INORGANIC ION-EXCHANGER FOR SELECTIVE EXTRACTION OF LITHIUM FROM LITHIUM-CONTAINING NATURAL AND INDUSTRIAL BRINES

Abstract

The invention relates to lithium-selective inorganic ion exchangers for the extraction of lithium from lithium-containing natural and technological brines. More specifically, invention relates to a technology for recovering lithium in the presence of oxidizing or reducing agents. The inorganic ion-exchanger is present in the form of solid particles which are represented by a chemical non-stoichiometric compound in the form of an inorganic polymeric aqua-oxo-hydroxo complex intended for selective extraction of lithium from lithium-containing natural and industrial brines, the inorganic ion-exchanger being represented by the following general formula:

H.sub.aNbO.sub.(2.5+0.5.Math.a).Math.bL.sub.2O.Math.cWO.sub.3.Math.dH.sub.2O;

wherein: “a” is a number ranging from 0.5 to 2.0, “b” is a number ranging from 0.01 to 0.5, “c” is a number ranging from 0.01 to 0.2, and “d” is a number ranging from 0.1 to 2.0.

Claims

1. An inorganic ion-exchanger in the form of solid particles comprising a chemical non-stoichiometric compound in the form of an inorganic polymeric aqua-oxo-hydroxo complex intended for selective extraction of lithium from lithium-containing natural and industrial brines, the inorganic ion-exchanger being represented by the following general formula:
H.sub.aNbO.sub.(2.5+0.5.Math.a).Math.bLi.sub.2O.Math.cWO.sub.3.Math.dH.sub.2O; wherein: “a” is a number ranging from 0.5 to 2.0, “b” is a number ranging from 0.01 to 0.5, “c” is a number ranging from 0.01 to 0.2, and “d” is a number ranging from 0.1 to 2.0.

2. The inorganic ion-exchanger, according to claim 1, wherein the polymeric aqua-oxo-hydroxo complex is a polymeric aqua-oxo-hydroxo complex of niobium and tungsten.

3. The inorganic ion-exchanger, according to claim 2, wherein the polymeric aqua-oxo-hydroxo complex of niobium and tungsten is a mixed polynuclear complex.

4. The inorganic ion-exchanger, according to claim 1, which has a total ion exchange capacity of at least 2.8 meq/g and an ion-exchange capacity specifically to lithium of at least 2.3 meq/g.

5. The inorganic ion-exchanger, according to claim 2, which has a total ion exchange capacity of at least 2.8 meq/g and an ion-exchange capacity specifically to lithium of at least 2.3 meq/g.

6. The inorganic ion-exchanger, according to claim 3, which has a total ion exchange capacity of at least 2.8 meq/g and an ion-exchange capacity specifically to lithium of at least 2.3 meq/g.

7. The inorganic ion-exchanger of claim 1, wherein the solid particles have dimensions in the range of 0.1 to 2.0 mm.

8. The inorganic ion-exchanger of claim 2, wherein the solid particles have dimensions in the range of 0.1 to 2.0 mm.

9. The inorganic ion-exchanger of claim 4, wherein the solid particles have dimensions in the range of 0.1 to 2.0 mm.

10. The inorganic ion-exchanger of claim 6, wherein the solid particles have dimensions in the range of 0.1 to 2.0 mm.

11. The inorganic ion-exchanger of claim 1, which is obtained by a method comprising the steps of: interacting a soluble niobate (V) with an acid that contains at least one tungsten (VI) compound, thus forming a hydrated niobium (V) oxide and a hydrated tungsten (VI) oxide, which co-precipitate and form mixed hydrated niobium (V) and tungsten (VI) oxides; granulating the mixed hydrated niobium (V) and tungsten (VI) oxide by freezing with subsequent defreezing, thus obtaining a granulated mixed hydrated niobium (V) and tungsten (VI) oxide; converting the granulated mixed hydrated niobium (V) and tungsten (VI) oxide into a lithium form by treating thereof with a lithium-containing compound selected from the group consisting of aqueous solutions of lithium hydroxide and lithium carbonate; calcining the lithium form of the granulated mixed hydrated niobium (V) and tungsten (VI) oxide to obtain a mixed, granulated tripled mixed lithium, niobium (V) and tungsten (VI) oxide, which constitutes a lithium-form of the inorganic ion-exchanger; and converting the lithium-form of the inorganic ion-exchanger into an H-form of the inorganic ion-exchanger by treating thereof with an acid solution.

