PROCESS FOR EXTRACTING TANTALUM AND NIOBIUM FROM AN AQUEOUS ACIDIC SOLUTION

Abstract

A process and an installation wherein a ternary system including an aqueous acidic solution, an organic solvent not miscible with water and a thermosensitive hydrotropic agent is used to selectively extract tantalum and optionally niobium by cycling extraction between low-temperature single-phase and high temperature two phase regions in the ternary phase prism far from the critical point.

Claims

1-16. (canceled)

17. A process for extracting, from an aqueous acidic solution, tantalum, in the form of a cationic salt, said process comprising at least the steps of: (i) providing, at a first temperature T1, a ternary mixture comprising: a) an aqueous acidic solution containing a mixture of metallic elements including at least tantalum to be extracted, b) an organic solvent not miscible with water, c) a quantity Q1 of a thermosensitive hydrotropic agent comprising a hydrophilic part and a hydrophobic part, T1 being comprised between 15 C. and 35 C. and being inferior to the critical temperature of said ternary mixture, (ii) heating said ternary mixture at a second temperature T2 at which said mixture presents a biphasic structure consisting of an aqueous phase and an organic phase at least partially loaded in at least tantalum, wherein T2 is comprised between 40 C. and 75 C., is superior to the critical temperature of said ternary mixture and is distinct by 15 C. to 50 C. from T1, (iii) separating, from the biphasic structure obtained in step (ii), said organic phase and said aqueous phase, (iv) extracting at least tantalum from said organic phase, wherein: said ternary mixture of step (i) is in a phase boundary pre-Ouzo zone, said pre-Ouzo zone being characterized as an ultra-flexible surfactant-free micro-emulsion comprising dynamic aggregates of about 20 to 300 molecules bound together, said hydrophilic part of said hydrotropic agent comprises at least one ethoxy group, the molarity of said aqueous acidic solution is at least 2M.

18. The process according to claim 17, wherein the concentration of said tantalum in said aqueous acidic solution is comprised between 0.1 g/L and 10 g/L.

19. The process according to claim 17, wherein the molarity of the aqueous acidic solution ranges from 2 M to 12 M.

20. The process according to claim 17, wherein said acidic aqueous solution comprises a strong acid chosen among sulphuric acid and nitric acid.

21. The process according to claim 17, wherein the molarity of said aqueous acidic solution is at least 5M and the process is for selectively extracting tantalum and niobium from said aqueous acidic solution.

22. The process according to claim 17, wherein the amount of said acidic aqueous solution in the ternary mixture of step (i) ranges from 10 to 90 weight % relative to the total weight of the ternary mixture.

23. The process according to claim 17, wherein said organic solvent is chosen among 1-octanol, 2-octanol, methyl isobutyl ketone, cyclohexanone, and tributylphosphate.

24. The process according to claim 17, wherein the amount of said organic solvent in the ternary mixture of step (i) ranges from 5 to 70 weight % relative to the total weight of the ternary mixture.

25. The process according to claim 17, wherein said hydrotropic agent is 1-propoxy-2-propanol or dipropylene glycol n-propyl ether.

26. The process according to claim 17, wherein the amount of said quantity Q1 of the hydrotropic agent in the ternary mixture of step (i) ranges from 10 to 55 weight % relative to the total weight of the ternary mixture.

27. The process according to claim 17, wherein T1 ranges from 20 C. to 30 C.

28. The process according to claim 17, wherein T2 ranges from about 45 C. to 70 C.

29. The process according to claim 17, wherein steps (i) to (iii) are reiterated at least once before step (iv) is carried out and after bringing said ternary mixture back to temperature T1.

30. The process according to claim 29, wherein said process comprises, after step (iii) and before each reiteration of steps (i) to (iii), at least the following sub-steps: (1a) cooling the aqueous phase recovered at step (iii) to temperature T1, (2a) mixing said aqueous phase with said organic solvent and said hydrotropic agent to obtain said ternary mixture, and (3a) adjusting the amount of said hydrotropic agent in said ternary mixture to said quantity Q1.

31. The process according to claim 29, wherein said process comprises, after step (iii) and before each reiteration of steps (i) to (iii), at least the following sub-steps: (1b) cooling the organic phase recovered at step (iii) to temperature T1, (2b) mixing said organic phase with a new aqueous acidic solution containing a mixture of metallic elements including at least tantalum to be extracted and said hydrotropic agent to obtain said ternary mixture, and (3b) adjusting the amount of said hydrotropic agent in said ternary mixture to said quantity Q1.

