By Hertel K. L.
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14, where the enrichment coefficient q^ versus the coordinate along the column plots are shown for different periods of column operation. 6 cm at a solution flow rate of 434 cm3/hour and a resin flow rate of 135 cnrVhour. A KU-1 sulfophenolic cation exchanger preloaded with an alkaline solution of Cs+ and Rb + mixture was entering the top of the column. The resin was treated with a mixture of Cs + and Rb + salts of the initial composition, acidified with acetic acid. The content of rubidium 48 GORSHKOV, MURAVIEV, AND WARSHAWSKY 400 ~ o 300 'o I o 200 u E £ U 'C 100 C 0) 100 200 coordinate along column, cm FIGURE 14.
The IX purification flowsheet for a component stronger in sorbability than the impurities (continuous reverse frontal separation) is shown in Fig. 9a. The 39 ION-EXCHANGE ULTRA PURIFICATION a MeR MeX separating part x. flow reversal part TT FIGURE 9. Scheme of column (left) and distribution of target component along column (right) for DC purification process by applying auxiliary ions. distribution of components concentration along the column height for this process is shown in Fig. 9b. The purification process scheme with altered direction of the interphase transfer in two-sectional counter-current column is shown in Fig.
2. Purification Methods Based on pH Adjustment Another example of purification processes based on alteration of the interphase mass-transfer direction are methods based on dependencies of both selectivity and IX capacity of polyfunctional ion exchanger on pH . Due to differences in the dissociation constants of functional groups, ion exchange becomes pH dependent, since the selectivity of the resin changes at different pH values. One example is the purification process, shown in Fig. 13, based on bifunctional sulfo-phenolic cation exchanger KU-1.