Description

BRIEF DESCRIPTION OF THE DRAWING

[0013] FIG. 1 shows the dependence of the capacity on lithium (E.sub.Li), the capacity on lithium (E.sub.Na) and the separation factor for the ion of lithium and sodium (P.sub.Li,Na) on the content in the sorbent of tungsten ions, where α is the content of W.sup.6+ in the sorbent in atomic percent; In this drawing, Curve E.sub.Li corresponds to lithium sorbent capacity obtained by using a lithium and sodium salts solution at the ionic ratio Li.sup.+:Na.sup.+=1:10, pH=12; Curve E.sub.Na corresponds to sodium capacity of the sorbent obtained from the same solution; Curve P.sub.Li,Na corresponds to the separation factor for the ion of lithium and sodium obtained from the same solution; the calcination temperature of the samples was 500±20° C.

SUMMARY OF THE INVENTION

[0014] The invention provides an ion-exchanger selective to lithium. Such an ion-exchanger is intended to extract lithium from natural and technological brines.

[0015] An inorganic ion-exchanger of the present invention is a chemical non-stoichiometric compound, which constitutes an inorganic polymeric aqua-oxo-hydroxo complex intended for selective extraction of lithium from lithium-containing natural and industrial brines and represented by the following general formula:

H.sub.aNbO.sub.(2.5+0.5.Math.a).Math.bL.sub.2O.Math.cWO.sub.3.Math.dH.sub.2O;

wherein: [0016] “a” is a number ranging from 0.5 to 2.0, [0017] “b” is a number ranging from 0.01 to 0.5, [0018] “c” is a number ranging from 0.01 to 0.2, and [0019] “d” is a number ranging from 0.1 to 2.0.

[0020] If the value of “a” is less than 0.5, the sorbent's ion-exchange capacity will decrease, and this, in turn, will decrease the sorbent efficiency. The value of “a” exceeding 2.0 will increase the solubility of the sorbent and thus will increase the loss of the sorbent in multiple-cycle processes of sorption-desorption.

[0021] The parameter “b” has a value that varies from 0.01 to 0.5, depending on the parameter “c” and the material synthesis temperature. In other words, If the value of “c” is less than 0.01, this will decrease the sorbent ion exchange capacity and the sorbent efficiency. The same result will occur if the value of “c” exceeds 0.2.

[0022] If the value of “d” is less than 0.1, this will decrease the ion-exchange capacity of the sorbent and thus reduce its performance efficiency. On the other hand, if the value of “d” exceeds 2.0, this will increase the solubility of the sorbent and thus will increase the loss of the sorbent in multiple-cycle processes of sorption-desorption (see data in the tables below).

DETAILED DESCRIPTION OF THE INVENTION

[0023] The invention relates to the field of chemical technology, namely, to selective inorganic sorbents (inorganic ion-exchangers) for extracting lithium from natural and technological brines. The invention may be used to extract lithium from neutral and slightly alkaline solutions with a high content of sodium ions and ions of other metals. In particular, the invention relates to an inorganic ion-exchanger for selective extraction of lithium from lithium-containing natural and industrial brines.

[0024] The term “brines” used in the context of the present patent specification covers any natural or technological solutions that contain lithium.

