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采用支撑液膜技术建立了进料相、膜相、反萃取相三相体系,实现了对洁霉素的分离提纯。该体系采用了洁霉素+异构烷烃(Isopar L)+HCl的反应体系,验证了进料浓度(Cbf)、进料相溶液pH、反萃取相溶液pH、萃取剂组成等因素对分配系数(D)的影响。同时,优化了膜组件实现萃取实验的操作条件,根据传质过程建立了数学模型。结果显示:当洁霉素Cbf为11.9 mmol/L、Isopar L体积分数(VF)为80%、进料相pH为10.1、反萃取相pH为1.2时,D最大为2.34。确定了膜组件操作条件为:管程流量Vf=520 m L/min,壳程流量Vs=500 m L/min。根据所建的数学模型分析了各部分传质阻力,其中管程传质阻力为6.7×10~5s/m,壳程传质阻力为3.7×10~5s/m,跨膜传质阻力为2.7×10~6s/m,跨膜传质阻力起主要作用。
Adopting the support liquid membrane technology, a three-phase system of feed phase, membrane phase and stripping phase was established, and the separation and purification of lincomycin was achieved. In this system, the reaction system of lincomycin + isopar L + HCl was used to verify the influence of factors such as feed concentration (Cbf), pH of the feed phase solution, pH of the stripping solution phase, extractant composition, (D) of the impact. At the same time, the operating conditions of membrane module for extraction experiment were optimized, and the mathematical model was established according to the mass transfer process. The results showed that when the lincomycin Cbf was 11.9 mmol / L, the volume fraction of Isopar L (VF) was 80%, the pH of the feed phase was 10.1 and the pH of the stripping phase was 1.2, the maximum D was 2.34. The operating conditions of the membrane module were determined as follows: tube flow Vf = 520 m L / min and shell flow Vs = 500 m L / min. According to the mathematical model, the mass transfer resistance of each part was analyzed. The mass transfer resistance of the tube was 6.7 × 10 ~ 5s / m, the shell-side transport resistance was 3.7 × 10 ~ 5s / m and the transmembrane mass transfer resistance was 2.7 × 10 ~ 6s / m, transmembrane mass transfer resistance plays a major role.