissolved in a diluent such as a C12-C15 isoparaffinic hydrocarbon. The modifier may be an alcohol, a trioctylamine (TOA), tri-n-butyl phosphate (TBP), or mixtures thereof. This compound is intended to enhance the capabilities of the cationic extractant and / or its ability to remain solubilized during use. US patent application US2008 / 0014133 describes a liquid extraction process of cesium and strontium in low concentration by employing cationic extractant molecules of the crown ether family in low concentration (0.04 to 0.095 Mol / L), combined with a fluorinated alcohol (called Fluoroheptanol m) in high proportion (>80% volume) and a glycol ether. US patent 6566561B1 describes a liquid-liquid extraction process of cesium at low concentration using solvation agents and phenoxyfluoro-alcohol type phase modifiers stable in basic medium, in the presence of cationic extractant molecules of the calixarene-ether-crown family at low concentration (0.001 to 0.20 Mol / L, preferably 0.01 Mol / L). In this field there is a very abundant bibliography among which we can cite the article by TG Levitskaia, et al. Anal. Chem. 2003, 75,405-412 which demonstrates that it is possible to extract soda (NaOH) from an aqueous solution by using a neutral sodium extractant, of the crown ether type, with a deprotonable lipophilic weak acid to allow the formation of a hydrophobic sodium alcoholate. [DC18C6](org) + [RCOH](org) + [Na+](aq) + [OH](aq) ** [RCO'Na+DC18C6](org) + H2O(aq) This document also presents examples of the extraction of NaF, NaCl, NaBr, NaNO₃, and NaClO₃ at 1 M salinity by combining 0.02 M DC₁₈C₆ with and then with seven weak acids (from the alcohol family) present at a concentration of 0.04 M, all dissolved in nitrobenzene. Two of these alcohols are fluorinated aromatic alcohols with a pKa of approximately 8.8. The salt extraction rate for hydrophobic ions such as picrate is relatively high. However, for hydrophilic anions, such as the chloride ion (Cl⁻), the recalculated salt extraction rates range from 0.06% to 0.16%, confirming the significant difficulty in extracting hydrophilic NaCl from water and the minimal influence of alcohols, at this concentration, on the extraction yield. Therefore, it appears that the industry is currently awaiting a brine treatment solution, whether contaminated by metals or not, that is effective for salt extraction across a wide salinity range and much less expensive in terms of both investment and implementation. It is often also expected to be able to separate the combinations of scale-forming ions, remove them or reduce the presence of specific salts and particularly those at the beginning of scaling of equipment by these waters and / or reuse some of the inorganic compounds present in these waters, in order to finance all or part of this treatment. The purpose of this patent application is, therefore, to describe a new technology for treating saline water and water contaminated with metals, and to address these problems by selectively or on a large scale extracting salts of varying economic value from the water for the treatment of industrial or natural saline waters. This technology can be widely applied to allow the discharge of this water into the environment while respecting ecosystems, for its reuse as process water, or to provide new or complementary economic value within the framework of mining, oil extraction, or the recycling of salts and / or metallic cations with high added value.This new technology also has the advantage that it does not generate new pollutants because the ions are extracted from the water in the form of electrically neutral compound salts, which are then removed from the extraction solvent by regenerating the active extract via a thermal rather than chemical method. Description of the invention For the extraction of salts from an aqueous medium, this application describes a liquid-liquid extraction deionization process with thermal regeneration that employs a liquid hydrophobic organic phase comprising or essentially consisting of, or consisting of, - at least one electrically neutral, hydrophobic organic compound capable of extracting (e.g., solvating, complexing, or chelating) a cation from the salts to be extracted from the aqueous phase, called MEO for Cation Extracting Molecule, - at least a second electrically neutral, hydrophobic organic compound capable of solvating the anions of the salts to be extracted from the aqueous medium, called MSA for Anion Solvating Molecule; and, eventually, - a fluidifier, preferably hydrophobic. Surprisingly, the combination of MSA and MEC according to the invention allows the synergistic extraction of neutral salts composed of cations and hydrophilic anions that are particularly difficult to transfer in an organic phase. The term hydrophobic means a compound, or a mixture of compounds, whose solubility in water at 25°C is at least less than 0.1 mol / L. Preferably, it is selected from among the hydrophobic compounds whose solubility in water at 25°C is less than 0.01 mol / L, preferably less than 0.0001 mol / L, and advantageously less than 1 x 10⁵ mol / L. The hydrophobicity or water solubility of a compound can be measured by standard methods, particularly by UV-visible spectrometry. MEC A MEC compound as described in the present application, its mixtures and uses in a process for extracting a cationic species from water containing said species as a liquid-liquid extraction water deionization process with thermal regeneration for the extraction of at least one divalent cationic species and at least one complementary anion are also part of the invention. The extracting agent (EAA), which allows the extraction of at least one cation, can be advantageously chosen from among molecules with a good capacity for extracting alkaline earth ions, such as calcium, strontium, or barium ions, or other divalent cations, depending on the separation requirements. Extraction is possible by replacing the solvation of cations and anions with water with their solvation by the extracting composition, which then allows interaction with the EEA and the extracting agent. The nature of these interactions encompasses phenomena such as ion-dipole interactions, accompanied by the formation of hydrogen bonds and electrostatic interactions, including van der Waals forces. Preferably, the EEA is a compound that allows complexation, and in particular chelation, of the cation. Chelation differs from simple complexation in that the cation is bound to the chelating ligand by at least two bonds / interactions. The MECs to be considered for the selective extraction of divalent cations from monovalent alkali metal cations are macrocycles of the metacyclophane (MCP) family, which possess a hydrophobic cavity described by n aromatic rings of the phenol type. The size of the macrocycle varies from 24 to 32 atoms, particularly carbon atoms. Preferably, the size of the macrocycle is 24 to 28 carbon atoms. These phenol-type aromatic rings can be linked to each other at the ortho position of the hydroxyl group, either directly or through 1-carbon methylene bridges (CH2-), 2-carbon bridges (-CH2CH2-), or 3-carbon bridges (CH2CH2CH2)-. If only direct linkages are present, these macrocycles are usually called ester groups, of type [0n]. If only 1-carbon methylene bridges (-CH2-) are present, these macrocycles are usually called calixarenes, of type [1n]. If only 2-carbon bridges (-CH2CH2-) are present, these macrocycles are usually called all-homocalixarenes, of type [2n]. The size of the bridges can also vary within the same macrocycle, spanning 0 to 3 carbon atoms. The nomenclature specifies this variety by calling them, for example, [1.3.1.3]MCP or [1.3]2MCP for a macrocycle of 4 aromatics connected ortho successively by a methylene bridge and then by a 3-carbon bridge and then again by a methylene bridge and finally by a 3-carbon bridge to close the cycle. The macrocycles of interest are then functionalized by non-hydrogenated amide groups for the selective extraction of alkaline earth metals, although they are not equally selective for the extraction of divalent transition metals. Thus, a MEC that allows the selective extraction of non-alkali cations, particularly divalent cations, versus alkali cations, particularly monovalent cations, is a macrocycle whose cycle is formed by 24 to 32 carbon atoms, functionalized by amide groups, and of the following formula (I) or (II): where - n is an integer that ranges from 5 to 8, - p is 1 or 2, - m is 3 or 4, - q and t, identical or different, are 0.1 or 2, -R is a tert-butyl, tert-pentyl, tert-octyl, O-methyl, O-ethyl, O-propyl, O-isopropyl, O-butyl, O-isobutyl, O-pentyl, O-hexyl, O-heptyl, O-octyl, OCH2Phenyl group, or a hydrogen atom, - R' and R, identical or different, are chosen from the group consisting of methyl, ethyl, propyl, isopropyl, butyl, isobutyl, pentyl, hexyl, heptyl and octyl groups, or R' and R form a set of a pyrrolidine, piperidine or morpholine ring. Thus, for compounds of formula (I), the integers nyp should be chosen such as 24 s (3+p) xns 32. For compounds of formula (II) the integers m, qyt should be chosen such as 24 s (7+q+t) xms 32. These molecules belong to the metacyclophane family. Advantageously, MEO is a molecule with the formula: Cyclo on 24 (of the Calix[6]arene family, of type [le]), where R, R' and R are as previously defined for formulas (I) and (II). When R' and R are both an ethyl group, the selective extraction of the divalent cations is particularly strong, in particular when the R radical is tert-butyl, OChaPh, H or O-methyl. Advantageously, the MEC is a molecule with the formula: (from the family of All-homocalix[5]arenes, of type

[25] ), where R, R', and R are as previously defined for formulas (I) and (II). Advantageously, the MEC is a molecule of formula: (from the family of All-homocalix[6]arenes, of type

[26] ), where R, R', and R are as previously defined for formulas (I) and (II). Advantageously, the MEC is a molecule of formula: N! A 28-membered ring (from the Calix[7]arene family, of type