[0025] Ion exchangers, also known as ionic sieves, are inorganic ion-exchange sorbents that exhibit the so-called ion-sieve effect, which is the effect of separation of ions in a solution following the difference in their ionic radii and charges. Dimensions of ionic positions in the material's crystal structure correspond to certain ions; therefore, larger size ions cannot enter unspecified positions. A unique feature of the ion-exchanger of the invention is its specific structure that provides high selectivity, especially to lithium ions.

[0026] It is also important to note that in the context of the present specification, the term “mixed hydrated niobium and tungsten oxide” does not mean a mechanical mixture of the hydrated niobium oxide with a hydrated tungsten oxide but rather means a chemical compound of a non-stoichiometric composition.

[0027] The objective of the invention is to provide an ion-exchanger selective to lithium. Such an ion-exchanger is intended to extract lithium from natural and technological brines.

[0028] An inorganic ion-exchanger of the present invention is a chemical non-stoichiometric compound, which constitutes an inorganic polymeric aqua-oxo-hydroxo complex intended for selective extraction of lithium from lithium-containing natural and industrial brines and represented by the following general formula:

H.sub.aNbO.sub.(2.5+0.5.Math.a).Math.bL.sub.2O.Math.cWO.sub.3.Math.dH.sub.2O;

wherein: [0029] “a” is a number ranging from 0.5 to 2.0, [0030] “b” is a number ranging from 0.01 to 0.5, [0031] “c” is a number ranging from 0.01 to 0.2, and [0032] “d” is a number ranging from 0.1 to 2.0

[0033] If the value of “a” is less than 0.5, the sorbent's ion-exchange capacity will decrease, and this, in turn, will decrease the sorbent efficiency. The value of “a” exceeding 2.0 will increase the solubility of the sorbent and thus will increase the loss of the sorbent in multiple-cycle processes of sorption-desorption.

[0034] The parameter “b” has a value that varies from 0.01 to 0.5, depending on the parameter “c” and the material synthesis temperature.

[0035] If the value of “c” is less than 0.01, this will decrease the sorbent ion exchange capacity and the sorbent efficiency. The same result will occur if the value of “c” exceeds 0.2.

[0036] If the value of “d” is less than 0.1, this will decrease the ion-exchange capacity of the sorbent and thus reduce its performance efficiency. On the other hand, if the value of “d” exceeds 2.0, this will increase the solubility of the sorbent and thus will increase the loss of the sorbent in multiple-cycle processes of sorption-desorption (see data in the tables below).

[0037] For use in the lithium-extraction process, it is preferable to have the inorganic ion-exchanger of the invention in the form of solid particles with dimensions ranging from 0.1 to 2.0 mm. On the one hand, with the size of particles less than 0.1 mm, it will be difficult to handle the sorbent in ion-exchange columns because of the passage of the particles into the lower part of the column through the cells of the filtering partitions. In other words, the size of particles exceeding 2.0 mm will delay the ion-exchange rate because of retardation of diffusion of lithium in the sorbent particles that occur in the ion-exchange process.

[0038] As mentioned above, the inorganic polymeric aqua-oxo-hydroxo complex is a complex of niobium and tungsten. It is a mixed polynuclear complex with a total ion exchange capacity of at least 2.8 meq/g and an ion-exchange capacity specifically to lithium of at least 2.5 meq/g.

[0039] What is meant under the term “mixed polynuclear complex” in the context of the present patent application is polynuclear coordination compounds, in the molecules of which there are several metal atoms surrounded by ligands and linked to each other through bridging groups. Bi- and trinuclear coordination compounds are the most studied. When the number of metal atoms is large, such compounds are called coordination or metal-containing polymers, metal polymers. The ratio between polynuclear compounds and coordination polymers is the same as between monomers, oligomers, and polymers in carbon chain high molecular weight compounds. Polynuclear compounds are sometimes referred to as compounds containing cells of directly bonded metal atoms, commonly referred to as clusters. There are homo- and heterometallic polynuclear compounds. The materials that are the subject of this application are cross-linked polymeric polynuclear bimetallic coordination compounds.

