WO2017085311A1 - Procédés d'extraction et de récupération de l'uranium présent dans une solution aqueuse comprenant de l'acide phosphorique - Google Patents
Procédés d'extraction et de récupération de l'uranium présent dans une solution aqueuse comprenant de l'acide phosphorique Download PDFInfo
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- WO2017085311A1 WO2017085311A1 PCT/EP2016/078292 EP2016078292W WO2017085311A1 WO 2017085311 A1 WO2017085311 A1 WO 2017085311A1 EP 2016078292 W EP2016078292 W EP 2016078292W WO 2017085311 A1 WO2017085311 A1 WO 2017085311A1
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B60/00—Obtaining metals of atomic number 87 or higher, i.e. radioactive metals
- C22B60/02—Obtaining thorium, uranium, or other actinides
- C22B60/0204—Obtaining thorium, uranium, or other actinides obtaining uranium
- C22B60/0217—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes
- C22B60/0252—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes treatment or purification of solutions or of liquors or of slurries
- C22B60/0265—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes treatment or purification of solutions or of liquors or of slurries extraction by solid resins
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B60/00—Obtaining metals of atomic number 87 or higher, i.e. radioactive metals
- C22B60/02—Obtaining thorium, uranium, or other actinides
- C22B60/0204—Obtaining thorium, uranium, or other actinides obtaining uranium
- C22B60/0217—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes
- C22B60/0221—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes by leaching
- C22B60/0226—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes by leaching using acidic solutions or liquors
- C22B60/0243—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes by leaching using acidic solutions or liquors phosphorated ion as active agent
Definitions
- the present invention relates to the field of extraction of uranium present in an aqueous medium containing phosphoric acid.
- uranium and more specifically uranium at oxidation state + VI, denoted uranium (VI) or U (VI), this uranium being present in an aqueous solution which further comprises phosphoric acid.
- the invention also relates to a process for recovering uranium (VI) present in such an aqueous solution.
- the aqueous solution from which can be extracted, or from which can be recovered, the uranium (VI) may in particular be an aqueous solution resulting from the attack, with sulfuric acid, a natural phosphate.
- the present invention finds particular application in the treatment of natural phosphates in order to recover the uranium present in these phosphates.
- Natural phosphates also known as phosphate ores, are used for the manufacture of phosphoric acid and fertilizers. They contain uranium at levels that can range from a few tens of ppm to several thousand ppm as well as varying amounts of other metals.
- the recovery potential of the uranium contained in these natural phosphates is a few thousand tons per year, which represents a significant source of uranium supply.
- valorization of uranium (VI) is therefore carried out from these concentrated aqueous phosphoric acid solutions, which will be called “aqueous solutions of phosphoric acid” in the remainder of the present description.
- This first route consists in subjecting the aqueous solution containing phosphoric acid and uranium to a hydro-metallurgical treatment based on the liquid-liquid extraction technique, which technique consists in bringing this aqueous solution, or aqueous phase, into contact with each other. with an organic phase comprising one or more extractants, to obtain an extraction, in the organic phase, of the uranium contained in the aqueous solution of phosphoric acid.
- these liquid-liquid extraction processes require a post-treatment of the extraction raffinate, which corresponds to the aqueous phase from which the uranium has been extracted, in order to eliminate the residual traces of solvents.
- organic substances either because of a phenomenon of entrainment of these organic solvents or because of their partial solubility in the aqueous phase.
- This post-treatment step allows the referral of this extraction raffinate to the industrial circuits.
- a second uranium extraction route has been proposed.
- This second route implements a solid-liquid extraction, which consists in extracting the uranium from an aqueous solution of phosphoric acid by bringing this aqueous solution into contact with a material insoluble in water and comprising groups Functional chemicals capable of retaining uranium, either by ion exchange or by chelation.
- the document [3] thus proposes an organic material, marketed under the name Duolite TM ES-467, having functional groups corresponding to the formula -CH2NH-CH2-PO3 "2 attached to a macroporous polystyrene matrix.
- the document [4] proposes to extract the uranium from an aqueous solution comprising between 5 mol / L and 8 mol / L of phosphoric acid, by means of a polymeric solid support, also called "resin".
- This polymeric solid support is composed of polyacrylates or styrene / vinylbenzene copolymers and impregnated with an organophosphorus extractant.
- resins sold under the name Amberlite TM (XAD-4, XAD-7, XAD-8 or XE-299) have been used as a polymeric solid support.
- Document WO 2014/018422 also provides a process for extracting uranium contained in an aqueous phosphoric acid solution employing one or two cycles for bringing said aqueous solution into contact with a resin ion exchange and operating continuously.
- the resins described in this document [5] are Lewatit TM commercial resins TP260, Amberlite TM IRC-747 or Purolite TM S-930.
- the object of the invention is therefore to propose a process for extracting uranium (VI) from an aqueous solution of phosphoric acid which is particularly effective, irrespective of the concentration of phosphoric acid in this solution. aqueous.
- this process must be able to be used to extract the uranium (VI) from aqueous solutions of phosphoric acid called "concentrated", such as aqueous solutions that result from the attack of a phosphate rock by water.
- sulfuric acid whose phosphoric acid concentration is typically at least 5 mol / L.
- the process according to the invention must also make it possible for this extraction of uranium (VI) to be very selective with respect to other metal cations likely to be present in the aqueous solution of phosphoric acid and, in particular, to to iron (lll).
- the process for extracting uranium (VI) according to the invention must, in a general manner, overcome the drawbacks of the prior art and in particular be free of the drawbacks noted above, both for the liquid extraction of liquid only for solid-liquid extraction.