[17] ), where R, R', and R are as previously defined for formulas (I) and (II). Advantageously, the MEC is a molecule of formula: (from the Calix[8]arene family, of type [1e]), where R, R' and R are as previously defined for formulas (I) and (II). When R' and R are both an ethyl group, the selective extraction of the divalent cations is particularly interesting, especially when the R radical is tert-butyl, OChhphenyl, H or Omethyl. Advantageously, the MEC is a molecule with the formula: VICE in z? (of type p.1.2.1.2.1JMCP or [2.1]3MCP), where R, R' and R are as previously defined for formulas (I) and (II). Advantageously, the MEC is a molecule of formula: (of type [3.1,3.1.3.1]MCP or [3.1]3MCP), where R, R' and R are as previously defined for formulas (I) and (II). Advantageously, the MEC is a molecule with the formula: vice in ze (of type [2.0.2.0.2.0]MCP or [2.0]3MCP), where R, R' and R are as previously defined for formulas (I) and (II). Advantageously, the MEC is a molecule of formula: Cycle at 27 (of type [3.0.3.0.3.0]MCP or [3.0]3MCP), where R, R', and R are as previously defined for formulas (I) and (II). Advantageously, the MEC is a molecule of formula: (of type [1.0.1.0.1.0.1.0]MCP or [1.0]4MCP), where R, R', and R are as previously defined for formulas (I) and (II). Advantageously, the MEC is a molecule of formula: (of type [2.0.2.0.2.0.2.0JMCP or [2.0]4MCP), where R, R' and R are as previously defined for formulas (I) and (II). In formulas (I) and (II): Particularly advantageous, the R group is tert-butyl. Particularly advantageous, the R' and R groups are both an ethyl group. Particularly advantageous, the R group is either tert-butyl or a hydrogen atom. Particularly advantageously, MEC is the compound with the formula: GAH5 (from the Calix[6]arene family, of type [1e], and CAS number: 111786-95-9). This MEC2 is particularly effective for the selective extraction of hydrophilic alkaline earth salts, in particular chloride salts, from an aqueous solution when these are combined with at least one MSA and optionally a fluidizer within a liquid-liquid extraction process with thermal regeneration of the liquid resin, according to the invention. The molecules belonging to these families of formula (I) are already identified by a CAS number, and in particular these are the following cation-extracting molecules: CAS No. R Macrocycle P n R· R 136534-29-7 tert-Butyl Calixarene 1,6 Pyrrolidinyl 111786-95-9 tert-Butyl Calixarene 1,6 Ethyl Ethyl 385376-74-9 O-Octyl Calixarene 1,6 Ethyl Ethyl 327154-32-5 OCH2Phenyl Calixarene 1,6 Ethyl Ethyl 185330-54-5 H Calixarene 1,6 Ethyl Ethyl 327154-34-7 O-Methyl Calixarene 1,6 Ethyl Ethyl 315191-66-1 tert-Butyl Calixarene 1,8 Ethyl Ethyl 327154-36-9 O-Octyl Calixarene 1,8 Ethyl Ethyl 193743-58-7 OCH2Phenyl Calixarene 1 8 Ethyl Ethyl 327154-37-0 H Calixarene 1 8 Ethyl Ethyl 315191-06-1 O-methyl Calixarene 1 8 Ethyl Ethyl The composition according to the invention may also comprise more than one MEC compound that allows the extraction of at least one cation, which may be advantageously chosen from among the compounds described in this application. Another object of the invention relates to the use of these MEC compounds for the extraction of salts and / or ions from an aqueous medium. In particular, these compounds can be used, individually or in mixtures, in a composition or in a process according to the invention as described in this application. Another object of the invention relates to the use of macrocycle-type MEC compounds with a ring size of between 16 and 22 atoms, particularly carbon atoms, and functionalized by amide groups, for salt extraction, and in particular the extraction of salts of hydrophilic anions such as chloride salts. Specifically, these compounds, associated with the MSA according to the invention, allow the bulk extraction of a solution containing a mixture of such salts, for example, chloride salts comprising different cations having an ionic radius between 55 pm and 180 pm, advantageously between 70 pm and 167 pm, and more particularly between 75 pm and 167 pm. Such cations are particularly monovalent lithium, sodium, potassium, rubidium, or cesium cations, or divalent calcium, strontium, or barium cations, including transition metal cations.Note that magnesium, which is a divalent cation with an ionic radius of 72 pm, is an exception and is not considered sufficiently extractable for these MECs to be used industrially for the purpose of extracting it from water. These compounds have the generic formula (III) and (IV): where - n is 4 or 5, - p is 1 or 2, - m is 2 or 3, - q and t, identical or different, are 0.1 or 2, - R is a tert-butyl, tert-pentyl, tert-octyl, O-methyl, O-ethyl, O-propyl, O-isopropyl, O-butyl, O-isobutyl, O-pentyl, O-hexyl, O-heptyl, O-octyl, OChaphenyl group, or a hydrogen atom, - R' and R, identical or different, are chosen from the group consisting of methyl, ethyl, propyl, isopropyl, butyl, isobutyl, pentyl, hexyl, heptyl and octyl groups, or R' and R together form a pyrrolidine, piperidine or morpholine ring. Thus, for compounds of formula (III), the integers nyp should be chosen such as 16 < (3+p) xns 22. For compounds of formula (IV) the integers m, qyt should be chosen such as 16 < (7+q+t) xm < 22. In particular, the MEC1 macrocycle of formula III where n=4, R = tert-butyl and R'=R=ethyl and CAS number 114155-16-7, in its cone configuration, is particularly effective for the bulk or global extraction of hydrophilic salts, in particular chloride salts, from an aqueous solution when combined with at least one MSA and optionally a fluidizer within a liquid-liquid extraction procedure with thermal regeneration of the liquid resin, according to the invention. Molecules belonging to these families of formulas (III) and (IV) are also already identified by a CAS number, in particular the following MEOs: CAS No. R Macrocycle P n R' R Configuration 150588-24-2 H Calixarene 1,4 Ethyl Ethyl cone 412334-02-2 H Calixarene 1,4 Butyl Butyl cone 1558817-92-7 H Calixarene 1,4 Morpholidynyl cone 149635-98-3 H Calixarene 1,4 Piperidinyl cone 145237-45-2 tert-Butyl Calixarene 1,4 Methyl Methyl cone 114155-16-7 tert-Butyl Calixarene 1,4 Ethyl Ethyl cone 162714-60-5 tert-Butyl Calixarene 1,4 Propyl Propyl cone 116906-60-6 tert-Butyl Calixarene 1,4 Butyl Butyl cone 162714-61-6 tert-Butyl Calixarene 1,4 Pentyl Pentyl cone 162714-62-7 tert-Butyl Calixarene 1,4 Hexyl Hexyl cone 162714-63-8 tert-Butyl Calixarene 1,4 Octyl Octyl cone 162714-67-2 tert-Butyl Calixarene 1,4 Ethyl CH2-Ph cone 353236-42-7 tert-Butyl Calixarene 1,4 Methyl Heptyl cone 171800-66-1 tert-Butyl Calixarene 1,5 Ethyl Ethyl cone 133801-01-1 tert-Butyl Calixarene 1,4 Pyrrolidinyl cone 353236-41-6 tert-Butyl Calixarene 1,4-piperidinyl cone 353236-67-6 tert-Butyl Calixarene 1,4-morpholinyl cone For calixarenes, cone-type and even partial cone-type cycle configurations are preferable to alternating 1,2 or alternating 1,3 configurations, without excluding these alternating configurations. Other 20-carbon metacyclophane-type cycles have been identified: CAS No. R Macrocycle tqm R' R” Configuration 353742-72-0 tert-Butyl MCP[1.3]2 1 2 2 Ethyl Ethyl 1,4-alternating 352742-73-1 tert-Butyl MCP[1.3]2 1 2 2 Methyl Methyl 1,4-alternating 353742-74-2 tert-Butyl MCP[1.3]2 1 2 2 Butyl Butyl 1,4-alternating A preferred aspect of the invention is that the MEC of formula (III) or (IV) has a Log K complexation constant, in methanol at 25°, of the cationic species to be extracted, of a value greater than 3 and less than 11, preferably greater than 5 and less than 9. These amide-type MECs are particularly well suited to the liquid-liquid extraction procedure by temperature difference according to the invention. Another object of the invention relates to the use of MEC compounds functionalized by ester or ketone groups for the selective extraction of alkali metal cations, as opposed to alkaline earth metal cations, but without being selective for the extraction of monovalent transition metals (Silver Ag+). In particular, these compounds can be used, individually or in mixtures, in a composition or in a process according to the invention as described in this application. Another object of the invention relates to the use of macrocycle-type MEC compounds with a ring size of between 16 and 24 carbon atoms, functionalized by ester or ketone groups, for the selective extraction of alkali salts, and in particular alkali salts with hydrophilic anions such as chloride salts. Specifically, these compounds associated with the MSA according to the invention allow the selective extraction of one or more alkali salts from a solution containing a mixture of such salts, for example, chloride salts comprising different cations having an ionic radius between 55 pm and 180 pm, advantageously between 70 pm and 167 pm. Such cations are particularly monovalent lithium, sodium, potassium, rubidium, and cesium cations, or divalent calcium, strontium, and barium cations, including transition metal cations. These compounds have the generic formula (V) and (VI): (V) (VI) where - n is 4, 5 or 6, - p is 1 or 2, - m is 2 or 3, - q and t, identical or different, are 0.1 or 2, - R is a tert-butyl, tert-pentyl, tert-octyl group, or a hydrogen atom, - R' is chosen from the group consisting of methyl, ethyl, propyl, isopropyl, butyl, isobutyl, pentyl, hexyl, heptyl and octyl groups, for the realization of a ketone-type ligand group or R' is chosen from the group consisting of the O-methyl, O-ethyl, O-propyl, O-isopropyl, O-butyl, O-isobutyl, O-pentyl, O-hexyl, O-heptyl, O-octyl, OCH2phenyl groups for the realization of an ester-type ligand group. Thus, for compounds of formula (V), the integers nyp should be chosen such as 16 s (3+p) xns 24. For compounds of formula (VI), the integers m, qyt should be chosen such as 16 < (7+q+t) xm £ 24. In particular, the MEC10 macrocycle of formula (V) where n=4, R=tert-butyl and RO-ethyl and of CAS No. 97600-39-0, in its cone configuration, is particularly effective for the selective extraction of sodium salts, in particular as sodium chloride salt, from an aqueous solution when combined with at least one MSA and optionally a fluidizer within a liquid-liquid extraction procedure with thermal regeneration of the liquid resin, according to the invention. In particular, the MEC11 macrocycle of formula (V) where n=5, R=tert-butyl and RO-ethyl and of CAS No. 152495-34-6, and the MEC12 macrocycle of formula (V) where n=6, R = tert-butyl and R=O-ethyl and of CAS No. 97600-45-8, in their cone configurations, are particularly effective for the selective extraction of alkali salts versus alkaline earth salts, particularly as alkali chloride salts, from an aqueous solution when combined with at least one MSA and optionally a fluidizer within a liquid-liquid extraction process with thermal regeneration of the liquid resin, according to the invention. The MEC11 is adapted to extract alkali chloride salts more globally (except lithium), while the MEC12 for a larger cycle diameter of 24 has an extraction capacity of larger diameter alkalis (cesium, rubidium, even potassium). Molecules belonging to these families of formulas (V) and (VI) are also already identified by a CAS number, in particular the following MECs: CAS No. R Macrocycle P n R' Configuration 97600-43-6 H Calixarene 1,4 O-Ethyl cone 144508-85-0 H Calixarene 1,4 O-Isopropyl cone 144508-84-9 H Calixarene 1,4 O-Tert-Butyl cone 97600-39-0 tert-Butyl Calixarene 1,4 O-Ethyl cone 160617-97-0 tert-Butyl Calixarene 1,4 O-Isopropyl cone 94530-27-5 tert-Butyl Calixarene 1,4 O-Tert-Butyl cone 149775-74-6 tert-Octyl Calixarene 1,4 O-Ethyl cone 152495-34-6 tert-Butyl Calixarene 1,5 O-Ethyl cone 123311-70-6 tert-Butyl Calixarene 1,4 tert-Butyl cone For calixarenes, cone-type and even partial cone-type cycle configurations are preferable to alternating 1,2 or alternating 1,3 type configurations, although not exclusive. According to a preferred embodiment, the composition does not comprise MEO of formula (V) or (VI) that allows the extraction of calcium ions, i.e., whose complexation constant Log K(Ca++) in methanol at 25°C is greater than 3. A preferred aspect of the invention is that the MEO of formula (V) or (VI) has a complexation constant Log K, in methanol at 25°C, of ​​the alkaline cationic species to be extracted, of a value greater than 3 and less than 11, preferably greater than 5 and less than 9. Furthermore, in the case of MEO selective for the extraction of alkaline cationic species, it may have a Log K value, in methanol at 25°C, of ​​less than 5, preferably less than 3 for alkaline earth cations, and in particular for calcium. These ester or ketone type MECs, of formula (V) or (VI), are particularly well adapted to the liquid-liquid extraction procedure by temperature difference according to the invention. MSA Compound The MSA can be a compound comprising from 6 to 50 carbon atoms, advantageously from 7 to 30 carbon atoms, and particularly from 8 to 20 carbon atoms, and which integrates at least one aromatic ring and at least one halogen atom or an electron-withdrawing group, particularly fluorinated. Advantageously, MSA is a compound with formula B: wherein at least one of the radicals Ra, Rb, Rc, Rd and Re, identical or different, is a halogen atom or an electron-withdrawing group, in particular a halogenated radical, from the following group: - F, Cl, Br, - CmF2m+i with m ≥ 4, where m is a non-zero integer, - CF2CF2CPH2P+1 with ps 4, where p is an integer, - CF2CpH2p+i with p ≠ 4, where p is an integer, - CH2CpF2p+1 with p 2 4, where p is an integer, - OCH2CF3, - C(=O)CF3, - CmHnFpClqBrs with m 2 4, where n, p, q, s are integers of which at least p, qos is non-zero, - C(=O)OCmH2m+i with m í 4, where m is an integer, and - C(=O)CmH2m.i with m 2 4, where m is an integer, the remaining radical(s) Ra, Rb, Rc, Rd and Re are chosen, identical or different, from the following non-electro-withdrawing radicals: - H, - CH3, - CH2CH3, - CH2CH2CpF2p+i with p 2 4, where p is an integer, - CmH2m-i with 3 2 m 2 10, where m is an integer, and - CmH2m+i with 3 2 m 2 10, where m is an integer; where only one of the radicals Ra to Re can be one of these last two