SU1053873A1 - Method of sorption cleaning of sulfate solutions of non-ferrous metals from chlorin - Google Patents

Abstract

A method of sorption purification of sulfate colored metal solutions from chlorine, including their passage through a strongly basic anion exchange resin followed by its regeneration with a solution of sulfur leu slots, so that in order to noBbnueRt the degree of purification of the solutions during the multicyclic anionite, a session, a session, a program, an anitonite, a session, a session, a flow of concentration 200t1500 g / l (L CZ

Description

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The invention relates to hydrometallurgy of non-ferrous metals and can be used in the purification of their sulphate solutions from chlorine ions.

A known method of purification of sulphate solutions of non-ferrous metals from chlorine. By sorption extraction on vinylpyridine anion exchangers and ampholytes, followed by regeneration by soda solutions 1.

The disadvantages of this method are its multi-stage and technological complexity / associated with the need to dispose of soda solutions. . .

The closest to the proposed technical essence and the achieved result is the method of sorption purification of sulphate solutions of non-ferrous metals - from chlorine, which includes passing them through a strongly basic anion exchange resin with its subsequent regeneration with a solution of sulfuric acid. Styrene-divine-benaene anion exchangers are used as a sorbent, and the latter are regenerated with sulfuric acid solution with a concentration of 50–100 g / l 2J.

The disadvantage of this method is that during the multi-cycle operation of the sorbent its capacity gradually drops from 10 -10.5 g / l. chlorine in the first cycle to 5 g / l per even; and, accordingly, the degree of purification of solution from chlorine is twice as low. Therefore, in practice, after 4-5 cycles of operation, the ion exchanger should be replaced with a fresh one.

The purpose of the invention is to increase the degree of purification of sulfate solutions of non-ferrous metals from chlorine during multi-cycle operation of anion exchange resin.

The goal is achieved by the fact that according to the method of dorbcion purification of sulphate solutions of non-ferrous metals from chlorine, including their passage through a strongly basic anion exchanger with its subsequent regeneration with a solution of sulfuric acid, the regeneration is carried out with a solution of sulfuric acid with a concentration of 200 to 1500 g / l.

The method is carried out as follows. ..

Sulfuric acid pactBop is passed through a column filled with a strong basic anion exchanger of the AB-17 type in the OH-form, containing chlorine and macromolecules of non-ferrous metals, mainly zinc, copper, 1-1.5 g / l of chlorine ions to saturation with chlorine. The exchange capacity before passing through the filtrate to the filtrate is, under these conditions, 7 to 10 g / l of sorbent. After saturation, the ion exchanger is washed with water to displace the remainder of the initial solution from the intergrain space and

it is regenerated with a solution of sulfuric acid with a concentration of 200–1500 g / l. When using such solutions, the regeneration proceeds completely in 5-6 column volumes of the eluent, with this exchange capacity of the ion exchanger remains almost unchanged for more than 20 cycles. The selected concentration range is necessary

 sufficient, since when using solutions with a concentration of less than 200 g / l, the capacity of the sorbent drops to 40% by 7-8 cycles, & during the regeneration of anionite with acid

At a concentration of more than 1500 g / l, chlorine is desorbed onto 100%, but the capacity of the anion exchanger drops by 10%. In addition, with an increase in the concentration of sulfuric acid beyond 1500 g / l, the anion exchange resin darkens and its activity decreases.

 After regeneration, the anion exchanger is washed with WATER to pH 5, with a lower pH, the capacity of the anion exchanger for chlorine decreases. The effectiveness of the proposed spbsbba is explained by the fact that in non-ferrous metal sulfate solutions

there are iron ions (III), which are in the range of pH 5-6 (optimal for gluten-free from solutions of chlorine ions) also quite well

0 are adsorbed by a strong base anion exchanger. Carrying out the subsequent regeneration according to the method of the prototype with solutions of sulfuric acid 50-100g / l does not allow complete desorption of iron and, as shown by special studies, by the 7th to 8th cycle iron ions completely block the active groups of the anion exchanger, thereby driving it to worthlessness

Q Example 1. Chlorine is purified from the solution obtained from leaching of the Velmyksi of the Almalyk zinc plant on SB-17 anionite.

The solution contains 140 g / l of zinc, 0.6 g / l of cadmium, 150 mg / l of iron (| Tg), c g / l of copper, b mg / l of cobalt and nickel, 0.6 mg / l of antimony and mouse and 1412 mg / l chlorine ion. In the glass column diameter

 30 mm is placed 100 ml of swollen

AB-17 anion exchanger, the layer height of which is 140 mm, and the initial solution is passed through it with a specific load of 25.

5 until saturation of anion exchange resin with chlorine

 25 - 30 column volumes (KO) solution. After that, the anion exchange resin is washed with 1 K.O. negotiable and 1 K.O. fresh promvody. The first water is added to the initial solution, the second in a turn. Washed anion exchange resin-. Ruut 6 K.O. solution of sulfuric acid with a concentration of 200 g / l and with a specific load of 12. , then

5 anion exchange resin is washed from the acid with water

to pH 5, and the cycle is repeated. A total of 22 cycles were performed. The chlorine-ion anion exchanger in this example averages 7-8 g / l of swollen sorbent with an initial capacity of 10.5 g / l.

P m and m er.2. Under similar conditions, chlorine is sorbed by the anion polymer and regenerated with a solution of sulfuric acid with a concentration of 500 g / l. The degree of regeneration is 100%, and the capacity of the anion exchanger is 8.3 g / l versus the initial 7.2 g / l. In the second cycle, the regeneration of the wire with a solution of sulfuric acid with a concentration of 1000 g / l, desorption of chlorine compresses 100% -, and the capacity after regeneration is 10.3 g / l. In the next cycle, regeneration is carried out. Sulfuric acid (1000 g / l), anioniG active, does not lose.

Chlorine is adsorbed to 100%, and the capacity of the anion exchanger during the subsequent

its chlorine saturation is 9.3 g / l.

Example 3. Conduct sorption, as in example 1, and regeneration is carried out with an acid solution with a concentration of 100 g / l, as in the method of the prototype. The capacity of anion exchange resin drops sharply (from 10.5 g / l in 1 cycle to 5.2 g / l in 4 cycle). I.

Thus, the regeneration of the anion exchanger with sulfuric acid of the proposed concentration increases the efficiency of the anion exchanger and increases its cyclical operation by three times. The technical and economic efficiency of the proposed method is due to the increased degree of purification of the solutions and the reduction in the consumption of anionite for the purification of non-ferrous metal solutions, Hg chlorine and

amounts to 30 - 40 thousand rubles / t sor

.benta.

Claims (1)

METHOD OF SORPTION CLEANING OF SULPHATE NON-FERROUS METALS SOLUTIONS FROM CHLORINE, including their passage through a strongly basic anion exchange resin followed by its regeneration with a solution of sulfuric acid, which is distinguished by the fact that, in order to increase the degree of purification of the solutions during multi-cyclic operation, anion exchange resin is regenerated sulfuric acid with a concentration of 200t1500 g / l