32. An installation for carrying out the process as defined in claim 17, wherein said installation comprises at least: a mixing chamber for preparing a ternary mixture comprising a) an aqueous acidic solution containing a mixture of metallic elements including at least tantalum to be extracted, b) an organic solvent not miscible with water, c) a quantity Q1 of a hydrotropic agent comprising a hydrophilic part and a hydrophobic part, said hydrophilic part comprising at least one ethoxy group, a heating device for heating said ternary mixture, a cooling device, means for conveying said aqueous acidic solution, said organic solvent, said thermosensitive hydrotropic agent and said mixture, and means for controlling at least the flow and the temperature of said solutions and mixture.

Description

BRIEF DESCRIPTION OF DRAWINGS

[0022] FIG. 1A represents the phase diagram at 25 C. and 60 C. of a ternary mixture of an aqueous phase, PnP and 2-octanol according to example 1.

[0023] FIG. 1B represents the Ta/Nb separation coefficient depending on the monophasic starting composition.

[0024] FIG. 2 represents an example of a flow diagram of several reaction cycles combining the flux of aqueous and organic phases in a counter-current arrangement.

[0025] FIG. 3 represents a scheme of performing the extraction according to the invention in the form of a cascade which allows to recycle the hydrotropic agent.

DETAILED DESCRIPTION

[0026] In a first aspect, the invention relates to a process for extracting, from an aqueous acidic solution, tantalum, in the form of a cationic salt, said process comprising at least the steps of: [0027] (i) providing, at a first temperature T1, a ternary mixture comprising: a) an aqueous acidic solution containing a mixture of metallic elements including at least tantalum to be extracted, b) an organic solvent not miscible with water, c) a quantity Q1 of a thermosensitive hydrotropic agent comprising a hydrophilic part and a hydrophobic part, T1 being comprised between 15 C. and 35 C. and being inferior to the critical temperature of said ternary mixture, [0028] (ii) heating said ternary mixture at a second temperature T2 at which said mixture presents a biphasic structure consisting of an aqueous phase and an organic phase at least partially loaded in at least tantalum, wherein T2 is comprised between 40 and 75 C., is superior to the critical temperature of said ternary mixture and is distinct by 15 C. to 50 C. from T1, [0029] (iii) separating, from the biphasic structure obtained in step ii), said organic phase and said aqueous phase, [0030] (iv) extracting at least tantalum from said organic phase, [0031] wherein: [0032] said ternary mixture of step i) is in a phase boundary pre-Ouzo zone, said pre-Ouzo zone being characterized as an ultra-flexible surfactant-free micro-emulsion comprising dynamic aggregates of about 20 to 300 molecules bound together, [0033] said hydrophilic part of said hydrotropic agent comprises at least one ethoxy group, [0034] the molarity of said aqueous acidic solution is at least 2M.

[0035] A ternary mixture in a pre-Ouzo zone, which is also designated as surfactant-free micro emulsion or ultra-flexible micro emulsion, is characterized by the combination of the following properties: [0036] comprises aggregates of more than 30 molecules locally covered by a partial monolayer of hydrotropic agent, such as defined in Th. Zemb et al., Proceedings of the National academy of science of the USA, 2016, 113(16), 4260-4262. [0037] the static light scattering gives an apparent average aggregate mass of more than 30 times of the molecular mass of the solvent used, [0038] the ternary mixture is far from its critical point, wherein for each component, the difference between said critical point and its mass percentage is of at least 3%, preferably of at least 5% and more preferably of at least 8% in the case of tantalum and niobium.

[0039] According to the invention, a hydrotropic agent is a compound that is soluble in both an aqueous and an organic phase. More precisely, a hydrotropic agent is a compound that solubilizes hydrophobic compounds in aqueous solutions. Hydrotropes typically consist of a hydrophilic part and a hydrophobic part (like surfactants), but the latter is usually too short to cause spontaneous self-aggregation and micelle formation (J. Mehringer, Werner Kunz, 2021, Advances in Colloid and Interface Science 294, 102476). There are acidic, basic or salt electrolyte hydrotropes and non-electrolyte hydrotropes. Their molecular volume is greater than 0.090 nm3 and less than 0.5 nm.sup.3. According to the present invention, said hydrotropic agent is miscible in water as well as in the organic solvent not miscible with water, and which, when present at the quantity Q1 (also denoted minimum hydrotrope concentration (MHC)), allows a significant solubilisation of at least tantalum in the form of an anionic salt. A hydrotropic agent reduces the surface tension of water without forming micelles by itself. This micellisation is evidenced by the existence of a plateau of surface pressure versus hydrotrope concentration.