radicals CmH2m-1 and CmH2m+1 and in which X is selected from the following radicals: OH, NH-R', where R' and R, identical or different, are chosen from the following radicals: - H, - CnH2n-i with 3 2 n 2 4, where n is an integer, - CnH2n+i with n ≤ 4, where n is a non-zero integer, - CH2CH2CpF2p+i with ps 2, op is an integer, - CH2CpF2p+i with p á 2, where p is an integer, - and an aryl radical of formula b: (b) where Ra, Rb, Rc, Rd and Re, identical or different, are as previously defined in formula B; and where R' is selected from the following radicals: - CmH2m+i with ms 20, preferably s 15, where m is an integer, - CmH2m-i with 3 sm á 20, where m is an integer, - CmHnFpClqBrs with ms 10, where n, p, q, s are integers of which at least p, qos is non-zero, - CH2CH2CpF2p+i with p < 4, where p is an integer, - CH2CpF2p+i with p ≥ 4, where p is an integer, - CF2CpH2p+i with ps 4, where p is an integer, - CF2CF2CpH2p+i with p < 4, where p is an integer, - CmF2m+i with m < 4, where m is a non-zero integer, - and an aryl radical of formula b: where Ra, Rb, Rc, Rd and Re, identical or different, are as previously defined in formula B. MSA compound - alcohol Such a compound is advantageously chosen from the group of fluorinated aromatics with an alcohol functional group and their derivatives. For example, this compound could be an alcohol derived from a phenyl methanol, such as 3-(Trifluoromethyl)benzyl alcohol (CAS No. 349-757). Preferably, this first compound is a phenylmethanolic compound advantageously comprising more than 3 fluorine atoms. Advantageously, this compound comprises at least two -CF3 radicals. According to one embodiment of the invention, this first MSA compound has radical X in formula B: which corresponds to a compound of formula A .C—R' \ R Ri, R2, R3, R4 and Rs, identical or different, but where any one of R1, R2 and R3 is a fluorinated radical, are chosen from the following radicals: - H, - F, - CmF2m+i with ms 4, where m is a non-zero integer, - CF2CF2CpH2P+i with p < 4, where p is an integer, and - CF2CpH2p+i with p < 4, where p is an integer; and in which R' and R, identical or different, are chosen from among the following radicals: - H - CnH2n-i with 3 to n to 4, where n is an integer, - CnH2n+i with n < 4, where n is a non-zero integer, - CH2CpF2P+i where ps 2, op is an integer, - CH2CH2CPF2P+1 where ps 2, op is an integer, - and an aryl radical of formula a: (a) where Ri, R2, R3, R4 and Rs, identical or different, are chosen from the group - H - F - CmF2m+i with m < 4, - CF2CF2CPH2p+i with p < 4, where p is an integer, - CF2CpK2p+i With ps 4, where p is an integer. MSA Compounds - Alcohol Advantageously, this first compound is chosen from the group consisting of the compounds described in Table I below: Table I: MSA Alcohol. Semi-developed formula Crude formula CAS No. Molar mass (g / mol) Density (g / cm3) Maximum [MSA] Mol / L Water solubility mMol / L pKa MSA1 F C8H7F3O 349-75-7 176.14 1.29 Liquid 7.32 32 14.6+ / -1.0 (estimated) MSA2 HO\ FFF C9H6F6O 32707-89-4 244.13 1.43 Solid 5.86 2.29 14.5+ / -1.0 (estimated) MSA3 F / HCk VF \ F / VF JL f Γ FFFT C15H6F1O 916975-23-0 544.18 1.62 2.98 0.0005 14.01 + / - 0.1 MSA4 C10H5F9O 312.13 1.53 4.90 0.39 13.59 + / - MSA Alcohol. Semi-developed formula Crude formula CAS No. Molar mass (g / mol) Density (g / cm3) Maximum [MSA] Mol / L Solubility in water mMol / L pKa HCh f F / KFFFF 1010101-84-4 0.1 MSA5 h0\ / CH3 ff Ί F Xf (XpF F C11H9F7O 131608-30-5 290.18 1.39 4.70 0.42 14.5 + / - 1.0 (estimated) MSA7 HO \ / ~~CH3 C12H12F6O 742097-71-8 286.21 1.30 Liquid 4.54 0.48 13.9+ / -1.0 (estimated) MSA8 C15H10F6O 1598-89-6 320.23 1.37 Liquid 4.28 0.07 13.3+ / -1.0 (estimated) According to one aspect of the invention, the hydrophobic organic liquid composition comprises at least one compound that allows the solvation of at least one anion. Preferably, these compounds are selected from the (MSA) type compounds described in this application. In particular, the liquid composition according to the invention may comprise a solid form of MSA, such as [3,5-Bis(Trifluoromethyl)phenyl]methanol (CAS No: 32707-89-4) combined with a hydrophobic liquid fluidifier or diluent. Alternatively, the liquid composition according to the invention may comprise a solid MSA (at operating temperatures), such as [3,5-Bis(Trifluoromethyl)phenyl]methanol (CAS No. 32707-89-4), associated with a liquid MSA (at operating temperatures) such as [(Trifluoromethyl)phenyl]methanol (CAS No. 349-75-7). In such a case, the liquid MSA1 has the dual function of MSA and fluidifier / thickener. The relative volume ratio of these compounds to each other may vary, but advantageously is within a ratio of 30 / 70 to 60 / 40 volume / volume (v / v). Preferably, this ratio is approximately 40 / 60 v / v, particularly for the MSA1 / MSA2 combination. MSA compounds - amide Such a compound is advantageously chosen from the group of fluorinated aromatics with an amide functional group and their derivatives. The compound MSA of formula B can also be an amide compound. In that case, the radical X in formula B is: CH2—NH where R' is as previously described, preferably, the amide is of formula: (C): where R' is selected from the following radicals: - CmH2m+i with ms 20, preferably 15 where m is an integer, - CmH2m-i with 3 < m ≤ 20, where m is an integer, and an aryl radical of formula b: wherein at least one of the radicals Ra, Rb, Rc, Rd and Re, identical or different, is a halogen atom or an electron-withdrawing group, in particular a halogenated radical, from the following group: - F, Cl, Br, - CmF2m+i with m ≠ 4, where m is a non-zero integer, - CF2CF2CpH2p+i with ps 4, where p is an integer, - CF2CpH2p+i with ps 4, where p is an integer, - CH2CpF2P+i with p < 4, where p is an integer, - OCH2CF3, - C(=O)CF3, - CmHnFpClqBrs with ms 4, where n, p, q, s are integers of which at least p, qos is non-zero, - C(=O)OCmH2m+i with m S4, where m is an integer, and - C(=O)CmH2m+i with ms 4, where m is an integer, the remaining radical(s) Ra, Rb, Re, Rd and Re are chosen, identical or different, from among the following non-electro-withdrawing radicals: - H, - CH3, - CH2CH3, - CH2CH2CPF2P+1 with p á 4, where p is an integer, - CmH2m-i with 3 sm á 10, where m is an integer, and - CmH2m+i with 3 sms 10, where m is an integer, where only one of the radicals Ra to Re can be one of these last two radicals CmH2m-1 and CmH2m+1. Preferably, the radical R' is an alkyl chain, linear or non-linear, and in particular an n-CzHis; n-CgHw; n-CnH23 or nC-i3H27 radical. These amide-type compounds are particularly well-suited to the liquid-liquid extraction process with thermal regeneration according to the invention. Other compounds of this type that can be used as MSAs for extraction compositions according to the invention are, for example: N-[3,5-Bis(trifluoromethyl)phenyl]acetamide (CAS No. 16143-84-3), N-[3,5-Bis(trifluoromethyl)phenyl]-2-chloroacetamide (CAS No. 790-75-0), N-[3,5-Bis(trifluoromethyl)phenyl]-2-bromoacetamide (CAS No. 99468-72-1), N-[3,5-N-trifluoromethyl)phenyl]-2-chlorobenzamide (CAS No. 56661-47-3), N-[3,5-N-trifluoromethyl)phenyl]-4-chlorobenzamide (CAS No. 56661-30-4), N-[3,5-N-trifluoromethyl)phenyl]-4-bromobenzamide (CAS No. 56661-31-5), N-[3,5-dichlorophenyl]acetamide (CAS No. 31592-84-4), N-[4-methyl-3,5-dichlorophenyl]acetamide (N°CAS. 39182-94-0), N-[3-fluoro-5-(trifluoromethyl)phenyl]acetamide (CAS No. 402-02-8), N-[2-fluoro-5-(trifluoromethyl)phenyl]acetamide (CAS No. 349-27-9), N-[4-chloro-3-(trifluoromethyl)phenyl]acetamide (CAS No. 348-90-3), N-[4-bromo-3-(trifluoromethyl)phenyl]acetamide (CAS No. 41513-05-7), N-[2,5-difluoro-3-(trifluoromethyl)phenyl]acetamide (CAS No. 1994-23-6), N-[3-(trifluoromethyl)phenyl]acetamide (CAS No. 351-36-0), N-[2-methyl-3-(trifluoromethyl)phenyl]acetamide (CAS No. 546434-38-2), N-[2-amino-3-(trifluoromethyl)phenyl]acetamide (CAS No. 1579-89-1), N-[3-(trifluoromethyl)phenyl]-2,2,2-trifluoroacetamide (CAS No. 2946-73-8), N-[3-(trifluoromethyl)phenyl]-2,2-dichloroacetamide (CAS No. 2837-61-8), N-[3-(trifluoromethyl)phenyl]-2,2,2-trichloroacetamide (CAS No. CAS. 1939-29-3), N-[4-chloro-3-(trifluoromethyl)phenyl]-2,2,2-trichloroacetamide (CAS No. 13692-04-1), N-[3-(trifluoromethyl)phenyl]-2-bromoacetamide (CAS No. 25625-57-4), N-[3-(trifluoromethyl)phenyl]propanamide (CAS No. 2300-88-1), N-[2-chloro-5-(trifluoromethyl)phenyl]propanamide (CAS No. 721-57-3), N-[3-(trifluoromethyl)phenyl](2,2-dimethylpropanamide) (CAS No. 1939-19-1), N-[2-methyl-3-(trifluoromethyl)phenyl](2,2-dimethylpropanamide) (CAS No. 150783-50-9), N-[4-chloro-2-methyl-3-(trifluoromethyl)phenyl](2,2-dimethylpropanamide) (N° CAS.112641-23-3), N-[3-(trifluoromethyl)phenyl](2-chloro-propanamide) (CAS No. 36040-85-4), N-[3-(trifluoromethyl)phenyl]butanamide (CAS No. 2339-19-7), N-[3-(trifluoromethyl)phenyl]isobutanamide (CAS No. 1939-27-1), N-[3-(trifluoromethyl)phenyl]cyclopentanecarboxamide (CAS No. 13691 -84-4), N-[3-(trifluoromethyl)phenyl](2-methyl-pentanamide) (CAS No. 1939-26-0), N-[3-(trifluoromethyl)phenyl](2,2-dimethylpentanamide) (CAS No. 2300-87-0), N-[3-(trifluoromethyl)phenyl](2-(4-bromophenyl)acetamide) (N° CAS. 349420-02-6), N-[3-(trifluoromethyl)phenyl]-1-adnanthanocarboxamide (N° CAS. 42600-84-0), N-[2-chloro-5-(trifluoromethyl)phenyl]octanamide (N° CAS. 4456-59-1). These molecules, used as MSAs, by their integration into a formulation that combines at least one MEC and optionally a fluidizer, allow the extraction of ionic species, and in particular hydrophilic salts, from water into the organic extracting phase. An MSA particularly suitable for use in an extraction process according to the invention is a molecule with the formula R = n-C7Hi5; n-CgHi9; n-CnH23 or n-CisH27, respectively called MSA9; MSA10; MSA11 and MSA12. A hydrophilic salt is understood to be a salt soluble in water at more than 1 g / L at 20°C, more particularly at more than 20 g / L at 20°C, and advantageously at more than 100 g / L of water at 20°C. FLUIDIFIER Since some of the MECs and MSAs are solid or viscous compounds at the operating temperatures of the extraction process, the use of a fluidizer is advantageous. Because the process according to the invention allows, in particular, the extraction of relatively high concentrations of salts, it is necessary to identify a fluidizer capable of dissolving at least 0.1 mol / L of accumulated MECs and MSAs. Indeed, traditional solvents such as acetone, ethyl acetate, heptane, dimethylformamide, nitromethane, methanol, ethanol, diethyl ether, or acetonitrile, for example, do not solubilize most known MECs at these concentration levels, and in particular the 16- to 32-atom ring macrocycles described above. In contrast, solvents or thinners such as dichloromethane, and particularly polar aromatic solvents, appear to be good candidates as solubilizers for this application. This can be explained by the similar nature of MSAs, which are generally aromatic compounds themselves. For example, 1,3-bis(trifluoromethyl)benzene (CAS No. 402-31-3) and, more preferably, benzyl benzoate (CAS No. 120-51-4), composed of two aromatic rings, meet this solubilization criterion for the formulations described. The presence of at least one electron-withdrawing group, such as a trifluoromethyl or chloride group, on one or two aromatic rings allows for the creation of particularly advantageous fluidizing compounds.Dichlorobenzene-type compounds (e.g., 1,2-dichlorobenzene (CAS No. 95-50-1)) and dichlorotoluene-type compounds (e.g., 2,4-dichlorotoluene (CAS No. 95-73-8)), their derivatives, and mixtures thereof are particularly well-suited diluents for diluting MECs according to the invention. Derivatives are understood to mean aromatic compounds substituted with the aforementioned trifluoromethyl group, such as a mixed-group solvent like 2,4-dichloro-(trifluoromethyl)benzene (CAS No. 320-60-5), but also diaromatic compounds such as diphenyl ether (CAS No. 101-84-8). It is also possible to choose an MSA in such a way that it combines the functions of MSA and diluent of MEC and / or other MSAs. According to a preferred aspect of the invention, the composition consists solely of the compounds MSA and MEC, and optionally in association with a fluidizing compound, thus constituting a composition consisting of MSA and MEC and a fluidizing compound. Another object of the invention relates to the use of these MSA compounds, and in particular MSA amides, for the extraction of salts and / or ions from an aqueous medium. Specifically, these compounds can be used, individually or in mixtures, in a composition or in a process according to the invention as described in this application. MSA concentration in the organic liquid composition According to a preferred aspect of the invention, the molar concentration of MSA (or a mixture of such compounds) in the composition according to the invention is at least 0.1 M. Preferably, this concentration is higher, at least 1 M, to allow for optimized extraction, particularly of hydrophilic anions. Depending on the anionic solvation efficiency of the chosen MSA, it can also be at least 2 M, advantageously at least 3 M, or, for example, at least 4 M. The concentration of MSA to be retained depends on its efficiency as an anion solvator. An excess of MSA that does not improve the extraction yield is undesirable. Similarly, a lack of flowability in the extraction composition due to a high concentration of MSA is also undesirable.In certain variations of the invention, MSA, or a mixture of MSAs, can be used pure in its liquid form (molar concentration of 7.32 M for [(Trifluoromethyl)phenyl]methanol (CAS No. 349-757) or 6.41 M for 3,5-bis(trifluoromethyl)aniline (CAS No. 328-74-5)). The final MSA concentration depends on the desired application and the relative cost of MSA and fluidizer to obtain the most cost-effective water deionization solution. Density, solubility, and viscosity According to an advantageous aspect of the invention, the MSA that allows the solvation of anions, in the organic liquid composition, and particularly the extracted organic liquid composition, of at least one anion, has a solubility in water, in its free or complexed form, of less than 0.1 mol / L, preferably