Method of extracting rhenium from molybdenum-containing solutions

FIELD: chemistry.

SUBSTANCE: invention can be used in rhenium hydrometallurgy. Rhenium is gathered from the starting solution on a weakly basic anionite on a styrene matrix. The rhenium-saturated anionite is washed with water and then treated with an ammonium salt solution with addition of ammonia solution until achieving pH 6.9 - 7.6. The anionite is then removed from the solution, washed with water once more and rhenium is desorbed with ammonia solution followed by extraction of rhenium in form of ammonium perrhenate, which is the end product.

EFFECT: invention increases the degree of purifying rhenium from molybdenum on non-porous and macroporous anionites.

2 tbl

 

The invention relates to hydrometallurgy rhenium, in particular to methods of extraction of rhenium from molybdenum-containing solutions, for example from leaching sulfuric acid systems wet dust collection molybdenum production and other technological solutions.

Molybdenum concentrates, of which rhenium is extracted by the way, are the richest source of raw source of rhenium. The content of molybdenum in the ammonium perrhenate - end product hydrometallurgical redistribution of rhenium is highly regulated.

There is a method of extraction of rhenium from solutions containing molybdenum, through the joint extraction of rhenium and molybdenum solution technical mixture of the tertiary amine in the solvent, Stripping rhenium and molybdenum solution of ammonia, selective sorption of rhenium from reextract on granular strong-base anion exchange resin, desorption rhenium solution of chloric acid and released from decorate by deposition in the form of heptasulphide with subsequent processing of heptasulphide rhenium on the ammonium perrhenate. (U.S. Pat. 730/284-1 Sweden, IPC7C01G 47/00. 1975). The disadvantages of this method are its multi-stage and complexity, as well as the use of expensive, chemically aggressive and dangerous reagent - chloric acid.

There is a method of extraction of rhenium from leaching sulfuric acid systems wet n is neulavlivaemy molybdenum production by joint extraction of rhenium and molybdenum solution technical mixture of the tertiary amine in kerosene with the addition oktilovom alcohol, Stripping rhenium and molybdenum aqueous solution of ammonia, the deposition of the main quantities of molybdenum from reextract in the form of molybdate calcium handling them with lime, subsequent deposition of rhenium after the precipitate of calcium molybdate in the form of perrenate potassium and translated perrenate potassium to ammonium perrhenate by using one of the known methods (Reznichenko, VA, Palant A. A. Solov'ev V.I. Complex use of raw materials in the technology of refractory metals. M.: Nauka, 1988. 240 C.). The disadvantages of this method are its multi-stage and intensity, low concentration of rhenium in the reextractors (up to 10-15 g/l), contamination of solutions of organic substances, present in the extractant, thereby resulting in the need for purification of refined and reextractors from organic substances.

There is a method of extraction of rhenium from acidic molybdenum-containing solutions by neutralization to pH~2, sequential extraction at the beginning of the molybdenum solution of di-2-ethylhexylamine acid in kerosene, then rhenium solution of trioctylamine in kerosene with the addition of tributyl phosphate with subsequent reextracting rhenium from the organic phase with a solution of ammonia evaporation of reextract, mixing VAT residue with lime calcinations of lime paste, leaching of rhenium from SPECA water, deposition of the process is and perrenate potassium and translated perrenate potassium to ammonium perrhenate (A.S. 176684 the USSR, MKI C01G 47/00. Publ. 17.11.65. BI No. 23). The disadvantages of this method are its multi-stage and complexity, high energy costs and significant loss of rhenium processing registergui reextractors, the need for cleaning refined from impurities of organic substances included in the composition of the extractant.