[0040] More detailed information about a mixed polynuclear complex may be found in Haiduc J., “Polymeric Coordination Compounds”, Russian Chemical Reviews, 1961, 30 (9), pp. 498-526, and Bunker, Bruce C.; Casey, William H. The aqueous chemistry of oxides [First edition], ISBN 9780199384259, Oxford University Press, 2016, 604 p.

[0041] To better understand the present invention, it would be advantageous to consider a method of manufacturing the proposed ion-exchanger. This method is a subject matter of a pending parent patent application of the same applicants.

[0042] A method for producing the proposed inorganic ion exchanger consists in contacting soluble niobates (V) with an acid in the presence of tungsten (VI) salts at an atomic ratio of niobium to tungsten in the range from 1 to (0.04÷0.12) to obtain a mixed hydrated oxide of niobium and tungsten in the worm of a precipitate, which is then granulated and converted into a lithium form sorbent (hereinafter referred to as an ion exchanger). Granulation is carried out by freezing the resulting precipitate at a temperature of −4÷−10° C. for 24-48 hours, followed by defrosting the obtained precipitate.

[0043] This conversion into a lithium form is carried out by treating the obtained product with a solution of a lithium-containing compound selected from the group consisting of lithium hydroxide LiOH and lithium carbonate Li.sub.2CO.sub.3. As a result, a Li-form of a granulated mixed hydrated niobium and tungsten oxide is obtained. The obtained Li-form product is calcined at an elevated temperature, specifically at 450÷550° C.; the finished product is then treated with an acid solution selected from the group consisting of nitric acid (HNO.sub.3), hydrochloric acid (HCl), sulphuric acid (H.sub.2SO.sub.4), or chloric acid (HClO.sub.4), to obtain a target product, i.e., a hydrogen-form sorbent (from now on referred to as an H-form sorbent).

[0044] Soluble niobates suitable for use in the method of the invention method are represented by alkali metal orthoniobates, such as Li.sub.3NbO.sub.4, Na.sub.3NbO.sub.4, K.sub.3NbO.sub.4, Rb.sub.3NbO.sub.4, and Cs.sub.3NbO.sub.4.

[0045] Soluble compounds of tungsten (VI) suitable for use in the method of the invention may be represented by monotungstates based on the anion WO.sub.4.sup.2-selected from the group consisting of such compounds as Li.sub.2WO.sub.4, Na.sub.2WO.sub.4, K.sub.2WO.sub.4, Rb.sub.2WO.sub.4, Cs.sub.2WO.sub.4, and (NH.sub.4).sub.2WO.sub.4.

[0046] Examples of H-form sorbents are given below in the section of Examples in Table 1 (the Li-form sorbents are similar and therefore are not included).

[0047] The uniqueness of the proposed method lies in the fact that the step of contacting a soluble niobate (V) with acid is carried out in the presence of tungsten (VI) salts and in that the ionic ratio of niobium (V) to tungsten (VI) in their interaction ranges from 1 to (0.04÷0.12). Another feature is that calcination of the precipitate in the Li form is carried out at a temperature in the range of 450 to 550° C.

[0048] An optimal ratio between niobium and tungsten in the material is chosen based on the experimental data obtained in studying the dependence of the exchange capacitance of the sorbent on lithium and the separation coefficient for lithium and sodium ions on the content of tungsten ions in the sorbent (FIG. 1).

[0049] FIG. 1 shows the dependence of the capacity on lithium (E.sub.Li), the capacity on lithium (E.sub.Na) and the separation factor for the ion of lithium and sodium (P.sub.Li,Na) on the content in the sorbent of tungsten ions, where a is the content of W6+ in the sorbent in atomic percent; In this drawing, Curve E.sub.Li corresponds to lithium sorbent capacity obtained by using a lithium and sodium salts solution at the ionic ratio Li.sup.+:Na.sup.+=1:10, pH=12; Curve E.sub.Na corresponds to sodium capacity of the sorbent obtained from the same solution; Curve P.sub.Li,Na corresponds to the separation factor for the ion of lithium and sodium obtained from the same solution; the calcination temperature of the samples was 500±20° C.