less than 0.01 mol / L, preferably less than 0.0001 mol / L and particularly less than 1x10 5 mol / L. According to another advantageous aspect of the invention, the MSA of at least one extracted anion has a density greater than 1 kg / liter, advantageously greater than 1.1 kg / liter, and ideally greater than 1.2 kg / liter. This design choice is closely linked to the choice of fluidizer, which, with its higher density, can compensate for a lack of density in the MSA. According to another advantageous aspect of the invention, the liquid MSA or the mixture of MSA + fluidizer has a viscosity at 25 °C of less than 100 mPa.s, preferably less than 50 mPa.s, for example less than 20 mPa.s. Relative concentration of MSA and MEC in the organic liquid composition To ensure maximum extraction of ionic species, the concentrations of MSA and MEC are selected based on the concentration of the ionic species to be extracted in the aqueous solution. An aqueous solution is defined as a liquid comprising more than 50 mol% water. Thus, at equal volumes of salt water and extraction formulation, the concentration of the MEC compound is advantageously equimolar to or greater than the concentration of the cation to be extracted. A concentration approximately twice as high generally constitutes a limit beyond which cation extraction is not substantially improved. The concentration of MEC effectively retained is limited primarily by the solubilization capacity of the MEC in MSA alone or in the MSA+fluidizer mixture, and / or by the viscosity of the overall formulation obtained, and / or by the optimum point of overall technical and economic equilibrium. Surprisingly, a molar concentration of MSA considerably higher than that of the anion to be extracted may be necessary to achieve optimized extraction. Thus, at least double, preferably triple, even quadruple, quintuple, or sextuple, or even more, the concentration of the anion to be extracted may be required to obtain satisfactory results, particularly when the anion is the chloride anion. The effective MSA concentration is limited primarily by the solubilization capacity of the MSA in the MEC+fluidant mixture and / or by the viscosity of the resulting overall formulation and / or by the optimum point of the overall technical and economic balance. Thus, the relative molar ratio of MSA / MEC in a composition according to the invention for extracting a salt consisting of an anion and a cation is advantageously greater than or equal to 1, 2, 3, 4, 5, or 6. The choice of the relative molar ratio of MSA / MEC to be maintained for an industrial application depends on the relative cost of these compounds, the technical and economic data of the project, and the solvation activity of the anions of the chosen MSA. Preferably, this ratio is at least 4 for an alcohol MSA and is between 1 and 4 for an amide MSA. The MEC concentrations given in the examples are relative to the volume of the MSA+fluidifier mixture and, therefore, do not account for the increase in overall formulation volume caused by the dilution of a macromolecule such as these MECs. The actual MEC concentration is therefore generally less than 10 to 25%, although this range is not a limiting factor. Use of the composition according to the invention The composition according to the invention can be advantageously used to extract hydrophilic ions (cations; anions) from an aqueous phase. It is important to note that this ion extraction is not offset by the transfer of chemical species, ionic or otherwise, from the organic phase to the aqueous phase or vice versa. This composition is particularly suited for the selective extraction of ionic species from an aqueous solution comprising several salts and / or ionic species. Thus, it is particularly suited for the selective extraction of at least one non-alkaline cationic species from an aqueous saline solution. Anions and cations to be extracted The MEC and MSA compounds comprising the composition according to the invention are compounds that allow the extraction and solvation of at least two, and preferably several, ionic species. The two ionic species may constitute one or more hydrophilic salts. According to one object of the invention, the MEC and MSA are selected so that more than one salt, and preferably several salts, can be extracted from a saline solution containing them. Preferably, these salts comprise or are chloride salts. According to another object of the invention, these ions are the components, for example, of one or more alkaline earth salts as well as salts of certain metals, such as cadmium (Cd2+), lead (Pb2+), or silver (Ag+) salts. A salt is understood to be an ionic compound composed of cations and anions that forms a neutral product with no net charge. These ions can be either inorganic (chloride Cl·, calcium Ca++...), or organic (acetate CH3-COO-, ammonium R3NH+...) and either monatomic (fluoride F-, magnesium Mg2+...) or polyatomic (nitrates NO3·, bicarbonate HCO3·, sulfate SO42·...). Particularly preferred, the compositions comprising a mixture of MEC and MSA, with or without a fluidizer, according to the invention, can extract from a solution comprising: at least one alkali metal cationic species, at least one non-alkali cationic species, particularly divalent, and at least one complementary anionic species, with a much greater quantity of said non-alkali cationic species than of that of the alkali metal cationic species. Alternatively or additionally, the quantity of alkali metal cationic species extracted by this composition is very low. By "much larger relative quantity and very low extraction" it is understood that the extraction rates (in molar percentage) of the cation(s) to be extracted are at least twice as high as the extraction rates of the alkali cations in the treated aqueous solution. This ratio can advantageously be at least 5, or even more than 10. Certain compositions according to the invention allow ratios of 13 to be achieved, based on the initial concentration of cations to be extracted and those not extracted. It even allows the extraction of all the ions to be extracted (e.g., Ca) with hardly any alkali cations (e.g., Na), especially when the alkali cations are very abundant. The cation(s) to be removed are preferably chosen from the alkaline earth metal group, and particularly calcium, strontium, and / or barium. Removing these divalent cations, and especially calcium, which is the most commonly found in water, helps prevent scaling caused by calcium combining with specific anions. An alkali metal is a chemical element in the first column (group 1, excluding hydrogen) of the periodic table. Lithium, sodium, potassium, rubidium, cesium, and francium are alkali metals. These are single-charge (+). The extraction of alkaline earth cation salts is carried out by complexing the MEC for this cation and by tracking anions from the aqueous phase to the organic phase in order to ensure neutralization of the + / - charges. The follower anions, solvated by the MSAs, are primarily the least hydrophilic anions, that is, the anions with the highest hydration free energy. Thus, the preferred order of extraction of anions from the aqueous phase into the organic formulations according to the invention is: BF4·, I', Br, NO3·, Cl·, HCO3·, CH3COO·, p, SO42', CO32'. Therefore, in the case of extracted alkaline earth salts, iodide, bromide, nitrate, and / or chloride salts will be the primary ones extracted. Since these salts are highly soluble in water, even at high water temperatures (CaCl2 is soluble in water at concentrations exceeding 40% by weight), they can be supplied as concentrated brine during the thermal regeneration stage of the solvent.The alkaline earth or metallic salts extracted according to the invention thus allow the separation of cations from anions at the beginning of scaling and potentially constituting scale-forming salts, transforming them into two distinct aqueous effluents. The partially deionized water according to the invention then consists of the most hydrophilic anions, namely fluorides, sulfates, and carbonates, and the unextracted alkali cations. This water, therefore, has lost all scale-forming capacity. It is softened. This is also the case for the water from the thermal regeneration of the process according to the invention, which consists mainly of alkaline earth and metallic chloride salts.Thus, the objective of the invention is to eliminate the scale barrier in a number of industrial applications by preventing the combined presence in the same effluent of cations and anions that, when combined, are insoluble or poorly soluble in water. The salts to be separated are, therefore, primarily carbonate salts (MgCCh, CaCO3, SrCCh, BaCCh, CdCO3, CoCO3, MnCO3, PbCCh, N1CO3, FeCO3, ZnCO3, etc.), sulfate salts (CaSO4, SrSO4, BaSO4, PbSO4, etc.), and fluoride salts (MgF2, CaF2, SrF2, BaF2, CdF2, FeF2, PbF2, etc.). The control of the precipitation of metal hydroxide salts (Mg(OH)2, Ca(OH)2, Cd(OH)2, Co(OH)2, Fe(OH)2, Ni(OH)2, Zn(OH)2...) is regulated by adjusting the pH of the water or by a salt precipitation of the extracted divalent cations towards water of neutral pH and even slightly acidic. The cations preferably extracted according to the invention are Ca2+, Sr2+, Ba2+, Pb2+, Cd2+, and silver Ag+. This list is not exhaustive of transition metals. The compositions according to the invention can also be used in methods according to the invention to extract Ca++, Sr++ and / or Ba++ in an organic phase. For the more hydrophobic anions such as perchlorates ClO4·, permanganates MnO4', picrates, lower concentrations of MSA are sufficient to effect their transfer to the organic phase in combination with at least one cation extracted by an MEC. The composition according to the invention is therefore particularly capable of being used in an extraction process as described in the present application and in particular a liquid-liquid extraction water deionization process with thermal regeneration. According to a preferred embodiment, the composition does not comprise any MEC that allows the extraction of sodium chloride, i.e., whose sodium complexation constant in methanol at 25°C, Log K(Na+) is greater than 3. According to a particular aspect of the invention, magnesium chloride salts are only slightly extracted or not extracted at all due to the use of MEC whose magnesium complexation constant in methanol at 25°C, Log K(Mg2+) is less than 3. LIQUID-LIQUID EXTRACTION PROCESS The invention also relates to a liquid-liquid extraction process of a non-alkaline cationic species from a saline aqueous solution, said saline aqueous solution comprising at least one non-alkaline cationic species, one alkali metal cationic species, and one complementary anionic species, said process comprising the following steps: a) the mixing in a first reactor, at a first temperature, of a liquid hydrophobic organic phase and of said saline liquid aqueous solution, for the subsequent obtaining of a treated liquid aqueous solution and of a liquid hydrophobic organic phase loaded with said non-alkaline cationic species and complementary anionic species, said liquid hydrophobic organic phase comprising an extractant molecule of said non-alkaline cationic species, a solvating molecule of said complementary anionic species and, optionally, a fluidifier; b) the separation, on the one hand, of the treated liquid aqueous solution and, on the other hand, of said liquid organic phase loaded with said complementary non-alkaline cationic and anionic species; said procedure being characterized by the fact that said extractant molecule of the non-alkaline cationic species is an MEC as previously described and that said solvating molecule of the complementary anionic species is an MSA advantageously as previously described, in particular an amide-type MSA Preferably, a subsequent step c) is carried out in which, at a second temperature preferably higher than the first, in liquid phase, in a second reactor, said liquid organic phase loaded with said non-alkaline cationic and complementary anionic species and a liquid aqueous regeneration solution are mixed, to subsequently obtain a regenerated liquid organic phase and a liquid aqueous regeneration solution loaded with said non-alkaline cationic and complementary anionic species, wherein the difference between said first and second temperatures ranges from 30°C to 150°C, preferably from 50°C to 100°C. The term non-alkali cation or non-alkali cationic species is intended to exclude cations derived from alkali metals. Preferably, non-alkali cationic species are divalent cations, such as alkaline earth metal cations. The process according to the invention is particularly suited to the extraction of one of the following cations: calcium, strontium, and barium. It can also be applied to monovalent metallic cations such as silver (Ag+), or to divalent metallic cations such as lead (Pb2+) and cadmium (Cd2+). According to a preferred aspect of the invention, the cationic species of an alkali metal is the sodium ion (Na+). Advantageously, this is only slightly extracted, or not extracted at all, from the saline solution. Non-alkali metal salts are composed of the aforementioned cations and a complementary anionic species. The term "complementary anionic species" indicates that the charge of the anionic species corresponds to that of the cationic species, neutralizing it and thus forming a salt with a neutral charge. The MECs and MSAs, as well as the eventual fluidizer, are as described above. Alternatively, MSA can also be a hydrophobic, and preferably protic, compound whose pKa in water at 25°C is at least 9, preferably at least 10.5 and is preferably lower than the pKa of water at 25°C, or at least lower than 15 at 25°C. The MEC can also be an organic and hydrophobic compound that has a complexation constant for the non-alkali cationic species to be extracted with a Log K value, in methanol at 25°C, greater than 3 and less than 11, preferably greater than 5 and less than 9. In addition, in the case of MECs selective for the extraction of non-alkali cationic species, it can have a Log K value, in methanol at 25°C, less than 