There is a method of extraction of rhenium from molybdenum sulfate solutions by sorption of rhenium and molybdenum on selesnevka the anion exchange resin, washing the resin with water, desorption of molybdenum sodium hydroxide solution, washing the anion exchange resin with water, desorption of rhenium 4 M solution of nitric acid, followed by separation of rhenium from decorativ in the form of ammonium perrhenate their deep evaporation from the distillation of nitric acid to achieve a concentration of rhenium in the distillation residues 70-100 g/l, introduction to distillation residues of ammonium nitrate as vicariates and cooling solutions to a temperature of not higher than 10°C (Bibikova VI, Ilchenko V.V., Semenov Z.A. Application of ion-exchange method for retrieving rhenium from molybdenite // Trudy inst. Research Institute for chromatography. Voronezh: Voronezh state University, 1968, No. 2. S-140). The disadvantages of this method are incomplete desorption of rhenium, its complexity and labor intensity, high energy costs in the processing of registergui of decorativ, the rapid decline in capacity of the anion on rhenium in terms tsiklicheskuyu.

Closest to the proposed method to the technical essence and the achieved result is a method of extraction of rhenium from molybdenum-containing solutions by selective sorption on porous selectitem the weakly basic anion exchange resin in styrene matrix, washing saturated rhenium of the anion from the original solution of water and desorption of rhenium aqueous solution of ammonia. From decorate after parki rhenium isolated in the form of ammonium perrhenate, which is purified by repeated recrystallization to obtain commercial ammonium perrhenate (Ion exchangers in nonferrous metallurgy, Ed. Cebelia. M.: metallurgy, 1975. 351 S. (Romanov V.M., Lebedev K.B. Rhenium. S-218)}.

In a further known method (prototype) was further refined and described in the works of some authors (for example, Kolmogorov A.G. and Yurkevich so-CALLED. To the question of the separation of molybdenum and rhenium exchange resin with different porosity // proc. Dokl. III vsesojuz. the owls. chemistry and technology of molybdenum and tungsten. Ordzhonikidze, 1977. S; Ali, Weak, AAC and other Ion-exchange technology of extraction of rhenium in the processing of molybdenum concentrates on azotnokislogo scheme // proc. Dokl. VII vsesojuz. proc. "Application of ion-exchange materials in industry and analytical chemistry. Voronezh, 1991. P80-81), who proposed to apply for extracting rhenium other resins with improved NWO is involved, but while maintaining intact the essence of the method lies in the use of non-porous celecrity weakly basic anion exchange resin.

However, when using the prototype method is not sufficiently complete separation of rhenium from molybdenum stages of sorption-desorption, which causes the need for repeated recrystallization of the selected ammonium perrhenate to reduce the content of molybdenum to the required limits and, therefore, results in a complicated way and increase the probability of loss of rhenium. A known method as well as the lack of flexibility due to the need to use to extract rhenium only non-porous celecrity anion exchange resin, inferior in their kinetic characteristics of the macroporous anion exchange resin, which reduces the productivity of the method.

The objective of the proposed technical solution is to increase the degree of purification of rhenium from molybdenum and giving way to the universality due to the implementation of use to extract rhenium is not only porous, but macroporous anion exchange resin.

This object is achieved in that in the method of extraction of rhenium from solutions containing molybdenum, by sorption of rhenium from the original solution of the weakly basic anion exchange resin in styrene matrix, washing saturated the CSOs rhenium anion-exchange water and desorption of rhenium solution of ammonia, followed by separation of the final product in the form of ammonium perrhenate, according to the invention after washing saturated rhenium anion-exchange water, the anion exchange resin further treated with a solution of ammonium salts with the addition of ammonia solution to achieve a pH of 6.9 and 7.6, is separated from the solution and again washed with water.

During the implementation of the method of the weakly basic anion exchange resin in styrene matrix is saturated with rhenium by contact with an acidic solution containing molybdenum (usually under dynamic conditions by passing the solution through a column filled with anion exchange resin), washed anion exchange resin with water from the original solution then is treated with anion exchange resin with a solution of ammonium salts, for example ammonium sulfate, with gradual addition of ammonia to control pH of the solution to achieve a pH of 6.9 and 7.6, and then separating the resin from the solution, washed with water and carry out desorption of the rhenium solution of ammonia, followed by separation of the final product in the form of ammonium perrhenate.