[0050] The obtained data shown in FIG. 1 indicate that the maximum value of the exchange capacity and selectivity to lithium ions is exhibited by materials whose composition corresponds to the ratio of niobium to tungsten in the range of 1 to (0.04 to 0.12).

[0051] The above-described content of the components in the original composition is necessary to maintain the ratio of niobium and tungsten in solution before mixing at a level needed to obtain it in a solid product—mixed hydrated niobium and tungsten oxide. In other words, the entire amount of niobium and tungsten introduced into the system must pass into the solid-state contained in the precipitate.

[0052] The optimal conditions needed for heat treatment of the obtained granular material saturated with lithium ions were determined from the experimental data relating to sorption properties of sorbent samples prepared with various W(VI)/Nb(V) ratios in the solid phase. The samples were calcined at different temperatures. The results are shown in tables in examples, which illustrate the influence of the heat treatment temperature in the synthesis of the material on the sorption-selective properties and chemical stability of the obtained sorption materials.

[0053] The results of the experiments show that the optimum temperature for calcining the Li-form of the granulated mixed hydrated niobium and tungsten oxide to obtain granulated mixed lithium, niobium, and tungsten oxide (i.e., a tripled mixed oxide, which is a Li-form of an inorganic ion exchanger) is in the range of 400° C. to 500° C. The time needed to keep the material at this temperature for the formation of the sorbent structure should be in the range of 2 to 3 hours. If the heat treatment is carried out under these conditions. In that case, the obtained sorbent, which possesses the ion-sieve effect, acquires a maximum exchange capacity and selectivity to lithium ions and is characterized by minimal losses in alternating sorption-desorption cycles.

[0054] The remaining operations of the proposed method for obtaining the granulated sorbent based on the precipitate of a mixed hydrated niobium and tungsten oxide and saturating the granulated material with lithium were carried out under the same conditions as in the method disclosed in the U.S. Pat. No. 11,179,715 mentioned above of P. Kudryavtsev, et al. More specifically, the cation exchanger was prepared by precipitation of hydrated niobium pentoxide by mixing 0.1 M solutions of potassium niobate and ZrCl.sub.4 in hydrochloric acid, sorbent granulating, saturating the granular product with lithium ions from 0.05÷0.1 M solution of lithium carbonate and then calcinating the product at 500±25° C. for 2÷3 hours. After calcination and conversion to the H-form (treatment with 0.1-0.2 M nitric acid solution), the sorbent was ready for lithium sorption. The obtained sorbent was suitable for extracting lithium from neutral and slightly alkaline solutions in the presence of both oxidizing agents and reducing agents.

[0055] The effectiveness of the proposed method is illustrated by the examples given below. However, it is understood that these examples should not be construed as limiting the scope of the invention and that they are given only for illustrative purposes.

[0056] The following methods and instruments were used for processing the materials and measuring the properties of the obtained products mentioned in the subsequent examples.

[0057] Equipment and Procedures Used in the Method of the Invention

[0058] Ion-Exchange Column

[0059] As ion-exchange column used in the method of the invention was a standard chromatographic column with a diameter of up to 10 mm. The height of the sorbent layer was maintained in the range of 10 to 15 column diameters. The solution was fed through the column at a constant linear speed, in the range of 1 to 10 mm/s. The feed rate of the solution was maintained by means of a peristaltic pump. During sorption experiments, special measures were taken to prevent air from entering the sorbent layer and partially dry the sorbent granules.