- the process according to the invention must be able to be implemented under conditions of optimized industrial safety and environmental safety, by avoiding the use of organic solvents as described in documents [1] and [2]. ] and, in particular, the implementation of a post-treatment stage of the residual traces of organic solvents present in the aqueous solution of phosphoric acid from which the uranium has been extracted, as is the case with the methods of liquid-liquid extraction of these documents [1] and [2].
- This method must therefore, and moreover, involve a reduced number of steps compared with the methods of the prior art.
- the process according to the invention also does not have to resort to a step of reducing the uranium (VI) to uranium (IV) prior to the extraction itself, but must allow a direct extraction of this uranium present in the degree of oxidation + VI in aqueous solutions of phosphoric acid such as those resulting from the sulfuric attack of natural phosphates.
- the organic material comprises a polymeric solid support impregnated with a compound corresponding to the following general formula (I):
- n an integer equal to 0, 1 or 2;
- R 1 and R 2 which are identical or different, represent a linear or branched, saturated or unsaturated hydrocarbon-based group comprising from 6 to 12 carbon atoms;
- R 3 represents:
- a hydrocarbon group saturated or unsaturated, linear or branched, comprising from 1 to 12 carbon atoms and optionally one or more heteroatoms;
- R 2 and R 3 together form a group - (CH 2) n - in which n is an integer from 1 to 4;
- R 4 represents:
- a hydrocarbon group saturated or unsaturated, linear or branched, comprising from 2 to 8 carbon atoms
- a hydrocarbon group saturated or unsaturated, comprising one or more rings, the ring or rings possibly comprising one or more heteroatoms;
- an aromatic group comprising one or more rings, the ring or rings possibly comprising one or more heteroatoms;
- R 5 represents a hydrogen atom or a hydrocarbon group, saturated or unsaturated, linear or branched, comprising 1 to 12 carbon atoms.
- the method according to the invention therefore consists of a solid-liquid extraction and, consequently, does not have the drawbacks associated with the use of organic solvents as in the case of a liquid-liquid extraction.
- an organic material comprising a polymeric solid support impregnated with a compound corresponding to the general formula (I) as defined above makes it possible to extract the uranium (VI) of a phosphoric acid aqueous solution in a high performance and selective manner, whatever the phosphoric acid concentration of this aqueous solution. More particularly, this extraction is carried out by complexing this uranium (VI) with the compound corresponding to the general formula (I), this compound being itself adsorbed on the polymeric solid support of the organic material.
- This document [6] proposes, in fact, the implementation of an organic-inorganic hybrid material for extracting uranium from aqueous solutions of phosphoric acid.
- This organic-inorganic hybrid material comprises a solid support of inorganic nature on which are covalently attached molecules of organic nature which comprise an amido-phosphonate unit capable of complexing uranium (VI) and retain it by this complexing mechanism.
- This solid support of inorganic nature is presented, by the document [6], as being chemically more stable than are the organic supports of the organic materials such as those proposed by the document [3].
- the extractions conducted with the particular organic material used in the context of the extraction process according to the invention are quite effective.
- the performance of the extraction process according to the invention is greater than that of the extraction method of the document [6].
- the process according to the invention makes it possible to carry out a direct extraction of the uranium present in the acidic aqueous solution at its oxidation state + VI.
- the process according to the invention does not include a step of reducing the uranium (VI) uranium (IV) prior to the extraction step itself, unlike the methods described in documents [3] and [4].
- the organic material used in the process according to the invention comprises a polymeric solid support impregnated with a compound corresponding to the general formula (I) specified above.
- the reader is therefore invited to refer to this document [2] for any information relating to this compound, to its synthesis process and, in particular, to the definition given therein terms such as "hydrocarbon group, saturated or unsaturated , linear or branched, comprising from x to y carbon atoms "," heteroatom ",” hydrocarbon group, saturated or unsaturated, cyclic, comprising from x to y carbon atoms "or” aromatic group ".
- the compound of the organic material corresponds to the following particular formula (I-a):
- R 1 and R 2 represent an alkyl group comprising from 8 to 10 carbon atoms
- R 3 and R 5 represents a hydrogen atom and the other one of R 3 and R 5 represents an alkyl group comprising from 4 to 10 carbon atoms, and
- R 4 represents an alkyl group comprising from 4 to 6 carbon atoms.
- the compound of the organic material is chosen from:
- DEHCEPE ethyl 1 - (/ V, / V-diethylhexylcarbamoyl) ethylphosphonate, denoted DEHCEPE, which corresponds to the formula (la) above in which R 1 and R 2 both represent a 2-ethylhexyl group, R 4 represents an ethyl group, one of R 3 and R 5 represents a hydrogen atom while the other of R 3 and R 5 represents a methyl group,
- DEHCNPE ethyl 1 - (/ V, / V-diethylhexylcarbamoyl) nonylphosphonate, denoted DEHCNPE, which corresponds to the particular formula (la) above in which R 1 and R 2 both represent a 2-ethylhexyl group, R 4 represents an ethyl group, one of R 3 and R 5 represents a hydrogen atom while the other of R 3 and R 5 represents an n-octyl group,
- DEHCNPB butyl 1 - (/ V, / V-diethylhexylcarbamoyl) nonylphosphonate, denoted DEHCNPB, which corresponds to the particular formula (Ia) above in wherein R 1 and R 2 are both 2-ethylhexyl, R 4 is n-butyl, one of R 3 and R 5 is hydrogen while the other is R 3 and R 5 represents an n-octyl group,
- DEHCNPI P isopropyl 1 - (/ V, / V-diethylhexylcarbamoyl) nonylphosphonate, denoted DEHCNPI P, which corresponds to the particular formula (la) above in which R 1 and R 2 both represent a 2-ethylhexyl group, R 4 represents an isopropyl group, one of R 3 and R 5 represents a hydrogen atom while the other of R 3 and R 5 represents an n-octyl group.