5, preferably less than 3 for alkali cations, and in particular for sodium. The pKa (or acidity constant) is defined by pKa = -log(Ka), where Ka is the acid dissociation constant that is measured in a standard way for such pKa. The recommended standard measurement method for high, basic pKa is preferably that described by Popov et al, IUPAC - Guidelines for NMR measurements for determination of high and low pKa Puré Appl. Chem., Vol. 78, No. 3, pp. 663–675, 2006. K is the complexation constant of a MEC and a non-alkali cation in methanol, at 25°C, which is measured according to the standard method of isothermal titration calorimetry. According to a particular aspect of the invention, the non-alkali cationic species is selectively extracted with respect to the alkali metal cationic species. This selection can reach the levels previously described. Contrary to many known ion extraction procedures, the procedure according to the invention does not rely on a change in pH to enable either the absorption or the salt precipitation of the captured ions, particularly through acid-base mobility of the hydrogen ion (H+). Thus, a preferred aspect of the invention is that the procedure does not comprise any step where the pH of the regeneration liquid aqueous solution is significantly modified, i.e., beyond a pH variation of + / - 2, for example, ±1, relative to the water being treated. According to a preferred aspect of the invention, the procedure does not include, in the regeneration step of the ion extraction solvent, the addition, use, or presence of compounds to modify the pH of the regeneration liquid aqueous solution, such as acids or bases, particularly inorganic acids such as sulfuric, hydrochloric, or nitric acids, or bases such as sodium hydroxide or potassium hydroxide. Furthermore, this process advantageously allows the extraction from the water being treated of at least one alkaline earth cationic species as well as anionic species such as Br or Cl' ions. It is worth noting that such anionic species are hydrophilic and particularly difficult to extract from an aqueous medium. A particularly advantageous aspect of the process according to the invention is that it allows the simultaneous extraction from an aqueous phase of cations, particularly Ca++ cations, and anions, particularly Cl· anions, and for concentrations of extracted salts that can potentially exceed 0.1 mol / L. STAGE a) The mixing step (a) of the aqueous saline solution and the hydrophobic organic phase can be carried out by agitation of the two liquid phases, for example by mechanical or orbital agitation, by the development of highly turbulent fluids, and / or by vertical interpenetration (static or agitated gravity column) when these two phases have different densities. The technological choice associated with implementing the procedure that is the object of the invention depends on the salt transfer kinetics associated with the procedure and the operating temperatures considered. It may be necessary to repeat these mixing steps (a) to achieve the desired salt extraction efficiency. In such cases, the fluids of the saline solution to be treated and the organic phase may flow in countercurrent flow in the mixing reactors for maximum deionization efficiency. It is also preferred that the mixing step a) not be done under conditions that lead to a microemulsion or a stable emulsion and that in all cases the chosen MSA does not have surfactant-type activity. STAGE b) Step b) of separating the aqueous and organic phases can advantageously be a simple gravity settling of the organic and liquid aqueous phases. This settling can take place in the reactor where mixing occurs. Alternatively, separation can be achieved by applying an external means, for example, centrifugation, possibly in a centrifuge separate from the reactor where the aqueous and organic phases are mixed. The settling time of the two phases is an important parameter of the process due to the volume of organic phase immobilized. Furthermore, a density difference between immiscible liquid phases of more than [missing value] is preferred. 0.1 kg / L, or even more than 0.2 kg / L. The organic phase is then advantageously chosen as having a higher density than the density of the water to be treated, the treated water, and the regenerated saline water produced. Alternatively, the organic phase can be chosen as having a lower density than the density of the water to be treated and the treated water. In both of these cases, the density difference must be sufficient to allow effective settling of the two phases when this type of mixture is used. In these two cases, if the density difference between the immiscible liquid phases used in the process is less than 0.1 kg / L, the use of a centrifugal settling system capable of separating liquid phases with a density difference of only 0.05 kg / L can be considered. STAGE c) Once the phases are separated, the liquid organic phase, laden with ionic species, is advantageously directed to one or more second reactors where, after being heated, it is brought into contact with liquid water. The regeneration water in this second reactor has a higher temperature than the first. This regeneration of the organic phase in hot water allows for more efficient deextraction of the salts absorbed in stage a), the hotter the regeneration water. This, therefore, allows for a reduction in the volume of regeneration water, an increase in the productivity of the liquid organic phase, a reduction in the number of desorption reactors used, and / or the production of regeneration water laden with highly concentrated deextracted salts.With the exception of temperature, this mixing step (c) that allows for the de-extraction of salts can be carried out under similar operating conditions to those described for mixing step (a) that allows for the extraction of salts. However, certain conditions, such as pressure, may vary to, for example, prevent the water or the fluidizer from boiling. Furthermore, performing this regeneration step of the extractant composition at a higher temperature impacts the hydrodynamics of the fluids, resulting in a decreased viscosity of the organic phase. This favors the settling of the phases and the kinetics of salt transfer between phases, potentially leading to the selection of a different technology than that used in step (a).The regeneration water or liquid aqueous solution will be chosen so that it is compatible with the extracted salts, in particular to avoid any scaling problems, especially in the heat exchangers cooling the hot water outlet from this stage. TEMPERATURE According to an advantageous aspect of the invention, step a) is carried out at room temperature. It is also advantageous that the saline solution is not subjected to a preheating or precooling step. Alternatively, there may be a preheating or precooling step. In such a case, it is preferable that the saline solution not be heated or cooled by more than 5°C, advantageously more than 2°C, relative to the saline solution to be treated. According to another advantageous aspect of the invention, the first temperature is a temperature below 50°C and above 0°C. This temperature can be advantageously selected from ranges from 10°C to 40°C, preferably from 15°C to 30°C, and particularly from 19°C to 26°C (e.g., 25°C). By temperature range from 10 'C to 50°C, we mean temperatures of 10 °C, 11 'C, 12 °C, 13 °C, 14 °C, 15'C, 16 °C, 17 °C, 18 °C, 19'0, 20 'C, 21 'C, 22 °C, 23 'C, 24'C, 25 'C, 26 'C, 27 'C, 28 °C, 29 'C, 30 'C, 31 'C, 32 'C, 33 'C, 34 °C, 35 °C, 36 'C, 37 'C, 38 °C, 39 °C, 40 °C, 41 'C, 42 °C, 43 °C, 44 °C, 45 'C, 46 °C, 47 °C, 48 °C, 49 °C or 50 'C. According to another particularly advantageous aspect of the invention, the second temperature is above 60°C, preferably above 85°C. This temperature can be chosen from ranges from 60°C to 150°C, preferably from 85°C to 125°C, and particularly from 90°C to 120°C (for example, 95°C). Por rango de temperatura que va de 60 °C a 150°C, se entiende temperaturas de 60 ’C, 61 ’C, 62 ’C, 63 ’C, 64 ’C, 65 ’C, 66 ’C, 67 ’C, 68 ’C, 69 °C, 70 ’C, 71 ’C, 72 ’C, 73 ’C, 74 ’C, 75 °C, 76 ’C, 77 ’C, 78 °C, 79 °C, 80 °C, 81 °C, 82 ’C, 83 °C, 84 ’C, 85 ’C, 86 ’C, 87 ’C, 88 ’C, 89 ’C, 90 ’C, 91 ’C, 92 ’C, 93 ’C, 94 ’C, 95 ’C, 96 ’C, 97 ’C, 98 ’C, 99 ’C, 100 ’C, 101 ’C, 102 ’C, 103 ’C, 104 ’C, 105 ’C, 106 ’C, 107 ’C, 108 ’C, 109 ’C, 110 ’C, 111 ’C, 112 ’C, 113’C, 114’C, 115’C, 116’C, 117’C, 118’C, 119’C, 120 ’C, 122 ’C, 124’C, 125 ’C, 126 ’C, 127 ’C, 128 ’C, 129 ’C, 130 ’C, 131 ’C, 132 ’C, 133 ’C, 134 ’C, 135 ’C, 136 ’C, 137 ’C, 138 ’C, 139’C, 140 ’C, 141 ’C, 142 ’C, 143 ’C, 144 ’C, 145 ’C, 146 ’C, 147 ’C, 148 ’C, 149 ’Co150’C. The first and second temperatures are necessarily selected so that the mixture remains in a liquid state at the operating pressure and the techno-economic performance of the invention is maximized. It is particularly advantageous that the difference between these temperatures, ΔT, be chosen within a range of 30°C to 150°C, preferably 50°C to 100°C. By ΔΤ that goes from 50 'C to 100 'C, a ΔΤ of 50 'C, 51 'C, 52 'C, 53 'C, 54 'C, 55 'C, 56 'C, 57 'C, 58 'C, 59 'C, 60 'C, 61 'C, 62 'C, 63 'C, 64'C, 65'C, 66'C, 67'C, 68'C, 69'C, 70'C, 71'C, 72'C, 73'C, 74'C, 75'C, 76'C, 77'C, 78'C, 79°C, 80°C, 81°C, 82°C, 83 °C, 84 °C, 85 °C, 86 °C, 87 °C, 88 °C, 89 °C, 90 °C, 91 °C, 92 °C, 93 °C, 94 °C, 95 °C, 96 °C, 97 °C, 98 °C, 99 °C or 100 °C. Also, if the first temperature is 20 °C, the second temperature will be more than 50 °C, advantageously more than 70 °C, for example 80 °C. Therefore, the procedure of the invention may comprise a first step a) that allows the transfer of specific ionic species, which are preferably complementary, from the saline liquid aqueous solution to be treated to the organic phase, at room temperature, followed by a step c) that allows the regeneration of the organic phase loaded with ionic species, preferably complementary, and which takes place at a temperature higher than room temperature but relatively low to come from renewable geothermal, solar or other energies (for example below 150 °C). According to a preferred aspect of the procedure, it comprises the following subsequent steps of: d) separation of said regenerated liquid organic phase and of the water or liquid aqueous regeneration solution loaded with said ionic species which are preferably complementary, e) indirect thermal contact, for example by heat exchanger, of said liquid organic phase loaded with ionic species and of said regenerated liquid organic phase. According to a particular aspect of the invention, it is advantageous that the process comprises heating and / or cooling stages of: - the organic phase charged with ionic species, - the organic phase, particularly the regenerated one, not charged with ionic species, - water, or aqueous solution, for regeneration, and - regeneration water, or aqueous solution, charged with discharged ionic species; that precede the introduction of these various phases or waters into the first and second reactors. Such heating stages can be carried out wholly or partly through heat exchanges between at least two of the various phases mentioned above (i.e., between the charged organic phases and in particular regenerated, not charged with ionic species, or between the aqueous phases which are water, and an aqueous, regeneration solution or between water and an aqueous, regeneration solution charged with discharged ionic species). In particular, the process according to the invention comprises a water heating step, or a regeneration aqueous solution heating step, carried out before step c) and / or comprises a heating step of the organic phase loaded with ionic species carried out before step c). Thermal regeneration of the extractant composition allows, for example, a reduction by a factor of two in the number of regeneration steps required before recycling it within the process. This advantage appears to be even more significant when using a resin with high MEC and, consequently, salt loading rates. Increasing the regeneration temperature allows for a reduction in the number of successive stages of contacting distilled water or regeneration water, thus enabling greater salt removal each time. PRESSURE The mixing stages a) and / oc) are advantageously carried out at atmospheric pressure of approximately 1 atm at sea level, or without the application of pressure means other than the weight of the liquids present in the reactor. If pressure is applied, it can be positive or negative. Such pressure can range from 0.8 atm to 80 atm, preferably from 1 to 10 atm. USE OF TREATED WATER Advantageously, the water or liquid aqueous regeneration solution used in step c) comes from the treated saline aqueous solution obtained after step a) after further treatment that prevents any risk of scaling during steps c), d) or e). Alternatively, it can come from an external source. COMPOSITION The organic phase comprises, or is essentially constituted by, the composition according to the invention described in this application. This composition is particularly effective for employing this process. Compositions particularly adapted for carrying out the process according to the invention comprise compositions associating an MSA amide with at least one of the MEC-type compounds as described above and optionally with a fluidizer. In the description of the invention, this composition may also be referred to as solvent or liquid resin. DEVICE - The invention also relates to a device for extracting at least one non-alkaline cationic species and at least one complementary anion, present in a liquid aqueous saline solution comprising: - a first reactor comprising a liquid hydrophobic organic phase or composition according to the invention as described in the present application. This device can advantageously understand: - a first reactor comprising said hydrophobic liquid organic composition and optionally the aqueous saline solution, in liquid state, for the subsequent obtaining of a treated aqueous saline solution and a hydrophobic liquid organic phase loaded with said non-alkaline cationic and complementary anionic species, said first reactor