New and significant unknown to the modern level of science and technology in the proposed technical solution is to offer pre-saturated with rhenium and washed with water weakly basic anion exchange resin in styrene matrix treated with a solution of ammonium salts with the addition of ammonia solution to achieve a pH of 6.9 and 7.6, again rinsed with water, and only then to carry out desorption of the rhenium solution of ammonia. Detecting the woman, when processing rich rhenium of the anion exchange resin with a solution of ammonium salts with the addition of ammonia solution to achieve a pH of 6.9-7.6 and subsequent washing with water almost the entire molybdenum, sorbed with rhenium, washed out of the resin, allowing the subsequent desorption of rhenium significantly reduce the concentration of molybdenum rhenium in decorato, to increase the odds of separation of rhenium and molybdenum in the course of sorption-desorption. This further simplifies the processing of decorativ on the ammonium perrhenate, and also gives the opportunity to use to extract rhenium is not only porous, but macroporous weakly basic anion exchange resin, which makes the method more versatile. When bringing the pH of the solution of ammonium salt in contact with the anion exchange resin, to values below 6,9 decreases the degree of washing of the anion of molybdenum, which leads to the increase of its concentration in registergui decorated and, thereby, to reduce the degree of separation of rhenium and molybdenum, while bringing the pH level is above 7.6 out of anion exchange resin together with molybdenum begin to leach appreciable quantities of rhenium. When the pH of the solutions below 6,9 molybdenum in the phase of the anion is mainly in the form of strongly sorbed polymer ions, for example, Mo8O264-or Mo7O246-and in the range of pH 6,9-7,6 goes into the Monomeric form of molestation MoO 42-weakly held by the anion exchange resin and is easily displaced from the anion exchange resin anion, forming part of ammonium salts. Rhenium over the whole range of acidity of the solution is in the form of perrenate ion ReO4-the selectivity of the anion to which is significantly higher than the molybdate ions. As for the anion exchange resin, the pH values of 6.9 and 7.6 degree of dissociation of the functional groups is quite high, with the increase of pH above 7.6 degree of dissociation of functional groups slaboosnovnym anion exchange resin is reduced, which leads to desorption and perrenate ion. This is true for both non-porous and macroporous anion exchange resin.

Thus, the claimed technical solution is new, involves an inventive step and is industrially applicable because they are based on the use of simple acceptance and use of available reagents.

1. Examples of the method carried out in static conditions

Used porous and weakly basic, macroporous anion exchange resin in styrene matrix Purolite A172 and Purolite A170, respectively (hereinafter referred to as A172 and A170) with the same functional weakly basic amino groups, the synthesis of which was recently developed by the company "Purolite Int. Ltd.". These anion exchange resins exhibit higher selectivity to rhenium in comparison with other currently available com is ironscheme anion.

The prepared solution composition, g/l: Re 0,4; Mo 2,0; H2SO498. Hanging wet anion exchange A172 and A170 at 1.0 g in terms of dry weight of the anion exchange resin was placed in a glass flask and was cited for saturation of rhenium and molybdenum in contact with 100 ml of the composition. A mixture of resins and the solution was mixed on the device for shaking for 12 h, followed by an analysis of the composition of solutions on rhenium and molybdenum. The results showed that in the experimental conditions, averaged capacity non-porous anion exchange resin A172 on rhenium was 39,8, molybdenum 35.2 mg/g of dry resin, macroporous anion exchanger A170 - 39,8 and 180,4 mg/g, respectively. Hanging anion exchange resins were washed from the solution with water and dried on the filter to a friable state. After that, they were the operations described below.

Non-porous anion exchange resin A

Example 1.1 (the Proposed method)

The sample saturated anion exchange resin A placed in a beaker, was added 20 ml of 1 M solution of (NH4)2SO4and started stirring of a mixture of anion exchange resin with a solution using a blade mixer. To the mixture was added dropwise concentrated (25%) ammonia solution. The pH of the solution in contact with the anion exchange resin was measured using a glass (ECL-47-07) and silver chloride (PCI-AM-3) electrodes on ionomer And-120. When achieving the AI pH of the solution, equal 6,90 not changing for 1 h, the stirrer was turned off, the anion exchange resin is separated from the solution by filtration through a paper filter and washed on the filter with 25 ml of distilled water. The solution after filtration and the solution after the washing were combined, their total volume was brought to 100 ml, after which the analysis was performed on the joint solution of rhenium and molybdenum. Then a sample of the resin was transferred into a flask and brought into contact with 50 ml of 8 M ammonia solution. The mixture of the resin and the solution was mixed on the device for shaking for 12 h, after which the analysis was performed on solution of rhenium and molybdenum.