- the compound impregnated in the organic material is butyl 1- (N, N-diethylhexylcarbamoyl) nonylphosphonate, denoted DEHCNPB.
- the polymeric solid support of the organic material is more preferably formed of a polymer which does not comprise, or practically none, of functional groups capable of reacting with the metal cations present in the aqueous solution S.
- This polymeric solid support may be formed of a polymer comprising at least one unit selected from an olefinic unit, a benzene unit, an acrylic ester unit, and mixtures of these units.
- this polymer may be a divinylbenzene / styrene copolymer or an acrylic ester polymer.
- the polymeric solid support has a specific surface area of between 300 m 2 / g and 1000 m 2 / g (determined by the BET method).
- the polymeric solid support has a pore diameter of between 50 ⁇ and 950 ⁇ .
- the polymeric solid support is in the form of beads, or beads, whose average size as presented by at least 90% of the balls in number, denoted dgo, is advantageously between 200 ⁇ and 900 ⁇ . .
- Polymeric solid supports that are suitable for the organic material are in particular available from Dow Chemical Company under the trade names Amberlite TM XAD-4, Amberlite TM XAD-7, Amberlite TM XAD-16 or Amberlite TM XAD-1180.
- Amberlite TM XAD-7 corresponding to a polymeric solid support based on an acrylic ester polymer, the other commercial references being, in turn, polymeric solid supports based on divinylbenzene / styrene copolymers.
- Other polymeric solid supports based on divinylbenzene / styrene copolymers are also available from Purolite under the trade names Hypersol-Macronet TM MN202 and Hypersol-Macronet TM MN500.
- the organic material is formed of the polymeric solid support in which the compound corresponding to the general formula (I) is impregnated, this impregnation being characterized by an adsorption of this compound on this polymeric solid support.
- the impregnation of this compound in the polymeric solid support is conventionally carried out wet, that is to say by dissolving the compound in a suitable volatile organic solvent and then bringing the solution thus obtained into contact with the polymeric solid support for that this one impregnates the compound. After impregnation of the compound in the polymeric solid support, the excess of organic solvent is evaporated, preferably under vacuum, whereby the organic material obtained is in a dry form.
- This impregnation of the compound in the wet polymeric solid support makes it possible to prepare an organic material in which the limit of exudation of the compound is not reached.
- the organic material comprises a mass percentage of at least 2.5% by weight of this compound, which is impregnated in the polymeric solid support, with respect to the total mass of the organic material.
- the organic material comprises a mass percentage ranging from 10% to 70% by m, and preferably from 20% to 60% by weight.
- the process for extracting uranium (VI) from an aqueous solution S comprising phosphoric acid comprises:
- the uranium (VI) is extracted by the organic material. This extraction is more particularly carried out by complexation of uranium (VI) with the compound of general formula (I). During this contacting step, the concentration of uranium (VI) in the aqueous solution decreases accordingly.
- the process according to the invention makes it possible to extract, with a high extraction yield, the uranium (VI) initially contained in the aqueous solution S, with an organic material which has a higher uranium (VI) carrying capacity than that described in [6].
- This contacting of this aqueous solution S with the organic material may be carried out by simple mixing, for example by means of a stirring system, for a time sufficient to allow the uranium (VI) to be extracted by the organic material.
- this contacting of the aqueous solution S with the solid organic material comprises at least one circulation of a mobile phase constituted by the aqueous solution S on a stationary phase constituted by the organic material.
- This stationary phase constituted by the organic material can be mobile and be in the form of a fluidized bed.
- This stationary phase constituted by the organic material may also be static and be arranged in a column.
- the mobile phase constituted by the aqueous solution S can be injected into the column containing the organic material. After circulation of this mobile phase on the stationary phase, a mobile phase depleted in uranium (VI) is collected at the column outlet.
- a mobile phase depleted in uranium (VI) is collected at the column outlet.
- This mobile phase depleted in uranium (VI) collected at the outlet of the column can be injected again in the same column for a second extraction, in order to recover the uranium (VI) which would not have been extracted during the first injection.
- the concentration of uranium (VI) in the liquid phase decreases as a function of these successive circulations of the mobile phase on the stationary phase.
- the separation is carried out concomitantly with this contacting step.
- the uranium extraction process (VI) according to the invention is appropriate particularly simple.
- the uranium (VI) extraction process of the aqueous solution S having been carried out, it is then possible to extract the uranium (VI) from the organic material to recover this uranium (VI) for recovery.
- the invention also relates to a process for recovering uranium (VI) from an aqueous solution S comprising phosphoric acid.
- this recovery method comprises:
- step (b) a removal of uranium (VI) from the organic material obtained in step (a) by bringing the organic material obtained at the end of step (a) into contact with a basic aqueous solution, and then a separation of the organic material and the basic aqueous solution, whereby the uranium (VI) is recovered in the basic aqueous solution.