[0060] Determination of the Content of Lithium

[0061] Determination of lithium in solutions was carried out by the method of emission photometry of a flame. The most intense resonance line in the spectrum of lithium, 670.8 nm, was used for the analysis. This line corresponds to the transition between the energy levels 2.sup.2S.sub.1/2 and 2.sup.2p0.sub.3/2 at the excitation energy of 1.85 eV. In determining lithium (with the use of the FLAME PHOTOMETER, FP8000 series device; A.KRÜSS Optronic), the sensitivity of the method was 0.001-0.0005 μg Li/ml. Lithium content was determined from the calibration based on reference solutions prepared based on pure metal salts and their mixtures present in the solutions under study, which were close in proportion to the test solutions. Determination of sodium content was carried out similarly.

[0062] Determination of the Content of Tungsten and Niobium

[0063] X-ray fluorescence spectroscopy was carried out to determine the content of tungsten and niobium in the composition of the investigated sorbent samples. Analysis was carried out on a laboratory energy-dispersive X-ray fluorescence (EDXRF) spectrometer, model Genius IF, the product of Xenemetrix, Israel. X-Ray Source of 50 kV, 50 W with Rh anode, Silicon Drift Detector (SDD) was used. The Genius IF has a unique patented geometry combining eight secondary targets, with eight customizable tube filters used in direct excitation mode to allow optimal excitation of all elements detected in EDXRF. The WAG (Wide Angle Geometry) secondary target technique provides the best tungsten and niobium analysis results. The X-ray tube excites the characteristic K lines of a secondary target (a pure metal) used to excite the sample—“monochromatically”.

[0064] The determination of the content of niobium was carried out along the line K.sub.a.sub.1.2, the sensitivity of the method was 0.05%. Determination of the tungsten content was carried out along the line K.sub.a.sub.1, the sensitivity of the method was 0.003%. The background in the analysis was considered by linear interpolation and by using a blank sample. Samples of materials for X-ray fluorescence analysis were prepared by compressing them in the form of tablets with NaCl (57653 SIGMA-ALDRICH ≥99.5% (AT)) at a pressure of 4000 kg/cm.sup.2. The instrument was calibrated using samples containing fixed amounts of niobium pentoxide (203920 ALDRICH 99.99% trace metals basis) and tungsten (VI) oxide (204781 powder, ALDRICH 99.995% trace metals basis).

[0065] Sorption-Selective Parameters

[0066] The following characteristics are taken as parameters describing sorption-selective properties: a total exchange capacitance E.sub.Li0, obtained by using 0.1 N LiOH solution as a sorbent; a selective lithium capacitance El.sub.i1 used for sorption from a solution of lithium and sodium salts at an ionic ratio Li.sup.+:Na.sup.+ in the range of 1 to 10 at pH=12; and a coefficient P.sub.Li,Na of selectivity of the sorbent concerning lithium, which is a direct parameter that characterizes separation of lithium from sodium and which is represented by the following formula:

[00001]$P_{\mathrm{Li},\mathrm{Na}}=\frac{E_{\mathrm{Li}1}.Math.C_{\mathrm{Na}}}{E_{\mathrm{Na}1}.Math.C_{\mathrm{Li}}},$ [0067] where [0068] E.sub.Li1 is a selective lithium capacity at sorption from a solution of lithium and sodium salts at ionic ratio Li.sup.+/Na.sup.+ of 1/10 at pH=12 (mg-eqv/g of sorbent); [0069] E.sub.Na1 is a sodium capacity at sorption from a solution of lithium and sodium salts at ionic ratio Li.sup.+/Na.sup.+ of 1/10 at pH=12 (mg-eqv/g of sorbent); [0070] C.sub.Li is a molar concentration of Li.sup.+ in a solution of lithium and sodium salts at ionic ratio Li.sup.+/Na.sup.+ of 1/10 at pH=12 (mol/l); [0071] C.sub.Na—molar concentration of Na.sup.+ in a solution of lithium and sodium salts at ionic ratio Li.sup.+/Na.sup.+ of 1/10, pH=12 (mol/l).