Example 1.2 (the Proposed method)

With the sample saturated anion exchange resin A operations described in example 1.1 except that the pH of the solution is brought to 7.14.

Example 1.3 (the Proposed method)

With the sample saturated anion exchange resin A operations described in example 1.1 except that the pH of the solution is brought to 7.32.

Example 1.4 (the Proposed method)

With the sample saturated anion exchange resin A operations described in example 1.1 except that the pH of the solution is brought to 7.60.

Example 1.5 (a Way similar to that proposed, but the pH is below the stated limits)

With the sample saturated anion exchange resin A operations described in example 1.1 except that the pH dissolve the and brought to 6.75.

Example 1.6 (a Way similar to that proposed, but the pH is higher than the stated limits)

With the sample saturated anion exchange resin A operations described in example 1.1 except that the pH of the solution is brought to 7.74.

Example 1.7 (Proposed method)

With the sample saturated anion exchange resin A operations described in example 1.1 except that the ion exchanger is brought into contact with 20 ml of 1 M solution of NH4NO3a pH of the solution is brought to 7.12.

Example 1.8 (the Proposed method).

With the sample saturated anion exchange resin A operations described in example 1.1 except that the ion exchanger is brought into contact with 20 ml of 1 M solution of NH4NO3a pH of 7.48 brought to.

Example 1.9 (Method chosen for the prototype)

The sample saturated anion exchange resin A placed in a beaker, was added 50 ml of 8 M ammonia solution. The mixture of the resin and the solution was mixed on the device for shaking for 12 h, after which the analysis was performed on solution of rhenium and molybdenum.

Macroporous anion exchange resin A

Example 1.10 (Proposed method)

With the sample saturated anion exchange resin A operations described in example 1.1 except that the anion exchange resin is used A, and the pH of the solution is brought to 6.90, while desorption is 6 M ammonia solution.

Example 1.11 (Proposed method)

With namesco is saturated anion exchange resin A operations, described in example 1.1 except that the anion exchange resin is used A, and the pH of the solution is brought to 7,24, while desorption is 6 M ammonia solution.

Example 1.12 (Proposed method)

With the sample saturated anion exchange resin A operations described in example 1.1 except that the anion exchange resin is used A, and the pH of the solution is brought up to 7.35, and when desorption is 6 M ammonia solution.

Example 1.13 (Proposed method)

With the sample saturated anion exchange resin A operations described in example 1.1 except that the anion exchange resin is used A, and the pH of the solution is brought to 7.60, while desorption is 6 M ammonia solution.

Example 1.14 (Method, similar to that proposed, but the pH is below the stated limits)

With the sample saturated anion exchange resin A operations described in example 1.1 except that the anion exchange resin is used A, and the pH of the solution is brought to 6.73 x, while desorption is 6 M ammonia solution.

Example 1.15 (Method, similar to that proposed, but the pH is higher than the stated limits)

With the sample saturated anion exchange resin A operations described in example 1.1 except that the anion exchange resin is used A, and the pH of the solution is brought to 7.70, while desorption is 6 M ammonia solution.

Example 1.16 (How close to the prototype, except that use is : macroporous anion exchange resin)

The sample saturated anion exchange resin A placed in a beaker, was added 50 ml of 6 M ammonia solution. The mixture of the resin and the solution was mixed on the device for shaking for 12 h, after which the analysis was performed on solution of rhenium and molybdenum.