- this process for recovering uranium (VI) comprises the following steps: bringing the aqueous solution S into contact with an organic material comprising a polymeric solid support impregnated with a compound corresponding to the following general formula (I):
- n an integer equal to 0, 1 or 2;
- R 1 and R 2 which may be identical or different, represent a hydrocarbon group, saturated or unsaturated, linear or branched, comprising from 6 to 12 carbon atoms;
- R 3 represents:
- a hydrocarbon group saturated or unsaturated, linear or branched, comprising from 1 to 12 carbon atoms and optionally one or more heteroatoms;
- a hydrocarbon group saturated or unsaturated, comprising one or more rings of 3 to 8 carbon atoms, the ring or rings possibly comprising one or more heteroatoms;
- an aryl group comprising one or more rings, the ring or rings possibly comprising one or more heteroatoms;
- R 2 and R 3 together form a group - (CH 2) n - in which n is an integer from 1 to 4;
- R 4 represents:
- a hydrocarbon group saturated or unsaturated, linear or branched, comprising from 2 to 8 carbon atoms
- a hydrocarbon group saturated or unsaturated, comprising one or more rings, the cycle or cycles being optionally include one or more heteroatoms;
- an aromatic group comprising one or more rings, the ring or rings possibly comprising one or more heteroatoms;
- R 5 represents a hydrogen atom or a hydrocarbon group, saturated or unsaturated, linear or branched, comprising from 1 to 12 carbon atoms,
- step (b) contacting the organic material obtained at the end of step (a) with a basic aqueous solution and then separating the organic material and the basic aqueous solution.
- step (b) of the recovery process according to the invention is particularly efficient and allows to recover quantitatively the uranium (VI) previously extracted by the organic material.
- the process according to the invention makes it possible to recover uranium (VI) with a yield of at least 95%, or even greater than 95%.
- the process according to the invention also makes it possible to recover, in a particularly selective manner, uranium (VI), in particular with respect to iron (III) if it is initially present in the aqueous solution S. Indeed, during step (b), only the uranium (VI) is desextracted. In fact, in contact with the basic solution, the iron (III) precipitates, in the form of Fe (OH) 3 iron hydroxide, on the organic material and is therefore notexextracted. It should be noted, however, that the presence of this precipitate of iron hydroxide (III) on the organic material does not affect the circulation of the various feed solutions within the column of organic material, the amount of iron (III) extracted during the step (a) remaining really minimal.
- step (a) is carried out by the extraction method as defined above, it being specified that the advantageous characteristics of this extraction method, such as those relating to the compound according to the general formula (I) and / or the polymeric solid support, can be taken alone or in combination.
- step (b) of the recovery process according to the invention the uranium (VI) extracted by the organic material is desextracted by contacting this organic material with a basic aqueous phase.
- the uranium (VI), desextracted from the organic material, is recovered in the basic aqueous solution.
- the contacting of the organic material with the basic aqueous solution may be carried out by simple mixing, for example by means of a system with stirring, for a time sufficient to allow the uranium (VI) to beexextracted in the phase basic aqueous
- this bringing into contact of the organic material obtained at the end of step (a) with the basic aqueous solution comprises at least one elution with a mobile phase constituted by the solution aqueous solution of a stationary phase constituted by the organic material.
- this stationary phase constituted by the organic material can be mobile and be in the form of a fluidized bed. It can also be static and be arranged in a column.
- This advantageous variant of contacting the organic material with the basic aqueous solution may, in particular, be carried out in a column.
- the separation of the organic material and the basic aqueous solution in which the uranium (VI) is located can be carried out by any usual separation technique for the separation of a solid and a liquid, such as filtration, centrifugation ...
- the contacting step consists of an elution, in a column, by the liquid phase of the stationary phase, the separation is carried out concomitantly with this contacting step.
- the recovery process of uranium (VI) according to the invention is also particularly simple implementation.
- the basic aqueous solution has a pH greater than or equal to 8.
- the pH of the basic aqueous solution is advantageously between 8.5 and 12 and preferably between 9 and 11.
- the basic aqueous solution is an aqueous solution of an alkali metal salt or an ammonium salt.
- the salt of the alkali metal or ammonium is preferably a carbonate.
- the alkali metal may be advantageously selected from sodium and potassium.
- Such a salt may especially be chosen from sodium carbonate and ammonium carbonate.
- the recovery method according to the invention can comprise, between steps (a) and (b):
- the recovery method according to the invention may furthermore comprise a regeneration of the organic material, so as to be able to envisage at least one subsequent extraction and, where appropriate, at least one subsequent recovery of uranium (VI) contained in a aqueous solution S.
- a regeneration of the organic material so as to be able to envisage at least one subsequent extraction and, where appropriate, at least one subsequent recovery of uranium (VI) contained in a aqueous solution S.
- the recovery method accompanied by such a regeneration of the organic material comprises, after step (b), (c) bringing the organic material obtained at the end of step (b) into contact with an acidic aqueous solution and then separating the organic material and the acidic aqueous solution, whereby the organic material is regenerated.
- the recovery method according to the invention can comprise between steps (b) and (c):
- step (b ') a washing with water of the organic material separated in step (b).
- step (c) bringing the organic material into contact with an acidic aqueous solution makes it possible to regenerate the organic material by protonation.
- the method according to the invention thus makes it possible to selectively and sequentially recover the uranium (VI), by the implementation of the steps (a) and (b), then the iron (III) by the implementation of the step (vs).
- This contacting of the organic material with the acidic aqueous solution may be carried out by simple mixing, for example by means of a stirred system, for a time sufficient to allow the regeneration of the organic material and, where appropriate, the dissolution of the organic material.