further comprising first mixing means and first means for the separation, on the one hand, of said liquid treated aqueous saline solution and, on the other hand, of said loaded liquid organic phase, - a second reactor comprising a liquid hydrophobic organic phase loaded with at least said non-alkaline cationic species and at least one complementary anion that neutralizes its charge and with a regeneration water, or aqueous solution, for the subsequent obtaining of a liquid aqueous regeneration solution loaded with said ionic species and with a regenerated organic phase, wherein said second reactor includes second mixing means and second means for the separation, on the one hand, of said regeneration saline solution loaded with ionic species and, on the other hand, of said regenerated organic phase; - eventually, means of temperature control in said second reactor; - communication means that allow the transfer between the first and second reactors of: - said liquid aqueous regeneration solution that can be extracted from said first reactor - said loaded liquid hydrophobic organic phase extracted from said first reactor - said regenerated liquid hydrophobic organic phase extracted from said second reactor - said liquid regeneration water loaded with salts from said second reactor; and, - a heat exchanger that combines, on the one hand, a portion of said loaded liquid hydrophobic organic phase extracted from said first reactor and, on the other hand, said regenerated liquid hydrophobic organic phase extracted from said second reactor; and optionally, - a heat exchanger that combines, on one side, said regeneration water, or liquid aqueous solution, and, on the other side, said liquid regeneration water loaded with complementary extracted ionic species. According to a particular aspect of the invention, the reactors, and particularly the parts of these reactors that are not movable, are not made of stainless steel. According to another particular aspect of the invention, the first reactor(s) do not comprise heating (radiators) or cooling (refrigerant) means. According to another particular aspect of the invention, the organic phase present in the device comprises, or is essentially constituted by, or consists of the composition according to the invention described in the present application. The device according to the invention can be advantageously installed in series to allow successive treatment stages of the water to be treated in order to reduce the content of the ionic species in the water until pure and / or purified water free of the ionic species to be extracted is obtained. Such a device is also covered by the present invention. Likewise, the device according to the invention can be advantageously installed in series to allow successive regeneration stages of the salt-loaded liquid hydrophobic organic phase in order to reduce the ionic species content in the resin until a resin sufficiently purified of the extracted ionic species is obtained. Such a device is also covered by the present invention. The invention also relates to a liquid-liquid extraction process for a salt or a mixture of salts composed of at least one hydrophilic anion, such as chloride (see Examples 1 and 2). The extracted cations can have an ionic radius between 55 pm and 180 pm, advantageously between 70 pm and 167 pm. Such cations are particularly lithium, sodium, potassium, rubidium, and cesium cations, which are monovalent cations, or calcium, strontium, or barium cations, which are divalent cations, including transition metal cations. This procedure comprises the following stages: (i) the mixing in a first reactor, at a first temperature, of a liquid hydrophobic organic phase and said saline liquid aqueous solution, for the subsequent obtaining of a treated liquid aqueous solution and a liquid hydrophobic organic phase loaded with said cationic species and complementary anionic species, said liquid hydrophobic organic phase comprising an extractant molecule of said cationic species of the type described above, a solvating molecule of said complementary anionic species and, optionally, a fluidifier; (ii) the separation, on the one hand, of the treated liquid aqueous solution and, on the other hand, of said liquid hydrophobic organic phase loaded with said complementary cationic and anionic species; said procedure being characterized by the fact that said extractant molecule of the cationic species is an MEC as previously described for macrocycles of 16 to 22 atoms, particularly carbon, and that said solvating molecule of the complementary anionic species is an MSA advantageously as previously described. Advantageously, the procedure includes a subsequent regeneration step of the hydrophobic organic liquid phase, which can be of the same type as previously described. Advantageously, the regeneration temperature is between 60°C and 150°C, preferably between 90°C and 120°C. The compounds and other procedural conditions may advantageously be those described with reference to the extraction procedure for non-alkaline cationic species. Likewise, the invention relates to a device that enables the implementation of the procedure and is substantially equivalent or identical to the device described above. DESCRIPTION OF THE FIGURES The invention will be better understood by reading the accompanying figures, which are provided as examples and are not intended to be limiting, in which: Figure 1 is a graph showing the evolution of the concentration in mMol / L of the five ions Na+, K+, Mg2+, Ca2+ and Cl* of a salt water initially at 180 g / L after 4 contacts in series with a composition of 0.4Mol / L of MEC1 and 1.2Mol / L of MSA9, all dissolved in 1,2-dichlorobenzene according to the invention, where at each stage the extraction equilibrium is allowed to be reached before proceeding to the next, as described in Example 2. Figure 2 is a graph showing the extraction rates in molar %, at room temperature, of 7 salts, LiCl, NaCl, KCl, MgCh, CaCl2, SrCl2 and BaCl2, extracted individually from salt water of initial concentration 0.1 Mol / L using a composition of 0.1 Mol / L of MEC2 and 3.5 Mol / L of MSA2, all diluted in dichloromethane according to the invention, expressed as a function of the ionic radius of the cation, as described in Example 3. Figure 3 is a graph showing the absorption isotherms of CaCI2 at room temperature and 80°C of a composition of 0.1 Mol / L of MEC2 and 1 Mol / L of MSA9, all dissolved in 1,2-dichlorobenzene according to the invention, as described in Example 4. Figure 4 is a graph showing a comparison of two regeneration phases at 20°C and 80°C of a composition of 0.1 Mol / L of MEC2 and 1 Mol / L of MSA9, all dissolved in 1,2-dichlorobenzene according to the invention, which has been loaded with CaCI2 to the level of 80 mMol / L before the initiation of several successive de-extraction phases in distilled water, as described in Example 5. Figure 5 is a table presenting the extraction rates in molar %, at room temperature, of 7 salts, LiCl, NaCl, KCl, MgCl2, CaCl2, SrCl2 and BaCl2, extracted individually from salt water of initial concentration 0.1 Mol / L by using a composition of 0.1 Mol / L of MEC1 to MEC8 and 3.5 Mol / L of MSA2 for MEC1 and MEC2, or 1 Mol / L of MSA9 for MEC3 to MEC8, all diluted in dichloromethane for MEC1 and MEC2 or in 1,2-dichlorobenzene for MEC3 to MEC8 according to the invention, expressed as a function of the ionic radius of the cation, as described in part in Examples 1 and 3. Figure 6 represents the NMR spectrum of compound MSA11. EXAMPLES Description of the MECs used in the implementation of the invention Different ion-extracting compositions according to the invention are exemplified. The 12 MECs used in these compositions are as follows: Nombre Nomenclatura Formula desarrollada MEC 1 4-tert-butil-Calix[4]areno tetrakis(N,Ndietilacetamida), n° CAS 114155-16-7, C68H100N4O8, PM= 1101,5 g / mol, MP= 223-226°C, Log K(Li+, MeOH, 25’C) = 4,0 Log K(Na+, MeOH, 25°C) = 7,9 Log K(K+, MeOH, 25’C) = 5,8 Log K(Rb*, MeOH, 25°C) = 3,8 Log K(Cs+, MeOH, 25’C) = 2,5 Log K(Mg++, MeOH, 25’C) < 1,2 Log K(Ca++, MeOH, 25’C) > 9,0 Log K(Sr+, MeOH, 25°C) > 9,0 Log K(Ba*+, MeOH, 25’C) = 7,2 λ-i ''ffCKs MEC 2 4-tert-butil-Calix[6]areno hexakis(N,Ndietillacetamida), n°CAS 111786-95-9, C102H150N6O12, PM= 1650 g / mol, Log K(Li+, MeOH, 25’C) = 2,6 Log K(Na+, MeOH, 25’C) = 2,8 Log K(K*, MeOH, 25°C) = 3,3 Log K(Rb+, MeOH, 25’C) = 2,6 Log K(Cs+, MeOH, 25’C) = 2,8 Log K(Mg++, MeOH, 25’C) = 1,3* Log K(Ca+\ MeOH, 25’C) = 8,2* Log K(Sr+, MeOH, 25°C) = 8,1* Log K(Bat+, MeOH, 25’C) = 8,3* *Calci 6 *° C-CH3 ^c-ch3 2 liados MEC 3 4-tert-butil-Calix[4]areno tetrakis(Npiperidinilacetamida), n° CAS 353236-41-6 C72H100N4O8, PM= 1148,6 g / mol, MP= 272-276°C X.4 <0 MEC 4 4-tert-butil-Calix[4]areno tetrakis(Npirrolidinilacetamida), n° CAS 133801-01-1 C68H94N4O8, PM= 1094 g / mol, Log K(Li+, MeOH, 25’C) = 3,0 Log K(Na*, MeOH, 25’C) = 7,2 Log K(K+, MeOH, 25’C) = 5,4 Log K(Rb+, MeOH, 25’C) = 3,0 Log K(Cs+, MeOH, 25’C) = 1,0 Log K(Mg++, MeOH, 25’C) = 1,2 Log K(Ca++, MeOH, 25’C) = 7,8 Log K(Sr+, MeOH, 25’C) = 8,1 Log K(Ba++, MeOH, 25’C) = 6,8 ó 4. MEC 5 4-tert-butil-Calix[4]areno tetrakis(N,N-di-npropilacetamida), n° CAS 162714-60-5 C76H116N4O8, PM= 1212,46 g / mol, MP= 191-194°C 4 MEC 6 4-tert-butil-Calix[4]areno tetrakis(N,N-etiln-propilacetamida), C72H108N4O8, PM= 1156 g / mol, i J4 MEC 7 4-tert-butil-Calix[4]areno tetrakis(N,N-di¡so-butilacetamida), C84H132N4O8, PM= 1324,46 g / mol, MP= 164-167°C MEC 8 4-tert-butil-Calix[4]areno tetrakis(N,N-diiso-propilacetamida), C76HH6N4O8, PM= 1212 g / mol, MEC 9 4-tert-butil-Calix[8]areno octakis(N,Ndietilacetamida), n° CAS 315191-66-1, CiseHaooNeOle, PM= 2100 g / mol, Log K(L¡+, MeOH, 25’C) = 2,1* Log K(Na+, MeOH, 25’C) = 2,2* Log K(K+, MeOH, 25’C) = 2,2* Log K(Rb*, MeOH, 25’C) = 1,9* Log K(Cs*, MeOH, 25’C) = 2,0* Log K(Mg++, MeOH, 25’C) = 1,3* Log K(Ca++, MeOH, 25’C) = 7,2 Log K(Sr++, MeOH, 25’C) = 7,2* Log K(Ba++, MeOH, 25’C) = 8,6* ‘Calculados 8 ^C-CHa Ha MEC 10 tetraetil éster de ácido 4-tertButilcalix[4]areno-tetraacético, n° CAS 97600-5-8, C6oH80Oi2, PM= 993,27 g / mol, Log K(Li+, MeOH,or, MEC 11 4-tert-Butylcalix[5]arene-pentaacetic acid pentaethyl ester, CAS No. 152495-34-6, C75Hioo015, MW= 993.27 g / mol, Log K(Li+, MeOH, 25°C) = 1.0 Log K(Na+, MeOH, 25°C) = 4.4 Log K(K+, MeOH, 25°C) = 5.3 Log K(Rb+, MeOH, 25°C) = 5.6 Log K(Cs+, MeOH, 25°C) = 5.5 HjC-C-0 MEC 12 hexaethyl ester 4-tertButylcalix[6]arene-hexaaacetic acid, CAS No 92003-62-8, CsoHwChe, PM= 1489.93 g / mol, I Γ~Χ θ*° “ITW2> All of these MECs are solids that are completely insoluble in water. Generic description of the exemplified implementation forms Extraction composition The extraction composition is obtained by solubilizing a quantity of MEC and MSA in the chosen fluidizer, dichloromethane (CH2Cl2), a dichlorobenzene, a dichlorotoluene, or any other fluidizer capable of solubilizing the MEC / MSA mixture to obtain the desired final concentrations after solubilizing the MEC and MSA in a minimum of 3 milliliters of fluidizer. If the chosen fluidizer is also an MSA compound, then the volume of MSA used must be at least 3 milliliters. The given concentrations of MSA2 and MSA9 are relative to the volume of fluidizer added, and the concentrations of MEC are relative to the volume of fluidizer plus MSA added. The organic extraction composition is then gently heated to promote solubilization of the organic compounds using a hot air gun (temperature of approximately 50 to 60°C) for a few seconds (10 to 30 seconds) until a clear solution is obtained.The composition is then left to stand for 24 hours at room temperature to ensure the stability of the resulting formulation. These sealed formulations are then placed under orbital shaking at 500 revolutions / minute for 2 hours after adding an equivalent volume of distilled water twice in order to allow water saturation of the entire formulation and pH control at inlet and outlet (pH of around 7, or at least maintained after contact with saturation water). The extracted mixture is then allowed to settle by decantation. All the mixtures are stable and settle quickly (a few minutes at most) into two distinct phases. Salt water - brine that contains particularly salts to be extracted An aqueous solution of the chloride salt(s) in question (NaCl or others) is prepared from twice-distilled water. The chloride salts used are: LiCl, NaCl, KCl, MgCl2, CaCl2, SrCl2, and BaCl2. Extraction / Deextraction mL of the prepared organic extraction composition are then collected in the lower phase of the decanted biphasic mixture and transferred to a flask containing 3 mL of water containing the chloride salt(s) considered (NaCl or other), and then the flask is sealed and subjected to orbital shaking (at 500 revolutions per minute), for 2 hours at room temperature (TA) i.e. between 20 and 25°C. In the case of extraction or de-extraction tests at higher temperatures, particularly at 60°C or 80°C, magnetic stirring (at 500 revolutions per minute) is carried out for 2 hours, with indirect thermostatic heating in a metal mold on a heating plate. During agitation, it is verified that droplets of approximately 1-2 mm are present to ensure that equilibrium is reached in the distribution of the chloride salt (NaCl or another) between the two liquid phases at the end of the agitation. The organic and aqueous phases appear clear and colorless or slightly cloudy. Once the two hours of stirring have been completed, stirring is stopped and the mixture is allowed to settle for approximately 10 minutes, or until the two phases have completely separated, at the test temperature. The upper aqueous phase is then collected, stirred, and diluted for salinity analysis by ion chromatography (using a Metrohm™ device that integrates a cation analysis column and an anion analysis column tailored to the desired ions and salt concentrations). Similarly, the initial aqueous chloride salt solution (NaCl or another) is also analyzed by this ion chromatography to determine its relative molar concentration of cations and chlorides before extraction. All extractions and analyses are performed in duplicate. Example 1: extractions at