The results are shown in table 1. (Total separation factor of rhenium and molybdenum were calculated as the ratio of the concentration ratio of rhenium and molybdenum in an ammonia decorate to the concentration ratio of rhenium and molybdenum in the original solution, which was conducted sorption:

From the results in table 1 suggest that the use of the proposed method allows to increase the concentration ratio of rhenium and molybdenum in desorbing and to increase the overall rate of separation of rhenium and molybdenum when extracting rhenium as non-porous and macroporous anion exchange resin. When bringing the pH to values below these limits the efficiency of the separation of rhenium and molybdenum is reduced due to incomplete leaching of molybdenum at an intermediate stage of processing anion exchange resin, bringing the pH to values above these limits increase loss of rhenium due to washing it together with the molybdenum at the stage of intermediate processing of anion exchange resins.

2. Examples of implementation of the method in dynamic conditions

PR is a trained model solution, the corresponding concentration on the core components of leaching sulfuric acid systems wet dust collection molybdenum production, composition, g/l: sulphuric acid 98; molybdenum 4; rhenium of 0.5. Sorption of rhenium in dynamic conditions all experiments were performed with this model solution. The solution was passed through the column with a working volume of 20 ml at a ratio of the height of the layer of ion exchanger to the internal diameter of the column 10 : 1, one of which was filled with non-porous anion exchange resin And 172, the second - macroporous anion exchange resin A with secondary amino groups. Bandwidth solutions ranged 0,75-0,85 beats. about./PM Solutions at the outlet from the column was analyzed for rhenium. After saturation rhenium anion exchange resin were washed with distilled water, were then carried out the operations described below.

Non-porous anion exchange resin A

Example 2.1 (the Method selected for the prototype)

Through rich rhenium and molybdenum) anion exchange resin A at a temperature of 50°C was skipped 8 M ammonia solution. Samples of the solution at the outlet of the column was determined by the concentration of rhenium and molybdenum.

Example 2.2 (the Proposed method)

The same anion exchange resin And 172, which was used in example 2.1, after desorption of rhenium and molybdenum according to example 2.1 was washed with water, after that it was again missed the original solution of the same composition. After on the ysenia rhenium anion exchange resin was washed with distilled water. Rich rhenium and molybdenum) anion exchange resin A was transferred into a glass. The anion exchange resin was added to 100 ml of a 1 M solution of (NH4)2SO4and started stirring of a mixture of anion exchange resin with a solution using a blade mixer. To the mixture was added dropwise concentrated (25%) ammonia solution. The pH of the solution in contact with the anion exchange resin was measured using a glass (ECL-47-07) and silver chloride (PCI-AM-3) electrodes on ionomer And-120. Upon reaching the pH of the solution equal to 7,43, not changing for 1 h, the stirrer was turned off, the anion exchange resin is separated from the solution by filtration through a paper filter and washed on the filter with 100 ml of distilled water. The solution after filtration and the solution after the washing were combined, their total volume was brought to 250 ml, after which the analysis was performed on the joint solution of rhenium and molybdenum. Then the resin was transferred into the column and through it at a temperature of 50°C was skipped 8 M ammonia solution. Samples of the solution at the outlet of the column was determined by the concentration of rhenium and molybdenum.

Macroporous anion exchange resin A

Example 2.3 (How close to the selected for the prototype, except that was used macroporous anion exchange resin)

Through rich rhenium and molybdenum) anion exchange resin A at room temperature was skipped 6 M ammonia solution. In samples of restorana output from the column was determined by the concentration of rhenium and molybdenum.

Example 2.4 (the Proposed method)

The same anion exchange resin A, which was used in example 2.3, after desorption of rhenium and molybdenum was washed with water, after that it was again missed the original solution of the same composition. After saturation rhenium anion exchange resin was washed with distilled water. Rich rhenium and molybdenum) anion exchange resin A was transferred into a glass. The anion exchange resin was added to 100 ml of a 1 M solution of (NH4)2SO4and started stirring of a mixture of anion exchange resin with a solution using a blade mixer. To the mixture was added dropwise concentrated (25%) ammonia solution. The pH of the solution in contact with the anion exchange resin was measured using a glass (ECL-47-07) and silver chloride (PCI-AM-3) electrodes on ionomer And-120. Upon reaching the pH of the solution equal to at 7.55, not changing for 1 h, the stirrer was turned off, the anion exchange resin is separated from the solution by filtration through a paper filter and washed on the filter with 100 ml of distilled water. The solution after filtration and the solution after the washing were combined, their total volume was brought to 250 ml, after which the analysis was performed on the joint solution of rhenium and molybdenum. Then the resin was transferred into the column and through it at a temperature of 50°C was skipped 8 M ammonia solution. Samples of the solution at the outlet of the column was determined concentration Renee molybdenum.

