アニオン交換体を用いる醗酵液よりイタコン酸の濃縮精製プロセス : 醗酵生産物の分離に関する研究 (第4報)

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One process for recovering itaconic acid from dilute fermented liquor by a reversible ion exchange process using anion and cation exchange resins has been reported (J. Ferment. Technol. 46,158). However, this process has not been adopted by the general chemical industry because the countercurrent operation is barely feasible both mechanically and economically.The following ion exchange processes, operable at atmospheric pressue, were investigated : Amberlite IRA 93-itaconic acid (H_2IA)-NH_3-H_2 (process I), Amberlite IRA 93-H_2IA-H_2SO_4-NH_3-H_2O (II) and Amberlite LA 2-kerosin-H_2IA-K_2CO_3-H_2O (III).Processes (I) and (III) were eliminated based on comparison of criteria such as (a) recovery yield of the desired product, and (b) elimination of undesirable by-products. Process (II) is more clearly shown as follows. [chemical formula]Reversible ion exchange capacities of the acid in the itaconate and sulfate cycles amounted to 1.4 meq/ml resubs, abd 41 to 44 percent of the acid adsorbed onto resins was obtained as crystals only by cooling the effluents eluted with 20g/dl H_2SO_4.That of sulfuric acid in the ammonium cycle was also 1.4 meq/ml resins, and the peak concentration of (NH_4)_2SO_4 in the effluent amounted to 14g/dl on elution with 14g/dl NH_4OH.This process was compared with conventional evaporation process. The estimated plant construction cost of this recovery process is about two thirds that of the conventional plant and the production cost estimate shows comparable savings provided the by product of (NH_4)_2SO_4 can be sold.
社団法人日本生物工学会の論文
1975-03-25

アニオン交換体を用いる醗酵液よりイタコン酸の濃縮精製プロセス : 醗酵生産物の分離に関する研究 (第4報)

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