EXAMPLES

Example 1

[0072] A 2-liter of 0.05M K.sub.3NbO.sub.4 solution (pH=12.7) was combined with a given amount of 0.05M K.sub.2WO.sub.4 solution. Then, with vigorous stirring, a 1.0 M HCl solution is poured in until a suspension with pH=5-6 is obtained and precipitated, thus producing a precipitate. The resulting precipitate is washed by successive decantation to a residual potassium concentration of 0.08-0.09 g/I and frozen at −5° C. for 30 hours. After thawing, the granulate is placed in an ion exchange column, and 4.5 l of 0.1 M lithium carbonate solution is passed through. The precipitate is unloaded from the column, dried in the air, heated to a temperature of 400-500° C. (temperature rise rate 10 deg/min), and maintained at this temperature for 3 hours. As a result, a sorbent is obtained in the lithium form, whose main fraction is granules 0.1-0.5 mm in size.

[0073] The effect of synthesis conditions in obtaining an ion exchanger on its sorption properties is summarized in the Table 1. This table presents the results of tests of sorbents obtained at various synthesis conditions but within the scope of the present invention. In the ion-exchange test, a solution of the following composition (g/l) is used: Li.sub.2CO.sub.3-5.5; NaCl: 53.0; NaOH-3.0 (pH=12.1). Desorption of lithium from the sorbent is carried out using a 0.1 M HNO.sub.3 solution.

TABLE-US-00001 TABLE 1 Influence of synthesis conditions on compositions and properties of sorbents (synthesis under conditions within the scope of the present invention) The sorbent Test results obtaining conditions Selective Li—Na The output of W(VI):Nb(V) Treatment Total ion capacity separation the fraction ratio in solution temperature exchange capacity by Li, E.sub.Li1, coefficient, 0.2 ÷ 0.7 mm, during synthesis T, ° C. Sorbent composition* E.sub.Li0, mg-eqv/g mg-eqv/g P.sub.Li, Na mass % 0.019:1 450 H.sub.0.65NbO.sub.2.82•0.05Li.sub.2O•0.02WO.sub.3 2.21 1.87 54.1 97 0.033:1 420 H.sub.0.65NbO.sub.2.82•0.05Li.sub.2O•0.03WO.sub.3 2.35 2.05 68.0 98 0.041:1 470 H.sub.0.65NbO.sub.2.82•0.05Li.sub.2O•0.04WO.sub.3 2.41 2.12 72.2 96 0.055:1 400 H.sub.0.69NbO.sub.2.85•0.03Li.sub.2O•0.05WO.sub.3 2.52 2.26 86.0 98 0.070:1 450 H.sub.0.70NbO.sub.2.85•0.03Li.sub.2O•0.07WO.sub.3 2.56 2.32 96.3 95 0.086:1 460 H.sub.0.67NbO.sub.2.83•0.04Li.sub.2O•0.09WO.sub.3 2.40 2.18 97.6 94 0.106:1 450 H.sub.0.61NbO.sub.2.80•0.07Li.sub.2O•0.10WO.sub.3 2.27 2.04 88.5 98 0.120:1 430 H.sub.0.54NbO.sub.2.77•0.10Li.sub.2O•0.12WO.sub.3 2.00 1.76 74.8 97 0.140:1 460 H.sub.0.50NbO.sub.2.77•0.12Li.sub.2O•0.14WO.sub.3 1.81 1.58 68.0 95 0.200:1 500 H.sub.0.45NbO.sub.2.77•0.14Li.sub.2O•0.20WO.sub.3 1.22 1.03 54.0 94 0.070:1 380 H.sub.0.70NbO.sub.2.85•0.01Li.sub.2O•0.07WO.sub.3 2.51 2.02 41.3 95 0.070:1 550 H.sub.0.70NbO.sub.2.85•0.03Li.sub.2O•0.07WO.sub.3 2.03 1.84 96.3 95 *The composition of the sorbent prepared for sorption of lithium (H-form)

Example 2

[0074] To compare the properties of the sorbents prepared by the method of the invention and conventional methods, weights of sorbents (50 g each) are placed in ion exchange columns with parameters of 3.2 cm.sup.2×30 cm. sorption is conducted from a solution containing (g/l): Li.sub.2SO.sub.4-5.5; NaCl-56.0; NaOH-3.0; pH=12.1.