The results are shown in table 2.

From the results in table 2 suggest that the use of the proposed method in 14-16-fold increase in the values of the coefficients of the separation of rhenium and molybdenum in the extraction of rhenium on non-porous weakly basic ion-exchange resin A and its macroporous similar to the anion exchange resin A and 14-16 times to reduce the concentration of molybdenum in deserveth that should simplify the processing registergui of decorativ and makes it possible to use for the extraction of rhenium from solutions containing molybdenum, not only porous, but macroporous anion exchange resin. Loss of rhenium (reversible) do not exceed 1-5% of the total number of adsorbed rhenium. These losses are reversible and can be returned to the process by selective sorption of rhenium on one of the anion exchange resin with subsequent desorption.

Thus, the inventive method of extraction of rhenium from solutions containing molybdenum, allows to increase the degree of purification of rhenium from molybdenum and is versatile, as it allows for the extraction of rhenium is not only porous, but macroporous anion exchange resin.

Table 1
The anion exchange resinSolNote the p (method) Handling a busy anionDesorption of the ammonia solution
pHWashed, mg/g of ion exchangerWashed, mg/g of ion exchanger
ReMoReMo
12345678910
A(NH4)2SO41.1 (proposed)6,900,433,5a 38.51,427,5137,5
1.2 (proposed)7,140,7 33,7of 37.91,329,1145,5
1.3(proposed)to 7.321,334,037,51,134,1170,5
1.4 (proposed)7,601,734,237,11,037,1185,5
1.5 (similar to that proposed, but the pH is below the stated limits)6,750,229,438,8the 5.76,834,0
1.6 (similar to that proposed, but the pH is higher than the stated limits)7,744,134,835,30,844,4222
NH4NO31.7 (before agemy) 7,121,833,037,61,134,2171
NH4NO31.8(offer)of 7.482,133,737,01,037,0185
-1.9 (Prototype)---38,734,81,15,6

Continuation of table 1
12345678910
A(NH4)2SO41.0 (proposed) 6,901,0176,138,64,29,246,0
1.11 (proposed)7,241,7177,4of 37.92,813,567,7
1.12 (proposed)7,352,1178,337,52,018,793,7
1.13 (proposed)7,602,4178,736,81,524,5127
1.14 (similar to that proposed, but the pH is below the stated limits)of 6.730,8168,139,012,23,2116,0
1.15 (near the s to offer, but pH is higher than the stated limits)7,704,6179,035,71,327,5137
-1.16 (in the prototype)---39,2178,50,221,1

Table 2
The anion exchange resinExample (method)Adsorbed rhenium, mg/mlProcessing of saturated anion exchange resin solution (NH4)2SO4Desorption of the ammonia solution
pHWashed, mg/ml anion-exchangeDesorbed (mg/ml anion-exchange
Re MoReMo
A2.1 (prototype)102,188,516,4of 5.443,2
2.2 (proposed)101,37.431,011,1of 87.31,179,4635
A2.3 (in the prototype)73,372,658,51,249,9
2.4 (proposed)71,7at 7.553,453,768,23,618,9152

The method of extraction of rhenium from the of rastvorov, containing molybdenum, by sorption of rhenium from the original solution of the weakly basic anion exchange resin in styrene matrix, washing saturated rhenium anion-exchange water and desorption of rhenium solution of ammonia, followed by separation of the final product in the form of ammonium perrhenate, characterized in that after washing saturated rhenium anion-exchange water anion exchange resin further treated with a solution of ammonium salts with the addition of ammonia solution to achieve a pH of 6.9 and 7.6, is separated from the solution and again washed with water.