- iron hydroxide iron hydroxide
- this bringing into contact of the organic material separated in step (b) and, where appropriate, washed in step (b '), with the acidic aqueous solution comprises at least one wash with a mobile phase constituted by the acidic aqueous solution on a stationary phase constituted by the organic material.
- This advantageous variant of contacting the organic material with this acidic aqueous solution may, in particular, be carried out in a column.
- the separation of the organic material and the acidic aqueous solution in which the iron (III) is located can be carried out by any usual separation technique for the separation of a solid and a liquid, such as filtration, centrifugation, ...
- the separation is carried out concomitantly with this contacting step.
- the uranium recovery process (VI) with regeneration of the organic material according to the invention is therefore also particularly effective. simple.
- the acidic aqueous solution has an H + ion concentration of less than or equal to 20 mol / L.
- This concentration of H + ions of the acidic aqueous solution is advantageously between 0.1 mol / L and 10 mol / L and preferably between 1 mol / L and 7 mol / L.
- the acidic aqueous solution is an aqueous solution comprising at least one inorganic acid.
- Such an inorganic acid may be selected from the group consisting of sulfuric acid, nitric acid, phosphoric acid and hydrochloric acid.
- this inorganic acid is sulfuric acid.
- the aqueous solution S whose uranium (VI) can be extracted according to the extraction process according to the invention or which is used in step (a) of the recovery process according to the invention can comprise phosphoric acid. in a very wide range of molar concentrations, such a molar concentration being, for example, at least 0.1 mol / L of phosphoric acid.
- the aqueous solution S may comprise from 1 mol / l to 10 mol / l, preferably from 2 mol / l to 9 mol / l and, more preferably still, from 3 mol / l to 7 mol / l d 'Phosphoric acid.
- the process according to the invention makes it possible to extract, with a high extraction yield, the uranium (VI) initially contained in the aqueous solution S comprising 5 mol / l of water. phosphoric acid and without degradation of the organic material or its polymeric solid support, contrary to what is taught in document [6].
- the aqueous solution S can in particular be a solution resulting from the attack of a natural phosphate with sulfuric acid.
- the aqueous solution S has a redox potential, or redox potential, of between 450 mV and 550 mV relative to a reference electrode. Ag / AgCl. Indeed, at such redox potential values, the uranium and iron contained in the aqueous solution S are in the form of uranium (VI) and iron (II).
- FIG. 1 illustrates the curves representing, on the one hand, the evolution of the concentration of uranium (VI) found in the fractions of aqueous solution collected, noted [Ujss and expressed in mg / L, as a function of the number of bed volumes of resin (denoted by BV) and, on the other hand, the evolution of the uranium (VI) load capacity of the impregnated resin, denoted Cu (ss) and expressed in g of uranium (VI) / L, based on the number of resin bed volumes (denoted BV), after injection of an aqueous synthetic solution of phosphoric acid S5 in a column comprising an impregnated resin according to the invention.
- V uranium
- FIG. 2 reproduces the curves of FIG. 1 and illustrates the curves representing, on the one hand, the evolution of the concentration of uranium (VI) found in the fractions of aqueous solution collected, denoted [U] s6 and expressed in mg / L, as a function of the number of resin bed volumes (denoted by BV) and, on the other hand, the evolution of the uranium (VI) load capacity of the impregnated resin, denoted Cu ⁇ s6) and expressed in g of uranium (VI) / L, as a function of the number of resin bed volumes (denoted BV), after injection of an aqueous synthetic solution of phosphoric acid S6, in a column comprising an impregnated resin conforming to to the invention.
- VI uranium
- Figure 3 illustrates the curves representing the evolution of the load capacities in uranium (VI), respectively noted CU (R Î ), CU (RI) and CU ⁇ 2) and expressed in g of uranium (VI) / L, according to the number of resin bed volumes (denoted BV), after injection of the aqueous synthetic phosphoric acid solution S7, in three separate columns comprising respectively an impregnated resin according to the invention Ri, a resin RI and a R2 resin.
- FIG. 4 illustrates the curves representing the evolution of the concentrations of uranium (VI) found in the fractions of aqueous solution collected, respectively denoted [U] m, [U] RI and [U] R 2 and expressed in mg / L, as a function of the number of resin bed volumes (denoted by BV), after injection of the aqueous industrial phosphoric acid solution S1, into three distinct columns respectively comprising an impregnated resin according to the invention Ri, a resin R1 and a resin R2.
- VI uranium
- Figure 5 illustrates the curves representing the evolution of the uranium (VI) load capacities, respectively noted CU (R Î ), CU ⁇ RI) and CU (R 2 ) and expressed in g of uranium (VI) / L , according to the number of resin bed volumes (denoted BV), after injection of the aqueous industrial solution of phosphoric acid SI, in three columns each comprising an impregnated resin according to the invention Ri, a resin RI and a resin R2.
- the polymeric solid support hereinafter referred to as "resin"
- resin is the Amberlite TM XAD-7 proprietary resin marketed by Dow Chemical Company.
- This resin which consists of an acrylic ester polymer, is in the form of beads having a particle size of between 250 ⁇ and 840 ⁇ , a specific surface area of 450 m 2 / g (BET method) and a pore diameter. 300 ⁇ , and
- the compound is butyl 1 - (/ V, / V-diethylhexylcarbamoyl) nonylphosphonate, denoted DEHCNPB.