[0040] According to the invention, the terms thermosensitive hydrotropic agent, refers to a hydrotropic agent able to introduce thermosensitivity to the demixing compositions of the ternary mixture of said hydrotropic agent, the organic solvent and the hydrophobic agent.

[0041] According to the invention, the terms dynamic aggregates refers to aggregates in aqueous solutions that show a critical aggregate concentration (determined by any standard technique such as surface tension) equal or more than 0.1M at room temperature (S. Schttl and D. Horinek, Current opinion in Colloid & Interface Science, vol. 22 (2016) pp. 8-13).

[0042] The process according to the invention presents the advantage of using a simple ternary system wherein the properties of the organic solvent and of the hydrotropic agent are combined in a single, monophasic, ternary mixture. In the process according to the invention, steps (i) to (ill) may be repeated in a cyclic process comprising n reaction cycles, by combining the flux of aqueous and organic phases in a counter-current arrangement.

[0043] In a process according to the invention, the diameter of aggregates in said ternary mixture at step (i) is determined by any appropriate method known by a person skilled in the art, preferably by X-ray light scattering with a correlation length above 2 nm.

[0044] According to the present invention, by surfactant-free monophasic micro-emulsion structure it is intended a monophasic ternary mixture having a micro-emulsion-like structure in the absence of any surfactant within said mixture. The absence of surfactant or detergent provides to a process according to the invention the advantage of being easier to implement and to avoid the necessity of eliminating said detergent.

[0045] The aqueous acidic solution containing a mixture of metallic elements including at least tantalum to be extracted according to the process of the invention is for example an acid concentration of ores or waste. The concentration of said tantalum in said aqueous acidic solution is preferably comprised between 0.1 to 10 g/L.

[0046] According to the invention, said acidic solution may be any solution comprising a strong acid and having a molarity ranging from 2 M to about 12 M. According to a preferred embodiment, the strong acid is sulphuric acid or nitric acid, sulphuric acid being particularly preferred.

[0047] According to a particular embodiment of the present invention, the molarity of said aqueous acid solution is at least 5 M. In that case, the process according the invention allows not only extraction of tantalum but also the extraction of niobium. Therefore, according to this particular embodiment, the molarity of said aqueous acidic solution is at least 5M and the process according to the present invention is for selectively extracting tantalum and niobium from said aqueous acidic solution.

[0048] The amount of said aqueous solution in the ternary mixture of step (i) may range from about 10 to 90 weight % (wt. %) and preferably from about 15 to 80 wt. % relative to the total weight of the ternary mixture.

[0049] According to the present invention, not miscible with water regarding the organic solvent refers to an organic solvent that cannot mix with water and forms a heterogeneous mixture. More precisely, said definition encompasses solvents which miscibility in water is less than 0.001 mole fraction and wherein the miscibility of water in said solvents is more than 0.1 mole fraction.

[0050] According to a particular embodiment of the present invention, said organic solvent is chosen among fatty alcohols having a carbon chain comprising at least 8 carbon atoms, Guerbet alcohols, ethyl acetates, aldehydes, ketones, phosphorus-based non-ionic liquids, amides, carbollides, carboranes, and phosphonates.

[0051] In a particular and preferred embodiment of the invention, said organic solvent is chosen among: 1-octanol, 2-octanol, methyl isobutyl ketone (MIBK,) cyclohexanone, and tributylphosphate (TBP). Among these organic solvents, 1-octanol and 2-octanol are particularly preferred.

[0052] The amount of said organic solvent in the ternary mixture of step (i) may range from about 5 to 70 weight % (wt. %) and preferably from about 5 to 50 wt. % relative to the total weight of the ternary mixture.

[0053] According to the invention, said quantity Q1 of the hydrotropic agent is typically above 10 weight % of said ternary mixture weight, preferably from 10 weight % to 55 weight % of said ternary mixture total weight, more preferably from 20 weight % to 50 weight % of said ternary mixture weight.