 

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9 cl, 3 tbl, 1 ex

FIELD: metallurgy.

SUBSTANCE: procedure consists in acid extraction of compounds of rare earth elements from phospho-gypsum by mixing extract suspension, in separation of insoluble sedimentation of crystal gypsum from extraction solution and in extracting compounds of rare earth elements from extraction solution. Also, acid extraction is performed with solution of mixture of sulphuric and nitric acids at ratio from 3.2 to 1.2 and concentration from 1 to 3 wt % at ratio L:S (liquid : solid) from 4 to 5 during 8-12 min with simultaneous hydro-acoustic effect onto mixed extraction suspension. Rare earth elements are extracted from extraction solution by means of cation-exchanging sorption with infiltration of extraction solution through cation-exchanging filter.

EFFECT: increased degree of extraction of rare earth elements and 2 times reduced time for process at lower concentrations and volumes of acid reagents.

3 cl, 2 tbl, 4 ex

FIELD: metallurgy.

SUBSTANCE: procedure consists in underground leaching nickel with solution of sulphuric acid and in pumping product solution out. Further, acidity of product solution is reduced, and nickel is sorbed on ionite resin with its following desorption. Upon desorption raffinate of nickel sorption is made-up with sulphuric acid and directed to leaching as leaching solution. Also, excessive sulphuric acid is sorbed on separate ionite with following desorption for reduction of product solution acidity. Upon nickel sorption raffinate is made-up with sulphuric acid and with sulphuric acid after operation of its desorption.

EFFECT: simplification of process, increased ecological safety and reduced consumption of sulphuric acid.

1 dwg, 1 tbl

FIELD: metallurgy.

SUBSTANCE: invention relates to method of extracting stibium from sulphate solutions. Proposed method comprises sorption on anionite and desorption of stibium from anionite by desorption solution. Sorption is carried out using Lewatit K 5517 anionite, while desorption is made via feeding desorption solution through stationary anionite layer at the rate of 0.35-0.46 m/h at 45-50°C. Desorption solution represents disulphide alkaline solution with molar ratio S/NaOH=0.5 and/or alkaline solution of sodium sulphide with sodium concentration of at least 26 g/l.

EFFECT: stibium extraction and increased stibium concentration in solution intended for electrolysis.

3 dwg, 3 tbl

FIELD: chemistry.

SUBSTANCE: invention relates to methods for synthesis of concentrated solutions of rhenic acid. The method for electrodialysis synthesis of concentrated solutions of rhenic acid involves using rhenium metal wastes as the anode material.

EFFECT: invention avoids use of expensive platinum materials as the anode and obtaining more concentrated rhenic acid solutions.

1 dwg, 1 tbl, 2 ex

FIELD: chemistry.

SUBSTANCE: rhenium (VII) ions are extracted from aqueous solutions of protonated or neutral form of N',N'-di-2-ethylhexylhydrazide 2-ethylhexanoic acid. When extracting Re(VII) ions from aqueous solutions of the neutral form of N',N'-di-2-ethylhexylhydrazide 2-ethylhexanoic acid a modifier - 2 vol. % 2-ethylhexanol is used.

EFFECT: invention simplifies the process of extracting rhenium ions from acidic aqueous solutions.

5 tbl, 4 ex

FIELD: medicine.

SUBSTANCE: invention refers to medicine and pharmaceutics and concerns applications of hexanuclear rhenium cluster composed of K4[Re6S8(CN)6] based on radioactive isotopes as an antitumour agent in radiotherapy and/or photodynamic therapy.

EFFECT: invention allows lowering general exposure of an organism by precise drug delivery.

1 dwg, 2 ex

FIELD: chemistry.

SUBSTANCE: method for rhenium isolation implies passing rhenium-containg solution through strongly-basic anion-exchange resin and elution of adsorbed rhenium with high-concentration aqueous solution of hydrochloric acid. Anion-exchange resin is treated with an oxidising aqueous solution, where hydrogen peroxide is used as an oxidiser.

EFFECT: increase in ion exchanger service life.

10 cl, 7 ex

FIELD: hydrometallurgy of rare and scattered elements.