- DEHCNPB butyl 1 - (/ V, / V-diethylhexylcarbamoyl) nonylphosphonate
- the DEHCN PB was first dissolved in a volatile solvent. The resulting mixture was then contacted with Amberlite TM XAD-7 resin to allow impregnation of the latter with DEHCNPB.
- organic material is in the form of impregnated resin dry beads, the mass proportion of DEHCN PB in the impregnated resin, or organic material, being 50% m.
- organic material and “impregnated resin”, which have the same meaning, are used.
- aqueous phosphoric acid solution consisting of an aqueous synthetic phosphoric acid solution comprising 1 mol / l of phosphoric acid and concentrations variables in uranium (VI) and, where appropriate, iron (III); this aqueous synthetic solution of phosphoric acid has a redox potential of 550 mV (relative to the reference electrode Ag / AgCl),
- the uranium (VI) concentrations which are determined by Inductively Coupled Plasma Atomic Emission Spectrometry (ICP-AES), were measured: in the aqueous synthetic solution of initial phosphoric acid, before it is brought into contact with the organic material formed by the impregnated resin dry beads, and in the liquid phase after contact with the resin, or filtrate.
- ICP-AES Inductively Coupled Plasma Atomic Emission Spectrometry
- the difference between the uranium (VI) concentration of the initial synthetic solution and that of the filtrate corresponds to the quantity of uranium (VI) extracted by the organic material.
- the uranium (VI) load capacity of this impregnated resin corresponds to the quantity of uranium (VI) extracted by this impregnated resin.
- This carrying capacity denoted Cu and expressed in mg of uranium / g of impregnated resin (denoted ing U / g), is determined by the following formula:
- Cini concentration of uranium (VI) in the aqueous synthetic solution of initial phosphoric acid (in mg / L)
- the distribution coefficient for uranium, denoted Kd, is determined by the following formula:
- Table 1 below describes the results obtained with four initial aqueous solutions of phosphoric acid, denoted SI to S4, whose initial concentrations of uranium (VI) and, where appropriate, iron (III) were varied. .
- SI to S4 initial aqueous solutions of phosphoric acid, denoted SI to S4, whose initial concentrations of uranium (VI) and, where appropriate, iron (III) were varied. .
- C ini in Fe (III) C ini in U (VI) Cf in in U (VI)
- Cu initial concentrations of uranium
- Example 1 The capacity of the organic material of Example 1 to extract and then recover uranium (VI) contained in an aqueous solution of phosphoric acid was also determined by column tests conducted according to the protocol described below.
- the load capacity denoted Cu and expressed in g of uranium / L of impregnated resin (denoted g U / L), is calculated via the formula given below:
- Cini concentration of uranium (VI) in the aqueous synthetic solution of initial phosphoric acid (in g / L)
- Cfin concentration of uranium (VI) in samplings recovered at the exit of the sampler (in g / L)
- Vresin impregnated resin packed bed volume (in L)
- the impregnated resin as obtained in Example 1 was hydrated with demineralised water so as to allow 15 ml of a packed volume of said impregnated resin to be taken. These 15 ml of impregnated and hydrated resin are placed in a column 2 cm in diameter, the height of the impregnated resin bed reached being close to 40 mm (the ratio between the height of the bed and the diameter of the column is from order of 2). 2.2.1 Evaluation of the extraction capacity of the U (VI) contained in an S5 solution
- An aqueous synthetic solution of initial phosphoric acid, denoted S5, with a redox potential of 550 mV (relative to the reference electrode Ag / AgCl), and comprising 1 mol / L of phosphoric acid and a concentration of 160 mg / Uranium (VI) is prepared and then injected at 10 BV / h (BV means "bed volume” or impregnated resin bed volume) in the column comprising the impregnated resin.
- a sampler is placed at the outlet of the column in order to recover samples of the aqueous solution, after contact of the solution S5 with the impregnated resin.
- This aqueous solution is depleted in U (VI), since the latter was extracted by the resin.
- the quantity of uranium (VI) present in each of the aqueous solution fractions collected at the column outlet is determined by ICP-AES and thus corresponds to the quantity of uranium (VI) which has not been extracted by the impregnated resin .
- the uranium (VI) breakthrough curve which shows the evolution of the uranium (VI) concentration in the fractions of aqueous solution collected at the outlet of the column, denoted [U] ss and expressed in mg / L , depending on the number of BV, and
- the leakage of uranium (VI) is negligible.
- the concentration of U (VI) in each of the fractions removed is less than 10% of the initial concentration of uranium (VI) present in the solution S5.
- the uranium (VI) leak increases to approach the initial concentration of uranium (VI) present in the S5 solution.
- the impregnated resin is then saturated with uranium (VI) and is thus no longer capable of extracting uranium (VI).
- the impregnated resin has a uranium (VI) furnace capacity of 19.2 g uranium / L, meaning that 288 mg of uranium (VI) has been extracted by this impregnated resin.
- a uranium (VI) furnace capacity of 19.2 g uranium / L, meaning that 288 mg of uranium (VI) has been extracted by this impregnated resin.
- the impregnated resin is then eluted with an aqueous solution of sodium carbonate at 1.5 mol / L, injected at 1 BV / h.
- Fractions of the eluate are collected at the column outlet to determine their volume and the amount of uranium U (VI) they comprise. These fractions are collected at regular intervals (every 2 h) and their characteristics are collated in Table 2 below. This table 2 also indicates the number of BV aqueous solution of sodium carbonate used over these time intervals, for the recovery of U (VI).
- Table 2 As can be seen from Table 2 above, the elution of uranium (VI) by the aqueous solution of sodium carbonate is quantitative: more than 95% of uranium (VI) initially extracted by the impregnated resin were eluted in 6 BV.