[0054] Examples of said hydrotropic agents are: propylene glycol alkyl ethers, with alkyl being chosen among: methyl, ethyl, propyl, isopropyl, butyl, isobutyl and pentyl, such as 1-propoxy-2-propanol (PnP), and dipropylene glycol n-propyl ether (dPnP).

[0055] Among these hydrotropic agents, 1-propoxy-2-propanol is particularly preferred.

[0056] In a particular embodiment of the process according to the invention, step (i) first comprises the mixing of said organic solvent and said hydrotropic agent, then it comprises the addition of said aqueous acidic solution, so as to prepare the ternary mixture of step (i).

[0057] According to the invention, both T1 and T2 differ from the critical temperature of said ternary mixture, wherein the respective difference between T1 or T2 and the critical temperature of said ternary mixture is of at least 3 C., preferably of at least 5 C., more preferably of at least 10 C.

[0058] The critical temperature of a given ternary mixture is easily determined by established methods such as the one described in: Alberto Arce, Alberto Arce, Jr., and Oscar Rodriguez, J. Chem. Eng. Data 2022, 67, 286-296.

[0059] According to a preferred embodiment of the present invention, T1 ranges from about 15 to 35 C. and more preferably from about 20 to 30 C.

[0060] According to a preferred embodiment of the present invention, T2 ranges from about 45 to 70 C. and more preferably from about 50 to 65 C.

[0061] Heating of the ternary mixture provided in step (i) from temperature T1 to temperature T2 at step (ii) can be carried out by any means or devices known by a person skilled in the art to appropriately heat said mixtures. As an example, one can mention microwave or Bain Marie.

[0062] At step (iii), said organic phase can be separated from said aqueous phase by any appropriate means such as for example by draining, pipetting, centrifugation, etc.

[0063] In step (ii), temperature T2 is maintained for a duration sufficient for phase separation to occur and solvent extraction of at least tantalum from the ternary mixture to the organic phase, typically for 1 to 20 minutes. If necessary for intensification, the process can be accelerated by a factor of hundred using centrifugal extractor of low acceleration (<3000 g)

[0064] According to the invention, both T1 and T2 differ from the critical temperature of said ternary mixture, wherein the respective difference between T1 or T2 and the critical temperature of said ternary mixture is of at least 3 C., preferably of at least 5 C., more preferably of at least 10 C. In a particular embodiment of the invention, during step ii) the ternary mixture may be centrifuged. This centrifugation carried out during said step ii) is intended to facilitate and/or to accelerate the extraction of at least tantalum according to the process of the invention.

[0065] According to a particular and preferred embodiment of the present invention, steps (i) to (iii) are reiterated at least once, more preferably from 2 to 20 times and even more preferably from 3 to 6 times, before step (iv) is carried out and after bringing said ternary mixture back to temperature T1.

[0066] In that case, and according to a first mode of realisation of this particular embodiment, the process comprises, after step (iii) and before each reiteration of steps (i) to (iii), at least the following sub-steps: [0067] (1a) cooling the aqueous phase recovered at step (iii) to temperature T1, [0068] (2a) mixing said aqueous phase with said organic solvent and said hydrotropic agent to obtain said ternary mixture, and [0069] (3a) adjusting the amount of said hydrotropic agent in said ternary mixture to said quantity Q1.

[0070] This first mode of realisation is preferably carried out when a single iteration of steps (i) to (iii) is not sufficient to extract all tantalum initially present in the initial aqueous acidic solution or to further extract niobium from said initial aqueous acidic solution. In this later case the molarity of the aqueous acid solution is then adjusted to at least 5 M to extract niobium.

[0071] According to a second mode of realisation of this particular embodiment, the process comprises, after step (iii) and before each reiteration of steps (i) to (iii), at least the following sub-steps: [0072] (1b) cooling the organic phase recovered at step (iii) to temperature T1, [0073] (2b) mixing said organic phase with a new aqueous acidic solution containing a mixture of metallic elements including at least tantalum to be extracted and said hydrotropic agent to obtain said ternary mixture, and [0074] (3b) adjusting the amount of said hydrotropic agent in said ternary mixture to said quantity Q1.

[0075] This second mode of realisation is preferably carried out to obtain an organic phase highly concentrated in at least tantalum.