SUBSTANCE: invention has for object isolating and concentrating rhenium and separating rhenium and molybdenum when processing various molybdenum-containing industrial products. Method according to invention comprises sorption of rhenium form solutions followed by desorption thereof. The latter operation is accomplished with mixture containing phosphoric acid hexabutylthiamide (1-3 % v/v) and aliphatic C6-C10-alcohol.

EFFECT: increased degree of recovery of rhenium from initial aqueous process solutions.

5 tbl

FIELD: hydrometallurgy; methods of extraction of osmium and rhenium from the washing sulfuric acid.

SUBSTANCE: the invention is pertaining to the field of the hydrometallurgy of osmium and rhenium, in particular, to the methods of utilization of the osmium-and-rhenium-containing sulfuric acid formed in the system of the wet gas purification of the copper and nickel works and may be used for extraction and concentration of osmium and rhenium from the washing sulfuric acid. The method provides for treatment of the washing sulfuric acid solution having the concentration of H2SO equal to 300-700 g/l with sodium or calcium hypochlorite up to provision of the value of the oxidized-reduced potential of 800-1000 mV for oxidization of osmium up to Os(VIII). Then the extraction of osmium and rhenium is sequentially exercised. At that in the beginning they extract osmium and then extract rhenium. The extraction of osmium is conducted using in the capacity of the extractant the diluent based on the saturated hydrocarbons, in particular, kerosene or the diesel fuel, at ratio of О:H = 1:5-25 with transfer of osmium into the extract, and rhenium - into the raffinate. The osmium-containing extract is subjected to the thermal treatment at 40-85°С, aged and filtered with production of the solid-phase osmium concentrate. Rhenium is extracted from the raffinate by the extractant containing 10-40 % of the tertiary amines at the ratio О:H=1:25-100. The technical result of the invention is the increased degree of extraction of osmium from the washing sulfuric acid with production of its individual concentrate at provision of the high degree of extraction of rhenium into the extract.

EFFECT: the invention ensures the increased degree of extraction of osmium from the washing sulfuric acid with production of its individual concentrate at provision of the high degree of extraction of rhenium into the extract.

6 cl, 4 ex

The invention relates to the chemistry of oxoalkoxide metals, promising as a source of compounds for obtaining the oxide and metal materials
The invention relates to methods of isolation and purification of rhenium
The invention relates to the field of recycling waste latinoreview catalysts on Al2O3basis

FIELD: hydrometallurgy; methods of extraction of osmium and rhenium from the washing sulfuric acid.

SUBSTANCE: the invention is pertaining to the field of the hydrometallurgy of osmium and rhenium, in particular, to the methods of utilization of the osmium-and-rhenium-containing sulfuric acid formed in the system of the wet gas purification of the copper and nickel works and may be used for extraction and concentration of osmium and rhenium from the washing sulfuric acid. The method provides for treatment of the washing sulfuric acid solution having the concentration of H2SO equal to 300-700 g/l with sodium or calcium hypochlorite up to provision of the value of the oxidized-reduced potential of 800-1000 mV for oxidization of osmium up to Os(VIII). Then the extraction of osmium and rhenium is sequentially exercised. At that in the beginning they extract osmium and then extract rhenium. The extraction of osmium is conducted using in the capacity of the extractant the diluent based on the saturated hydrocarbons, in particular, kerosene or the diesel fuel, at ratio of О:H = 1:5-25 with transfer of osmium into the extract, and rhenium - into the raffinate. The osmium-containing extract is subjected to the thermal treatment at 40-85°С, aged and filtered with production of the solid-phase osmium concentrate. Rhenium is extracted from the raffinate by the extractant containing 10-40 % of the tertiary amines at the ratio О:H=1:25-100. The technical result of the invention is the increased degree of extraction of osmium from the washing sulfuric acid with production of its individual concentrate at provision of the high degree of extraction of rhenium into the extract.

EFFECT: the invention ensures the increased degree of extraction of osmium from the washing sulfuric acid with production of its individual concentrate at provision of the high degree of extraction of rhenium into the extract.

6 cl, 4 ex

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