room temperature of saline solutions in monosalts with the MEC1. In this example, the MEC used is 4-tert-butyl-Calix[4]arene tetrakis(N,N-diethylacetamide) (MEC1 of CAS No: 114155-16-7). It was synthesized from 4-tert-Butylcalix[4]arene of crude formula C44H56O4 and CAS No. 60705-62-6, purchased from TCI Chemicals, according to the synthesis procedure described in the publication “Selective alkali and alkaline earth cation complexation by calixarene amides, New J.Chem, 1991,15,33-37”. The MSA used is MSA2, CAS No. 32707-89-4; C9H6F6O, MW = 244.13 g / mol, a white solid available from various suppliers. Its characteristics are as follows: Parameters Values ​​Units Density (1.433) kg / L Viscosity - mPa.s BP 255 °C MP 55 °C FP 97 °C Log P 3.0 (estimated) - Solubility 2.29 mmol / L pKa 14.7+ / - 1 - The extractant composition considered comprises 0.1 mol / L of MEC1 and 3.52 mol / L of MSA2 in dichloromethane (CH2Cl2) obtained as previously described. The initial concentration of the salt considered in water, whether LiCl, NaCl, KCl, MgCl2, CaCl2, SrCl2, or BaCl2, is 0.1 mol / L. After performing these 7 specific (duplicate) extractions on salts, the amounts of cations extracted in relative molar percentage before and after extraction at room temperature and isovolume water / extractant formulation are indicated in Table I: Table I MEC1 0.1 M Extraction rate at TA (Org. / Water = 1) MSA2 3.52 M LiCl NaCl KCl MgCh CaCl2 SrCl2 BaCl2 Fluidifier CH2Cl2 73.7% 85.8% 75.8% 5.4% 59.4% 64.0% 46.1% The extraction of cations from a brine consisting of a single alkali or alkaline earth chloride therefore varies from 5.4% to 85.8% depending on the cation. In these single-salt solutions, and for this MEC1, the extraction level of the salts is very good except for magnesium, which, with its ionic radius of 76 pm and its strong hydrophilicity, does not fall within the extraction limit of this 16-carbon macrocycle, which is still too large. This formulation, therefore, appears to be well-suited for the large-scale desalination of saline water, even brine (water with a salinity greater than 50 g / liter). Example 2: Extraction of salts from a brine using MECI. The extractant composition is as follows: 0.4 Mol / L of MEC1 (see example 1, CAS No. 114155-16-7), supplemented with 1.2 Mol / L of MSA9 of formula: O where R is the heptyl radical: nC?Hi5. This compound has been synthesized using the method described in Example 9, which appears later. The fluidizer used to solubilize these two compounds is 1,2-dichlorobenzene, CAS number 95-50-1 purchased from TCI-CHEMICALS and identified by the acronym 12CIPh. The brine is a highly saline water, at 180 g / L (or 5.6 mol / L), composed of sodium, potassium, calcium, magnesium, and chloride ions in the proportions shown in Table II below. The saline water to be treated was contacted with a relative volume three times that of this extracting solution in order to approximate the operational conditions. Table II below shows the concentrations in mmol / L of water of each of the ions before and after each of the four extraction stages, carried out at room temperature (TA). Table II MEC1 0.4 M Evolutions of salinity at RT, in mMol / Liter MSA9 1.2 M Na K Mg Ca Cl Total Fluidifier 12CIPh Initial 1650 20.8 77.1 447 3432 5626 Org. / Water 3 Extracl 1162 22.5 83.4 495 2703 4466 Extrac2 429 23.4 86.4 492 2292 3322 Extrac3 8.54 13.9 87.6 360 1083 1553 Extrac4 3.70 3.65 94.2 114 469 685 Equivalent4 g / Liter 0.09 0.14 2.29 4.57 16.62 23.70 These data are illustrated in Figure 1. It is clear that the first salt to be extracted is NaCl, and then, starting with the third extraction stage, calcium and potassium chlorides begin to be extracted, while the NaCl concentration continues to decrease in the water. As expected, magnesium is not extracted. In the end, after four phases of contact and mixing between liquid phases, the total salinity of the water decreases from 180 g / L to 23.7 g / L. A fifth extraction could achieve complete desalination, close to the MgCk level. Example 3: extractions at room temperature of saline solutions in monosalts with the MEC2. Example 3 is performed under the same conditions as Example 1 except that MEC1 is replaced by MEC2. The MEC used is 4-tert-butyl-Calix[6]arene hexakis(N,N-diethylacetamide (MEC2 of n' CAS: 111786-95-9). It was synthesized internally from 4-tert-Butylcalix[6]arene —I— of crude formula CeeHeAOe and CAS No. 78092-53-2, purchased from TCI C Chemicals, according to the synthesis procedure described in the publication L 1 -I® Selective Complexation and Membrane Transport of Guanidinium Salts F R / by Calix[6]arene Amides, Israel J.Chem, 1992, 32, 79-87. / Xc F— / fl·—ςp V—OH The MSA used is MSA2 of CAS No. 32707-89-4; CgHeFeO, MW= 244.13 g / mol, white solid, which can be obtained from various distributors. After performing the 7 specific (duplicate) extractions on salts, the amounts of cations extracted in relative molar percentage before and after extraction at room temperature and water volume / extractant formulation are indicated in Table III: Table III MEC2 0.1 M Extraction rate at TA (Org. / Water = 1) MSA2 3.52 M LiCl NaCl KCl MgCh CaCl2 SrCl2 BaCl2 Fluidifier CH2Cl2 21.9% 22.7% 25.4% 13.5% 57.8% 63.8% 63.2% The extraction of cations from a brine consisting of a single alkali or alkaline earth chloride therefore varies from 13.5% to 63.8% depending on the cation. In these single-salt solutions, divalent cations are extracted in quantities two to three times greater than monovalent cations, with the exception of the much more hydrophilic and smaller magnesium ion, Mg2+, which in this case is difficult to extract, as illustrated in Figure 2. The composition according to the invention thus demonstrates a particularly interesting specificity of this formulation for numerous industrial applications where calcium, although more hydrophilic than sodium (AG'hid = -1515 kJ / mol versus -406 kJ / mol), despite both having a very close ionic radius (102 and 100 pm), is extracted 2.54 times better from water in their respective chloride forms. Example 4: Characterization of an extractant composition that integrates MEC2 for the extraction of CaCl? This series of examples establishes two CaCI2 extraction isotherms at 20°C and 80°C for an extractant composition comprising 0.1 Mol / L of MEC2, combined with 1 Mol / L of MSA 9; all dissolved in 1,2-dichlorobenzene. After performing the 7 specific (duplicate) extractions on salts, the amounts of cations extracted in relative molar percentage before and after extraction at room temperature and isovolume of water / extractant formulation are indicated in Table IV: Rate IV MEC2 0.1 M Extraction rate at RT (Org. / Water = 1) MSA9 1 M 0.01 M 0.02M 0.03M 0.04 M 0.1M 0.2M 0.4M Fluidizer 12CIPh 39% 42% 41% 40% 34% 27% 16% The same extraction series was then performed at 80°C to obtain the following table V: Table V MEC2 0.1 M Extraction rate at 80°C (Org. / water = 1) MSA9 1 M 0.01M 0.02M 0.03M 0.04M 0.1M 0.2M 0.4M Fluidizer 12CIPh 11% 16% 18% 17% 18% 16% 10% There is a strong influence of extraction temperature on extraction efficiency. Based on these studies and the collected data, it was possible to plot these absorption isotherms in Figure 3 for concentrations in mol / L. The abscissa represents the concentration of NaCl in the water, and the ordinate represents the concentration of NaCl in the organic phase at absorption equilibrium. The liquid-liquid salt extraction procedure according to the invention is exothermic in absorption and endothermic in regeneration, allowing thermal regeneration in hot water of the extracting organic composition. Example 5: Extraction procedure that includes thermal regeneration of the extractant composition that integrates MEC2 and impacts associated with the desorption of CaCk Two samples of the extractant composition from Example 4, with a higher CaCl₂ load at 20°C, were contacted with saline water containing 1 mol / L CaCl₂ at room temperature to increase the salt load of the dissolved MEC₂ cation extractant molecules, bringing them closer to their salt saturation level (0.1 mol / L). These two samples were then contacted with an equal volume of distilled water at 20°C and stirred. One of the two two-phase samples was subsequently heated to 80°C and kept under stirring. Having assessed the initial salt load at 80 mmol / L, this appears to decrease to 15.27 mmol / L from the first regeneration stage at 80°C, while in the regeneration at 20°C the residual salt concentration is 29.3 mmol / L. Figure 4 illustrates the results obtained in several stages of serial contact with an isovolume of distilled water of the hydrophobic organic liquid phase loaded with salts.Thermal regeneration of the extractant composition is much more efficient due to a twofold reduction in the number of regeneration steps required to achieve the same overall CaCl2 deextraction rate. In practice, this advantage appears to be even more significant when using a resin with high MEC and, consequently, salt loading rates. Increasing the regeneration temperature reduces the number of successive stages of contacting distilled water at equal volume, while simultaneously allowing for greater salt removal each time. It also enables access to regeneration water with a higher concentration of removed salts due to the use of a smaller volume of regeneration water. Example 6: Comparative examples: Selective extractions at room temperature of cations from a binary mixture of NaCl / CaCh salt A brine containing an equimolar mixture of salts, 0.05 mol / L of NaCl and 0.05 mol / L of CaCl2 each, prepared as previously described, was contacted with two extractant compositions, one of which is according to the invention. These compositions differ from each other only in by the MEC compound used, which remains from the family of disubstituted primary amides but whose macrocycle size is modified, being 16 carbons (MEC1) and 24 carbons (MEC2) respectively. These compositions are obtained according to the procedure described above. Each extractant composition comprises 0.1 mol / L of MEC and hn'^cthis 2.4mol / L of MSA9 in 1,2-dichlorobenzene. 1,2-Dichlorobenzene (CAS No.: 95-50-1), with a purity greater than II.I 99%, comes from the company TCI Chemicals. ' The amounts of cations, in molar percentage, extracted from the mixture are indicated in Table VI: Table VI MEC1 / MEC2 Cations Na+ Ca++ 4-tert-ButylCalix[4]CH2C(=O)NEt2 %E 88.0% 10.0% 4-tert-ButylCalix[6]CH2C(=O)NEt2 %E 4.0% 56.0% Depending on the selected MEC, in a salt mixture, the extraction of these cations exhibits increased selectivity, or the cation most extracted in its pure form becomes predominantly extracted in the salt mixture. Co-absorption in this case is favorable for the extraction that was initially the best. In particular, the formulation incorporating the 24-unit carbon cycle MEC2 has a calcium extraction rate 14 times higher than that of sodium in a mixture at cation concentrations compared to a rate of 2.54 for solutions containing only one of these salts (see examples 1 and 3). Such extraction capabilities have numerous industrial applications in water descaling. Example 7: Selective extractions at room temperature of cations from a binary mixture of NaCl v CaCl2 salts at different initial concentrations. A brine containing a mixture of NaCl and CaCl2 is prepared as previously described to obtain the following initial salt concentrations in mixture: 0.2 Mol / L of NaCl and 0.03 Mol / L of CaCl2. The extractant resin is composed of 0.1 Mol / L of MEC2, 3.52 Mol / L of MSA2, and a supplement of liquid MSA1, also used as a fluidizer. The amounts of cations, in molar percentage, extracted from the mixture are indicated in Table VII: Vile Table MEC2 Cations Na* Ca** 4-tert-ButylCalix[6]CH2C(=O)NEt2 %E 5.0% 88.0% It is observed that the ratio of extraction rates for Ca / Na is 17.6, which validates one of the objects of the invention as a consequence of an improvement in the deviations in the extraction in multi-salts, in the presence of a common anion. Example 8: Selective extractions at room temperature of cations from a mixture of four salts: NaCl, CaCl, SrCk, and BaCh A brine containing a mixture of NaCl, CaCl2, SrCl2, and BaCl2 was prepared as previously described. The concentrations of dissolved salts are given in Table VIII in mmol / L. The extraction was performed a second time with modified concentrations of divalent salts. The concentrations of dissolved salts are given in Table IX in mmol / L. The extractant composition consists of 0.1 Mol / L of MEC2 and a mixture of two MSAs. This mixture is made up of MSA2, commonly called [3,5Bis(Trifluoromethyl)benzyl alcohol] (35TFMBnOH) with CAS No. 32707-89-4 at a level of 60% by volume, and MSA1, called [3-(Trifluoromethyl)benzyl alcohol] (3TFMBnOH), with the crude formula C8H7F3O, MW = 176.14 g / mol, and CAS No. 349-75-7, at a level of 40% by volume, which acts both as a fluidifier and as an MSA due to its liquid form. The extraction is performed as described in example 1 and at room temperature. The amounts of cations extracted in molar percentage are indicated in Tables VIII and IX, respectively for initial and final ionic concentrations expressed in mMoles / L. Table VIII Cations CATIONS (mMol / L) ANIONS Cl- (mMol / L) Initial Concentration Final Concentration % Extraction Initial Concentration Final Concentration Na+ 193.52 199.4775 0% 257.74 213.38 Ca2+ 29.13 0.4916 98% Sr2+ 4.29 0 100% Ba2+ 4.69 0 100% Table IX Cations CATIONS ANIONS Cl- Initial Concentration Final Concentration % Extraction Initial Concentration Final Concentration Na+ 196.04 195.9835 0% 245.4 203.16 Ca2+ 9.25 0 100% Sr2+ 9.17 0 100% Ba2+ 9.32 0 100% Here it is observed that for high relative concentrations of sodium with respect to these 10 divalent scaling cations, an extraction selectivity of 100% can be obtained. The selective extraction of divalent cations demonstrates the ability of the compositions according to the invention to effectively combat scaling and purify water, thanks to a selective extraction of calcium Ca++, strontium and barium. Example 9: Synthesis of compounds MSA9, MSA10, MSAC11 and MSA12 Summary outline EITHER

