渗透汽化膜的制备及其应用进展

doi:10.16085/j.issn.1000-6613.2021-0972

摘要/Abstract

摘要：

渗透汽化（pervaportion, PV）作为一种新颖的分离技术在工业范围内得以应用，至关重要的是它在恒沸混合物、近沸混合物分离方面的显著优势。相比分馏、精馏、萃取等传统分离方法，渗透汽化技术具有经济、高效、便于管理的优点，但目前缺少优质的渗透汽化膜材料和先进的膜制备方法。本文综述了近年来渗透汽化技术以及渗透汽化膜的研究现状，首先介绍了PV技术的分离机理、PV膜的制备方法、PV技术在工业上的应用领域等，并重点讨论了料液温度、料液浓度、料液流速、膜上下游蒸汽压差、膜材料等关键因素对渗透汽化分离性能的影响。文中提出未来渗透汽化技术应在膜材料方面积极探索，选用聚合物为材料，并结合先进的膜制备方法来进一步降低膜的厚度，从而明显地提高膜渗透通量。

关键词: 渗透汽化膜, 有机物分离, 渗透通量, 分离因子

Abstract:

Pervaportion (PV), as a novel separation technology, has been applied in the industrial scope. The most important thing is its significant advantages in the separation of azeotropic and near-azeotropic mixtures. Compared with traditional separation methods such as fractionation, distillation and extraction, pervaporation technology has the advantages of economy, high efficiency and easy management. However, at present, pervaporation membrane materials with high quality and advanced membrane preparation methods are lacking. Pervaporation technology in recent years are reviewed and the research status of pervaporation membrane, firstly introduces the separation mechanism of PV technology, PV membrane preparation methods, application of PV technology in the industrial field, etc., and focus on the material liquid temperature, slurry concentration, velocity of material liquid, steam pressure difference, upstream and downstream of membrane materials and other key factors affect the performance of pervaporation separation. It is suggested that the future pervaporation technology should actively explore the membrane material, choose polymer as the material, and combine with the advanced membrane preparation method to further reduce the thickness of the membrane so as to significantly increase the membrane permeation flux.

Key words: pervaporation membrane, organic separation, osmotic flux, separation factor

中图分类号:

TQ028.8

马顺选, 宋小三, 王三反, 张轩. 渗透汽化膜的制备及其应用进展[J]. 化工进展, 2021, 40(S2): 256-264.

MA Shunxuan, SONG Xiaosan, WANG Sanfan, ZHANG Xuan. Preparation and application of pervaporization membranes[J]. Chemical Industry and Engineering Progress, 2021, 40(S2): 256-264.

图/表 5

图1 混合体系渗透汽化过程示意图

图2 渗透汽化实验装置示意图1—磁力搅拌器；2—料液罐；3—转子流量计；4—蠕动泵；5—膜组件；6—渗透物收集罐；7—真空泵；8—真空表；9—止水阀

图3 典型的中空纤维纺丝系统图示[15]1, 4—纺丝原液罐；2—压力调节阀；3—压力表；5—纺丝涂料阀；6—内凝固浴罐；7—钻孔液体泵；8—喷丝头；9—空气间隙；10—外凝固浴；11—卷丝鼓；12—纤维收集容器；13—冲洗水

表1 发酵与渗透汽化耦合发酵过程对比[24]

工艺	乙醇浓度峰值/g $?$ L^-1	微生物密度值/g $?$ L^-1	原料转化利用率/%	最终乙醇产量/g $?$ L^-1 $?$ h^-1
纯发酵过程	36	5	86.5	0.251
发酵与PV耦合	11	6	94.3	0.692

表1 发酵与渗透汽化耦合发酵过程对比[24]

工艺	乙醇浓度峰值/g $?$ L^-1	微生物密度值/g $?$ L^-1	原料转化利用率/%	最终乙醇产量/g $?$ L^-1 $?$ h^-1
纯发酵过程	36	5	86.5	0.251
发酵与PV耦合	11	6	94.3	0.692

表2 渗透汽化膜分离有机物/水体系的实验结果

膜材料	分离对象	工艺条件	渗透通量/g $?$ m^-2 $?$ h^-1	分离因子
PEBA/MCM-41^［32］	苯酚	70℃，0.5%（质量分数），1mm Hg 4%（MCM-41填料的质量分数）	157	36
PDMS/PVDF^［33］	乙醇	60℃，25%（体积分数）	281.4	8.23
Hydrophobic titanium dioxide^［34］	甲基叔丁基醚	35℃，1.3%（质量分数）	1180	91
Si0₂-PEBAX/PAN^［35］	吡啶	30℃，5mg·g^-1，5‰（SiO₂填充质量）	76	3.39
β-CD-f-PEBA^［36］	苯酚	50℃，8mg·L^-1，0.5%（β-CD填料质量分数）	63	43.3
PEBA2533^［37］	邻甲酚	80℃，5000mg·L^-1	410	92.7
PDMS/ ZIF-8^［38］	丁醇	60℃，0.96%（质量分数），2%（ZIF-8填料质量分数）	2800	49.2

表2 渗透汽化膜分离有机物/水体系的实验结果

膜材料	分离对象	工艺条件	渗透通量/g $?$ m^-2 $?$ h^-1	分离因子
PEBA/MCM-41^［32］	苯酚	70℃，0.5%（质量分数），1mm Hg 4%（MCM-41填料的质量分数）	157	36
PDMS/PVDF^［33］	乙醇	60℃，25%（体积分数）	281.4	8.23
Hydrophobic titanium dioxide^［34］	甲基叔丁基醚	35℃，1.3%（质量分数）	1180	91
Si0₂-PEBAX/PAN^［35］	吡啶	30℃，5mg·g^-1，5‰（SiO₂填充质量）	76	3.39
β-CD-f-PEBA^［36］	苯酚	50℃，8mg·L^-1，0.5%（β-CD填料质量分数）	63	43.3
PEBA2533^［37］	邻甲酚	80℃，5000mg·L^-1	410	92.7
PDMS/ ZIF-8^［38］	丁醇	60℃，0.96%（质量分数），2%（ZIF-8填料质量分数）	2800	49.2

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