[0075] Tests of sorbents are carried out in the following sequence. The sorbents are loaded into columns and treated with solutions of HNO.sub.3 at a concentration of 0.2 mol/I. The columns are then washed with water until the media's reaction becomes neutral, and lithium is sorbed from the solutions of the above compositions (filtration rate: 40-60 ml/h, flowing volume: 1500-1600 ml). After the sorption of lithium, the columns are washed with water (300-400 ml), and ion exchangers are regenerated under the action of 0.1-0.2 mol/l of HNO.sub.3. At the regeneration stage, the filtration rate is maintained at about 100 ml/h, and 800-900 ml of the solution is passed. After completion of regeneration, the columns are washed with water until the media become neutral, and a new lithium sorption cycle is started. In total, during the tests, five sorption/desorption cycles are conducted. The averaged test results are shown in Table 2.

TABLE-US-00002 TABLE 2 Sorbent Test Results with Model Solutions Li—Na Losses Exchange capacity, separation per one Column mg-eqv/g coefficient, working Treated Sorbent E.sub.Li1 E.sub.Na1 P.sub.Li, Na cycle, % Volumes According to 2.35 ± 0.25 ± 96 ± 1.5 91 ± the invention 0.20 0.03 5 8 Conventional 1.42 ± 0.36 ± 38 ± 2.1 51 ± 0.20 0.04 6 7

[0076] As shown in Table 2, the sorbent obtained according to the proposed method has sorption-selective characteristics and chemical stability more than two times higher than the sorbent obtained by the known methods.

Example 3

[0077] In these series of tests, experiments are conducted for testing a synthesized sorbent by sorption from a natural underground brine of high mineralization. To compare the properties of the sorbents prepared by the method of the invention and conventional methods, weights of sorbents (50 g each) are placed in ion exchange columns with parameters of 3.2 cm.sup.2×30 cm.

[0078] The brine has the following composition (g/l): Li.sup.+—0.013; Na.sup.+—76.0; K.sup.+—2.7; Mg.sup.2+—3.8; Ca.sup.2+—19.5; NH.sub.4.sup.+—0.13; Cl.sup.−—154; Br.sup.−—0.7; I.sup.−—0.01; SO.sub.4.sup.2−—0.12; HCO.sub.3.sup.−—0.07; pH=8.7. Prior to desorption, the sorbent is washed with a 0.1M NH.sub.4Cl solution to remove salting-out alkaline earth ions. The desorption is conducted with a solution of 0.1N HNO.sub.3.

[0079] Comparative data on the characteristics of sorbents obtained by the known and proposed methods are presented in Table 3.

TABLE-US-00003 TABLE 3 Sorbent Test Results on Real Natural Brines Li—Na Losses Exchange capacity, separation per one Column mg-eqv/g coefficient, working Treated Sorbent E.sub.Li1 E.sub.Na1 P.sub.Li, Na cycle, % Volumes According to 2.31 ± 0.26 ± (5.4 ± 0.9 4400 ± the invention 0.20 0.03 0.2) .Math. 10.sup.4 200 Conventional 0.87 ± 0.18 ± (0.9 ± 1.3 1800 ± 0.11 0.02 0.1) .Math. 10.sup.4 200

[0080] The invention has been shown and described with reference to specific examples. It is understood that these examples should not be construed as limiting the invention application and that any changes are possible within the limits of the attached claims.