SU1125045A1 - Method of desoption of chlorine from anion exchanger - Google Patents

Abstract

The use of chlorine desorption from sulfuric acid with sulfuric acid, in order to simplify the process by eliminating the stage of processing the filtrate after chlorine desorption and the possibility of its multiple use, desorption is carried out with sulfuric acid at a concentration of 700 900 g / l at 70-90 C.

Description

This invention relates to hydrometallurgy of non-ferrous metals and can be used for the selective extraction of chlorine from sulphate solutions and slurries containing non-ferrous metals as valuable components. The closest to the proposed technical essence and the achieved result is the method of chlorine desorption from the anion exchange resin, which consists in the fact that chlorine desorption from the anion exchange resin is carried out with sulfuric acid solution with a concentration of 10-100 g / l of flJ. The disadvantage of this method is that that the filtrate after desorption of chlorine from an anion exchanger contains chlorine ions, which does not allow its repeated use in the desorption process. The purpose of the invention is to simplify the process by eliminating the stage of processing of the filtrate after desorption of chlorine and the possibility of its repeated use. The goal is achieved by the fact that according to the method desorption is carried out with sulfuric acid with a concentration of 700-900 g / l at. The method is carried out as follows. After sorption of chlorine, the anion exchanger is treated with a solution of sulfuric acid with a concentration of 700–900 g / l at 7090 ° C, and the ratio of ion exchanger-eluate is 1: (3 4). With the indicated parameters chlorine, the transition from the anion exchanger to the eluate is recovered from the sylvate in the form of gaseous hydrogen chloride. Lp accelerating the removal of hydrogen chloride through the pulp of ion exchanger blows air. Yars of hydrochloric acid are drawn by known methods, for example, in water or alkaline absorbers. The eluate, purified from chlorine 452 pa, is again used to regenerate the next portion of the anion exchanger, and the regenerated ion exchanger is directed to the chlorine sorption stage. PRI me R. From anion exchanger AB-27, which is saturated in the process of chlorine sorption from pulp from leaching of Waelce oxides and slags from waste electrolyte (anion exchange resin for chlorine, 5 g / l), chlorine is desorbed under static conditions with a solution of sulfuric acid with concentrations of 600, 700, 800, 900 g / l at different temperatures and the ratio of ion-eluent 1: 3. The process takes 2 hours. In order to speed up the removal, air is blown through the pulp of the ion exchanger from the eluate of HC1 vapor. Data on the degree of desorption and the degree of dechlorination of the eluate. Depending on the content and temperature, c. Thus, it follows from the above data that in order to carry out effective desorption of chlorine and repeated use of the filtrate, the desorption process must be carried out at an acidity of the medium 700–900 g / l and 70–90 s. The lower concentration and temperature conditions are chosen from the condition of a high degree of desorption and purification of the filtrate from chlorine. The upper limit is due to the chemical and thermal stability of anion-bungers. The use of the proposed method of chlorine desorption from anion exchangers, in comparison with the known, almost complete extraction of chlorine from anion exchangers with small volumes of I eluent HC1 vapor;

60

60.4

70 80 90

60 70 80 90

60 70 80 90

Continuation of the table

84.7 89.3 94.8

65.7

. 87.4

91.9

96.3

71.1 92.1 97.4 98.1

Claims (1)

METHOD DESORPTION CHLORINE from the anion exchanger sulfuric acid, of m l and h and w u and d _h I that, in order to simplify the process by eliminating the step filtrate recycling after chlorine desorption and reusability of its use, stripping are sulfuric acid with a concentration of 700 -900 g / l at 70-90 ⁱⁿ C. 1 1125045