[0076] In both the first and second modes of realisation of this particular embodiment, adjusting the amount of said hydrotropic agent in said ternary mixture to said quantity Q1 at step (3a) or (3b) is needed in order to keep the efficient performance in distribution coefficient during step (ii).

[0077] In both the first and second modes of realisation of this particular embodiment, the cooling steps (1a) and (1b) from temperature T2 to temperature T1 can be carried out thanks to any cooling devices such as for example an ice bath or refrigerated devices.

[0078] At step (iv), extracting tantalum from said organic phase may be carried by washing said organic phase with aqueous acidic solution. As an example, when the organic solvent of the organic phase is octanol, said organic phase can be washed out with a 0.1 to 0.2 M aqueous sulfuric acid solution to transfer tantalum from the organic phase to the aqueous sulfuric acid solution. As another example and when the organic phase comprises both tantalum and niobium, said organic phase is firstly washed out with a 3.5 to 4.0 M first aqueous sulfuric acid solution to transfer niobium from the organic phase to said first aqueous sulfuric acid solution, and then said organic phase is secondly washed out with a 0.1 to 0.2 M second aqueous sulfuric acid solution to transfer tantalum from the organic phase to said second aqueous sulfuric acid solution.

[0079] In a second aspect, the present invention relates to an installation for extracting of at least tantalum in the form of an anionic salt, according to the process defined according to the first aspect of the present invention. More particularly, the present invention relates to an installation for carrying out the process according to the invention, wherein said installation comprises at least:

[0080] a mixing chamber for preparing a ternary mixture comprising a) an aqueous acidic solution containing a mixture of metallic elements including at least tantalum to be extracted, b) an organic solvent not miscible with water, c) a quantity Q1 of hydrotropic agent comprising a hydrophilic part and a hydrophobic part, said hydrophilic part comprising at least one ethoxy group, [0081] a heating device for heating said ternary mixture, [0082] a cooling device, [0083] means for conveying said aqueous acidic solution, said organic solvent, said thermosensitive hydrotropic agent and said mixture, and [0084] means for controlling at least the flow and the temperature of said solutions and mixture.

[0085] Further features and advantages of the invention will be apparent from the detailed description of the following examples, as well as from the attached figures in which:

[0086] FIG. 1A represents the phase diagram at 25 C. and 60 C. of a ternary mixture of an aqueous phase, PnP and 2-octanol according to example 1. FIG. 1B represents the Ta/Nb separation coefficient depending on the monophasic starting composition.

[0087] FIG. 2 represents an example of a flow diagram of several reaction cycles combining the flux of aqueous and organic phases in a counter-current arrangement. In a first stage, an initial aqueous acidic solution 1 containing a mixture of metallic elements including at least tantalum to be extracted and a thermosensitive hydrotropic agent, is combined, in a first mixing chamber 2a, with an organic phase 5b coming from a second mixing chamber 2b and a thermosensitive hydrotropic agent at a temperature T1 to form a homogeneous, nanostructured ternary mixture 3a in which the amount of said hydrotropic agent is equal to Q1. Next, the ternary mixture 3a is separated into two phases with the help of a heating device (not represented) reaching temperature from T1 to T2 and their density differences. This creates an aqueous raffinate 4a mainly containing the undesired metal(s) and an organic phase 5a at least partially loaded in at least tantalum. In a second stage, the aqueous raffinate 4a is sent towards the second mixing chamber 2b and mixed with an organic phase 5c coming from a third mixing chamber 2c and with a sufficient amount of a thermosensitive hydrotropic agent coming from a container 6b, to form a homogeneous, nanostructured ternary mixture 3b in which the amount of said hydrotropic agent is readjusted to said quantity Q1, said hydrotropic agent being identical to the hydrotropic agent used in the first step of the process. Next, the ternary mixture 3b is separated into two phases with the help of a heating device (not represented) reaching temperature from T1 to T2 and their density differences. This step creates an aqueous raffinate 4b mainly containing the undesired metal(s) and an organic phase 5b at least partially loaded in at least tantalum. In a third stage, the aqueous raffinate 4b is sent towards a third mixing chamber 2c and mixed with a fresh organic solvent 7 and with a sufficient amount of a thermosensitive hydrotropic agent coming from a container 6c, to form a homogeneous, nanostructured ternary mixture 3c in which the amount of said hydrotropic agent is readjusted to said quantity Q1, said hydrotropic agent being identical to the hydrotropic agent used in the first and second steps of the process. When the process is ended, each of the tantalum-loaded organic phases 5a, 5b and 5c can be recovered. The aqueous phase 8 coming from the third mixing chamber 2c and containing unwanted metallic elements can be removed.