- a sampler is placed at the outlet of the column in order to determine, by ICP-AES analysis, the quantity of uranium (VI) present in each of the aqueous solution fractions collected at the column outlet and, by difference, the amount of uranium (VI) extracted.
- the amount of iron (III) extracted by the impregnated resin has not been determined directly via the aqueous solution fractions collected at the exit of the sampler; the amount of iron extracted by the resin in each of the fractions remains too small compared to the 2.9 g Fe / L present initially in the solution S6; the iron delta extracted in each of the fractions can not be measured.
- This mineralization consists of dissolving the resin to determine the quantities of uranium (VI) and iron (III). To do this, the resin is first calcined and then dissolved in nitric acid.
- This mineralization made it possible to determine that the amount of Fe (III) present on the impregnated resin amounts to 21 mg, a value which corresponds to an iron load capacity (III) of the impregnated resin, denoted CFe, of 1, 4 g Fe (III) / L.
- the resin column was washed with water at 4 BV / h and then elution of the uranium (VI) present on the resin impregnated with an aqueous solution of sodium carbonate at 1.5 mol / L, injected at 1 BV / h.
- uranium (VI) is quantitatively recovered in the eluate but not in the iron (III).
- iron (III) precipitates on the resin in the form of Fe (OH) 3 iron hydroxide.
- the iron (III) is substantially not extracted by the impregnated resin. The amount of the iron hydroxide precipitate (III) on the resin is therefore small and does not interfere with the flow of aqueous solutions of sodium carbonate or sulfuric acid into the resin column.
- This elution makes it possible to de-poison the resin impregnated with iron present in the form of Fe (OH) 3 and to regenerate the extractant DEHCNPB from the impregnated resin.
- the phosphonic acid function of the extractant which was deprotonated during the elution step with the aqueous solution of sodium carbonate, is here reprotonated during elution with the aqueous solution of sulfuric acid.
- the impregnated resin is then ready for a new cycle of extraction / desextraction.
- Fractions of aqueous solution were collected at the column outlet, at regular intervals (every 2 hours), during this elution with the aqueous sulfuric acid solution, and were analyzed.
- RI formed by a copolymer of styrene / divinylbenzene and phosphonic groups in the sodium form, sold under the name Lewatit ® TP 260, and - 15 ml of resin, denoted R2, formed by a crosslinked polystyrene and acid groups di- (2-ethylhexyl) phosphoric (D2EH PA), sold under the name Lewatit ® VP OC 1026.
- D2EH PA di- (2-ethylhexyl) phosphoric
- the U (VI) loading capacity was determined by measuring the uranium concentrations in all the fractions collected at the column outlet. After extraction and then extraction of the uranium (VI), a mineralization of these resins was conducted for each of them so as to determine the amounts of iron (III) extracted by each of these resins R 1, R 1 and R 2.
- the impregnated resin Ri used in the process according to the invention makes it possible to reach values of uranium (VI) charge capacities, and therefore of extraction, which are clearly greater than those obtained with commercial resins R1 and R2 commonly used to extract uranium (VI) from aqueous solutions of phosphoric acid.
- the impregnated resin R 1 also makes it possible to extract this uranium (VI) with a selectivity with respect to iron (II) which is incontestably greater than that conferred by these resins R 1 and R 2.
- This industrial solution denoted S1
- S1 initially comprises 5 mol / L of phosphoric acid, 130 mg / l of uranium (VI) and 2.8 g / l of iron (11 l) and has a redox potential of 490 mV ( relative to the reference electrode Ag / AgCl).
- the industrial solution SI is injected into each of the columns at a flow rate of 10 BV / h and for 26 h.
- This Figure 4 shows that the leakage of uranium (VI) is limited during the first 20 BV with the implementation of the impregnated resin Ri.
- the U (VI) loading capacity was determined by measuring the concentrations of uranium (VI) in all the fractions collected at the column outlet. After extraction and then extraction of the uranium (VI), a mineralization of the organic materials was carried out on each of the three columns so as to determine the quantities of iron (III) which were extracted by each of the resins R 1, R 1 and R 2.
- Table 5 confirms the decrease in the load capacity of uranium (VI) but also iron (III) with the increase in the molar concentration of phosphoric acid in the aqueous solution from which uranium is to be extracted.
- the impregnated resin used in the extraction and recovery processes according to the invention constitutes by far the better compromise to extract uranium (VI) and this, in a particularly selective way vis-à-vis iron (III).