Claims

1. CLAIMS 1. A process for deionizing water by liquid extraction with thermal regeneration, applied to the extraction of a bivalent non-alkaline cationic species and a complementary anionic species from a saline liquid aqueous solution, said saline liquid aqueous solution comprising: - a salt of said non-alkaline cationic species, and - a salt of a cationic species of an alkali metal, said process comprising the following steps: a) mixing in a first reactor, at a first temperature, a liquid hydrophobic organic phase and said saline liquid aqueous solution, to subsequently obtain a treated liquid aqueous solution and a liquid hydrophobic organic phase loaded with said non-alkaline cationic species and complementary anionic species, said liquid hydrophobic organic phase comprising an extractant molecule of said non-alkaline cationic species,a solvating molecule of said complementary anionic species and, optionally, a fluidifier; b) the separation, on the one hand, of the treated liquid aqueous solution and, on the other hand, of said hydrophobic liquid organic phase loaded with said non-alkaline cationic species and complementary anionic species; and c) the mixing, at a second temperature, in liquid phase, in a second reactor, of said hydrophobic liquid organic phase loaded with said non-alkaline cationic species and complementary anionic species and of a liquid aqueous regeneration solution, for the subsequent obtaining of a regenerated hydrophobic liquid organic phase and a liquid aqueous regeneration solution loaded with said non-alkaline cationic species and complementary anionic species,where the difference between said first and second temperature varies from 30 °C to 150 °C; where said extractant molecule of a non-alkaline cationic species is a macrocycle whose ring is formed by 24 to 32 carbon atoms, functionalized by amide groups, and of the following formula (I) or (II): - p is 1 or 2, - m is 3 or 4, - qyt, identical or different, are 0, 1 or 2, - R is a tert-butyl, tert-pentyl, tert-octyl, O-methyl, O-ethyl, O-propyl, O-isopropyl, O-butyl, O-isobutyl, O-pentyl, O-hexyl, O-heptyl, O-octyl, OChaphenyl group or a hydrogen atom, - R* and R, identical or different, are chosen from the group consisting of methyl, ethyl, propyl, isopropyl, butyl and isobutyl, pentyl, hexyl, heptyl and octyl groups or R' and R together form a pyrrolidine, piperidine or morpholine ring.

2. A process according to claim 1, wherein the extractant molecule of at least one non-alkaline cationic species is selected from the compounds of formula (I) to macrocycle calixarene, with p=1, and R, R', R” and n as defined below: RR' R” n tert-Butyl Pyrrolidinyl 6 I tert-Butyl Ethyl Ethyl 6 O-Octyl Ethyl Ethyl 6 OCh- Phenyl Ethyl Ethyl 6 H Ethyl Ethyl 6 O-methyl Ethyl Ethyl 6 tert-Butyl Ethyl Ethyl 8 O-Octyl Ethyl Ethyl 8 OCh-Phenyl Ethyl Ethyl 8 H Ethyl Ethyl 8 O-methyl Ethyl Ethyl 8 advantageously in their cone-type or partial-cone-type configurations.

3. A process according to any one of claims 1 to 2, wherein said non-alkaline cationic species is at least one of the following cations: calcium, strontium, and barium.

4. A process according to any of claims 1 to 3, wherein the non-alkali cationic species is selectively extracted with respect to the cationic species of an alkali metal.

5. Process according to any of claims 1 to 4, wherein the cationic species of an alkali metal is the sodium ion Na+.

6. A liquid-mediated extraction deionization process with thermal regeneration, applied to the selective extraction of at least one alkali cationic species and a complementary anionic species from a saline liquid aqueous solution, said saline liquid aqueous solution comprising: - a salt of said at least one alkali cationic species, and - a salt of an alkaline earth metal cationic species, said process comprising the following steps: a) mixing in a first reactor, at a first temperature, a liquid hydrophobic organic phase and said saline liquid aqueous solution, to subsequently obtain a treated liquid aqueous solution and a liquid hydrophobic organic phase loaded with said alkali cationic species and complementary anionic species, said liquid hydrophobic organic phase comprising an extractant molecule of said alkali cationic species,a solvating molecule of said complementary anionic species and, optionally, a fluidifier; b) the separation, on the one hand, of the treated liquid aqueous solution and, on the other hand, of said hydrophobic liquid organic phase loaded with said alkaline cationic species and complementary anionic species; and c) the mixing, at a second temperature, in liquid phase, in a second reactor, of said hydrophobic liquid organic phase loaded with said alkaline cationic and complementary anionic species and of a liquid aqueous regeneration solution, for the subsequent obtaining of a regenerated hydrophobic liquid organic phase and a liquid aqueous regeneration solution loaded with said alkaline cationic and complementary anionic species, wherein the difference between said first and second temperatures varies from 30 °C to 150 °C; wherein said extracting molecule of an alkaline cationic species is a macrocycle whose ring is formed by 16 to 24 carbon atoms,functionalized by ester or ketone groups.

7. A process according to claim 6, wherein the extractant molecule of at least one alkaline cationic species is selected from the compounds of formula (V) or (VI): (V) where (VI) - n is 4, 5 or 6, - p is 1 or 2, - m is 2 or 3, - qyt, identical or different, are 0, 1 or 2, - R is a tert-butyl, tert-pentyl, tert-octyl group or a hydrogen atom, - R' is selected from the group consisting of methyl, ethyl, propyl, isopropyl, butyl, isobutyl, pentyl, hexyl, heptyl and octyl groups, for the realization of a ketone-type ligand group or R' is selected from the group consisting of the O-methyl, O-ethyl, O-propyl, O-isopropyl, O-butyl, O-isobutyl, O-pentyl groups, O-hexyl, O-heptyl, O-octyl, OCFk-Phenyl for the realization of an ester-type ligand group.

8. A process according to any of claims 6 to 7, wherein the extractant molecule of at least one alkaline cationic species is selected from the compounds of formula (V) a macrocycle calixarene, with p=1, and R, R' and n as defined below R R' n H O-ethyl 4 H O-isopropyl 4 H O-tert-butyl 4 tert-butyl O-ethyl 4 tert-butyl O-isopropyl 4 tert-butyl O-tert-butyl 4 tert-octyl O-ethyl 4 tert-butyl O-ethyl 5 tert-butyl tert-butyl 4 tert-butyl O-ethyl 6 advantageously in their cone-type or partial-cone-type configurations.

9. A process according to any of claims 6 to 8, wherein the extractant molecule has a complexation constant Log K, in methanol at 25°C, of ​​the alkaline cationic species to be extracted, of a value greater than 3 and less than 11, preferably greater than 5 and less than 9.

10. A process according to any of claims 6 to 9, wherein the at least one alkaline cationic species is selected from lithium, sodium, potassium, rubidium, and cesium.

11. Process according to any of claims 6 to 10, wherein the process consists of a selective extraction of alkali salts to hydrophilic anions, such as chlorides.

12. A process according to any one of claims 1 to 11, wherein the fluidizer is selected from polar aromatic solvents derived, for example, from dichlorobenzenes, dichlorotoluenes, their derivatives and mixtures thereof.

13. A process according to any one of claims 1 to 12, wherein the solvating molecule of said complementary anionic species is a hydrophobic, and preferably protic, compound whose pKa in water at 25°C is at least 9, preferably at least 10.5 and is preferably less than the pKa of water at 25°C, or at least less than 15 at 25°C.

14. Process according to any of claims 1 to 13, wherein the solvating molecule of said complementary anionic species is a molecule of formula: wherein R is R = n-CzHis, n-CgHw, n-CuH23 or n-Ci3H27.

15. Hydrophobic liquid organic composition comprising an extractant molecule of a non-alkali cationic species, a solvating molecule of a complementary anionic species, and a fluidifier, the composition being characterized in that the extractant molecule of a non-alkali cationic species is a macrocycle whose ring is formed by 24 to 32 carbon atoms, functionalized by amide groups, and of the following formula (I) or (II): (II) where - n is an integer from 5 to 8, - p is 1 or 2, - m is 3 or 4, - qyt, identical or different, are 0, 1, or 2, - R is a tert-butyl, tert-pentyl, tert-octyl, O-methyl, O-ethyl, O-propyl, O-isopropyl, O-butyl, O-isobutyl, O-pentyl, O-hexyl, or O-heptyl group, O-octyl, OCHzphenyl or a hydrogen atom, - R' and R”, identical or different, are chosen from the group consisting of methyl, ethyl, propyl, isopropyl, butyl, isobutyl, heptyl and octyl groups or R' and R together form a pyrrolidine, piperidine or morpholine ring.

16. A hydrophobic liquid organic composition comprising an extractant molecule of an alkali cationic species, a solvating molecule of a complementary anionic species, and a fluidifier, the composition being characterized in that the extractant molecule of an alkali cationic species is a macrocycle whose ring is formed by 16 to 24 carbon atoms, functionalized by ester or ketone groups, and in particular of formula (V) or (VI): where - n is 4, 5, or 6, - p is 1 or 2, - m is 2 or 3, - qyt, identical or different, are 0, 1, or 2, - R is a tert-butyl, tert-pentyl, tert-octyl group, or a hydrogen atom, - R' is selected from the group consisting of methyl, ethyl, propyl, isopropyl, butyl, isobutyl, pentyl, hexyl, heptyl, and octyl groups, for the The binding group of the ketone type or R' is chosen from the group consisting of the groups O-methyl, O-ethyl, O-propyl, O-isopropyl, O-butyl, O-isobutyl, O-pentyl, O-hexyl, O-heptyl, O-octyl,OCH2-Phenyl for the realization of an ester-type ligand group.

17. Hydrophobic liquid organic composition according to any of claims 15 to 16, wherein the solvating molecule of said complementary anionic species is a hydrophobic, and preferably protic, compound whose pKa in water at 25°C is at least 9, preferably at least 10.5 and is preferably less than the pKa of water at 25°C, or at least less than 15 at 25°C.

18. Hydrophobic liquid composition according to any of claims 15 to 17, wherein the solvating molecule of a complementary anionic species is a molecule of formula: wherein R is R = n-CrHis, n-CgHw, n-CnH23 or n-Ci3H27.

19. Hydrophobic liquid organic composition according to claim 15 to 18, wherein the fluidizer is selected from polar aromatic solvents derived, for example, from dichlorobenzenes, dichlorotoluenes, their derivatives and mixtures thereof.

20. Use of a composition according to any of claims 15, 17 to 19 for the selective extraction of at least one non-alkaline divalent cationic species and a complementary anionic species from an aqueous saline solution.

21. Use of a composition according to any of claims 16 to 19 for the selective extraction of at least one alkaline cationic species and a complementary anionic species from an aqueous saline solution.