[0088] FIG. 3 represents a scheme of performing the extraction according to the invention in the form of a cascade which allows to recycle the hydrotropic agent. In the first step, an [A] initial aqueous acidic phase containing water, sulphuric acid, PnP (1-propoxy-2-propanol), and the metal salts is combined with a [B] initial organic phase containing PnP and 2-octanol at a temperature T1 to form a [C] homogeneous, nanostructured ternary mixture in a mixing chamber. Next, the mixture is separated into two phases with the help of a [D] heating device (spiral) reaching temperature from T1 to T2 and [E] their density differences. This step creates an [F] aqueous raffinate mainly containing the undesired metal(s) and a [G] tantalum partially-loaded organic phase. By adding [A] fresh aqueous phase, this step can be [T] repeated until a [H] tantalum fully-loaded organic phase is achieved. The [F] aqueous raffinate can be recycled by loading it with desired metals again.

EXAMPLE: Separation of Tantalum and Niobium

[0089] The present example describes selective extraction of tantalum and niobium by a process of the invention.

[0090] A ternary mixture is prepared, comprising: [0091] an acidic aqueous phase of 4 M sulphuric acid, comprising niobium and tantalum. [0092] 1-Propoxy-2-propanol (PnP) as temperature-sensitive hydrotropic agent, to ensure the miscibility of aqueous phase and the organic solvent, [0093] 2-octanol as organic solvent not miscible with water.

[0094] The phase diagram for this system at 25 and 60 C. and the separation coefficient are respectively indicated in FIGS. 1A and 1B.

[0095] As it can be seen on this figure, the distribution coefficient (kD) as well as the Ta/Nb separation coefficient (InS) show two maxima around the compositions reported in Table 1 below:

TABLE-US-00001 TABLE 1 Maxima 1 .sup.kD = 3.2 9.3 wt % 38.2 wt % 52.5 wt % InS = 4.2 2-Octanol PnP aq. phase Maxima 2 .sup.kD = 5.3 20.6 wt % 48.7 wt % 30.8 wt % InS = 6.9 2-Octanol PnP aq. phase

[0096] In a first step, aqueous phase, PnP and 2-octanol were mixed as follows: PnP and 2-octanol were mixed in a proportion of 0.82 and 0.18 with a tolerance +/0.02, then the aqueous solution was added to obtain a mass fraction 0.4/0.1/0.5for PnP/2-octanol/aqueous solution, with a possible variation of 0.03 for each component (the points being in between the two lines drawn for 25 C and 60 C).

[0097] Mixing the three components at low temperature T1 at 25 C., of this composition resulted in the formation of a homogeneous, nanostructured micro-emulsions exhibiting certain advantages such as high contact surface between aqueous and organic phase, low viscosity and fast achievement of thermodynamic equilibrium. At this temperature, the ions distributed between the existing aqueous and organic pseudo phases according to the distribution coefficient.

[0098] In a second step, the temperature was increased to 60 C. (T2). Due to the temperature-sensitivity of the hydrotropic agent, the phase borders of the ternary system changed as indicated in FIG. 1A. The result was a phase separation into an aqueous-rich and an organic-rich phase. The distribution coefficient was above 50 in favour of the solvent phase as shown in FIG. 1, allowing separation from iron and purification by associating elements in cascade This step can be accelerated by the use of a centrifuge. The volume ratio between these two phases is depending on the tie-line of the phase diagram at 60 C. Tantalum was mainly transferred into the organic-rich phase while niobium mainly stays in the aqueous phase. The separation coefficient is high and depends on the initial composition of the phase diagram (cf. FIG. 1B).

[0099] The number of cycling steps and consequently the separation between the two metals can be increased by combining the flux of aqueous and organic phase in a counter-current arrangement, as shown in FIG. 2. In each step, an aqueous phase and an organic phase are mixed at room temperature in an appropriate volume ratio to achieve a homogeneous phase. After that, the temperature is increased again to separate the two resulting phases that are transferred to the next cycling chambers. From 3 to 20 cycles comprising steps ii) and iii) can be performed, preferably from 6 to 10 cycles.