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- Environmental & Geological Engineering (AREA)
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- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
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Abstract
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Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
MA42557A MA42557B1 (fr) | 2015-11-19 | 2016-11-21 | Procédés d'extraction et de récupération de l'uranium présent dans une solution aqueuse comprenant de l'acide phosphorique |
US15/776,993 US20180355457A1 (en) | 2015-11-19 | 2016-11-21 | Methods for extracting and retrieving the uranium present in an aqueous solution including phosphoric acid |
TNP/2018/000168A TN2018000168A1 (fr) | 2015-11-19 | 2016-11-21 | Procédés d'extraction et de récupération de l'uranium présent dans une solution aqueuse comprenant de l'acide phosphorique |
AU2016356075A AU2016356075A1 (en) | 2015-11-19 | 2016-11-21 | Methods for extracting and retrieving the uranium present in an aqueous solution including phosphoric acid |
CN201680066596.2A CN108350527A (zh) | 2015-11-19 | 2016-11-21 | 从含磷酸的水性溶液中提取和回收铀的方法 |
IL259307A IL259307A (en) | 2015-11-19 | 2018-05-13 | Methods for extracting and retrieving the uranium present in an aqueous solution including phosphoric acid |
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FR1561141A FR3044018B1 (fr) | 2015-11-19 | 2015-11-19 | Procedes d'extraction et de recuperation de l'uranium present dans une solution aqueuse comprenant de l'acide phosphorique |
FR1561141 | 2015-11-19 |
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WO2017085311A1 true WO2017085311A1 (fr) | 2017-05-26 |
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PCT/EP2016/078292 WO2017085311A1 (fr) | 2015-11-19 | 2016-11-21 | Procédés d'extraction et de récupération de l'uranium présent dans une solution aqueuse comprenant de l'acide phosphorique |
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US (1) | US20180355457A1 (fr) |
CN (1) | CN108350527A (fr) |
AU (1) | AU2016356075A1 (fr) |
FR (1) | FR3044018B1 (fr) |
IL (1) | IL259307A (fr) |
MA (1) | MA42557B1 (fr) |
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US20180350246A1 (en) | 2017-06-05 | 2018-12-06 | X Development Llc | Methods and Systems for Sharing an Airspace Wide Unmanned Aircraft System Database Across a Plurality of Service Suppliers |
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US3711591A (en) | 1970-07-08 | 1973-01-16 | Atomic Energy Commission | Reductive stripping process for the recovery of uranium from wet-process phosphoric acid |
US4316877A (en) * | 1979-11-23 | 1982-02-23 | Allied Corporation | Extraction of uranium values from phosphoric acid |
US4402917A (en) | 1980-09-05 | 1983-09-06 | Allied Chemical Corporation | Extraction of uranium from phosphoric acid using supported extractants |
US4599221A (en) | 1983-08-01 | 1986-07-08 | The State Of Israel, Atomic Energy Commission, Nuclear Research Center Negev | Recovery of uranium from wet process phosphoric acid by liquid-solid ion exchange |
WO2013167516A1 (fr) | 2012-05-07 | 2013-11-14 | Areva Mines | Nouveaux composés bifonctionnels utiles comme ligands de l'uranium(vi), leurs procédés de synthèse et leurs utilisations |
WO2014018422A1 (fr) | 2012-07-21 | 2014-01-30 | K-Technologies, Inc. | Procédés de récupération d'uranium à partir d'acide phosphorique obtenu par voie humide à l'aide de techniques d'échange d'ions à cycle unique double ou double unique |
WO2014127860A1 (fr) | 2013-02-25 | 2014-08-28 | Commissariat à l'énergie atomique et aux énergies alternatives | Matériau hybride organique-inorganique, utile pour extraire l'uranium(vi) de milieux aqueux comprenant de l'acide phosphorique, ses procédés de préparation et ses utilisations |
FR3002951A1 (fr) * | 2013-03-11 | 2014-09-12 | Areva Mines | Utilisation de composes a fonctions amide et phosphonate pour extraire l'uranium(vi) de solutions aqueuses d'acide sulfurique, issues notamment de la lixiviation sulfurique de minerais uraniferes |
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PE20110691A1 (es) * | 2008-07-31 | 2011-10-23 | Urtek Llc | Extraccion de uranio a partir del acido fosforico por via humeda |
CA2767395C (fr) * | 2009-07-07 | 2018-03-06 | Cytec Technology Corp. | Procedes de recuperation de metaux a partir de solutions aqueuses |
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2015
- 2015-11-19 FR FR1561141A patent/FR3044018B1/fr active Active
-
2016
- 2016-11-21 WO PCT/EP2016/078292 patent/WO2017085311A1/fr active Application Filing
- 2016-11-21 CN CN201680066596.2A patent/CN108350527A/zh active Pending
- 2016-11-21 MA MA42557A patent/MA42557B1/fr unknown
- 2016-11-21 TN TNP/2018/000168A patent/TN2018000168A1/fr unknown
- 2016-11-21 AU AU2016356075A patent/AU2016356075A1/en not_active Abandoned
- 2016-11-21 US US15/776,993 patent/US20180355457A1/en not_active Abandoned
-
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- 2018-05-13 IL IL259307A patent/IL259307A/en unknown
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US4599221A (en) | 1983-08-01 | 1986-07-08 | The State Of Israel, Atomic Energy Commission, Nuclear Research Center Negev | Recovery of uranium from wet process phosphoric acid by liquid-solid ion exchange |
WO2013167516A1 (fr) | 2012-05-07 | 2013-11-14 | Areva Mines | Nouveaux composés bifonctionnels utiles comme ligands de l'uranium(vi), leurs procédés de synthèse et leurs utilisations |
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WO2014127860A1 (fr) | 2013-02-25 | 2014-08-28 | Commissariat à l'énergie atomique et aux énergies alternatives | Matériau hybride organique-inorganique, utile pour extraire l'uranium(vi) de milieux aqueux comprenant de l'acide phosphorique, ses procédés de préparation et ses utilisations |
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Also Published As
Publication number | Publication date |
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TN2018000168A1 (fr) | 2019-10-04 |
MA42557B1 (fr) | 2019-10-31 |
AU2016356075A1 (en) | 2018-05-31 |
CN108350527A (zh) | 2018-07-31 |
IL259307A (en) | 2018-07-31 |
FR3044018A1 (fr) | 2017-05-26 |
US20180355457A1 (en) | 2018-12-13 |
FR3044018B1 (fr) | 2017-12-22 |
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