渗透汽化是膜分离技术的一种，在有机溶剂脱水等工业领域应用广泛。工业应用实践表
明，组件投资费用偏高制约着渗透汽化技术的发展。有机管式膜组件结构简单，易于密
封，便于安装、拆卸和更换，成本低廉，它的研究对于提高渗透汽化的经济性具有重要
意义。
论文采用“浸涂烘干法”在管式聚丙烯腈（PAN）超滤基膜内表面制备了聚乙烯醇（PVA
）复合层，研究了制膜工艺及涂膜参数对复合膜性能的影响，选择了合理的制膜工艺，
确定了适宜的涂膜工艺参数，制备得到了性能良好的管式复合膜，并对膜的性能进行了
系统的实验研究，对膜的结构进行了表征。
研究表明，管式膜制备合理的工艺为基膜制备及表面改性、组器、质检、清洗、涂层、
干燥及后处理。合适的涂膜工艺参数为：对于复合材料为17－99（MW78000，98％醇解度
）的膜，采用浓度为6％(wt)的PVA膜液，进行一次涂膜；静置时间为3min，放空时间为
2min；干燥时间为2h，热空气入口温度为55℃，气量为4m3/h；热处理时间为1h，热空气
入口温度为140℃，气量为4m3/h。在此条件下制得的管式复合膜经马来酸交联后用于醇
浓度95％（wt）的乙醇水体系的渗透汽化分离，料液温度为65℃，膜后真空度为300Pa条
件下，膜的分离系数一般在30－80之间，好的为160左右；渗透通量一般在230－360g/(
m2·h)之间。
扫描电子显微镜对复合膜的断面和表面形貌观测结果表明，在基膜表面覆盖了一层厚度
在2－5μm之间的致密复合层，复合层与基膜结合紧密。
复合膜用于乙醇水体系的放大试验表明，膜面积为0.0574m2的管式复合膜，在料液温度
为70℃，膜后真空度为300Pa条件下，将2095g乙醇溶液从95％处理到99.5％用时22h，乙
醇回收率89.3％；对于年处理1000吨95％乙醇溶液的无水乙醇生产装置，预计所需膜面
积为75.4m2。
论文首次制备了PVA/PAN管式复合膜，并为进一步的研究工作提供了有指导意义的结论。

关键词：渗透汽化，管式膜，复合膜，膜制备，浸涂烘干法，膜性能
Abstract
A tubular type membrane was prepared for the dehydration of ehanol and isopr
opanol in pervaporation. A polyvinyl alcohol (PVA) active layer was formed o
n the inner surface of a porous polyacrylonitrile (PAN) support by a dip-coa
ting and atmosphere-drying technique. The effects of membrane preparation te
chnique and conditions on performance were studied. The best preparation pro
cesses and the optimal parameters were selected. A series of experiments wer
e performed to investigate the membrane performances. Scanning electron micr
oscopy (SEM) photographs of the virgin and composite membrane were taken to
characterize the physical changes of membrane cross-section and surface.
The final preparation processes consisted of preparation of substrate and it
s treatment, assembling a module, quality examination, washing, coating, dry
ing and heat treatment. The optimal technological parameters were as follows
: the concentration of PVA solution was 6%(wt), the number of coating was 1,
the time PVA solution stayed in the tubular module 3 minutes, the time PVA
flowed out 2 minutes, the time of drying 120 minutes using an about 55℃ air
at a 4m3/h flux, the time of heat treatment 60 minutes using an about 140℃
air at a 4m3/h flux. The membrane preparated using above method was cross-l
inked with maleic acid. This composite membrane was used to separate water f
rom ethanol solution by pervaporation. Under the conditions that the concent
ration of ethanol solution was 95%(wt), the feed temperature was 65℃ and th
e vacuum pressure was 300Pa, the separation factor of the membrane was about
45-80, the better of which was 150, and the total flux varied from 280 to 3
60g/(m2·h).
It was confirmed by SEM photographs that the active layer with a thickness o
f 2-5 μm coated on the porous support closely.
At 70℃, with. 0.0574m2 membrane area, it spent 22 hours for 2095g 95wt% eth
anol mixture to concentrate to 99.5wt%. 89.3% ethanol was reclaimed. So for
a PV plant which produced 1000t/a of EtOH, 75.4m2 membrane area will be need
ed.
It’s the first time to make the PVA/PAN tubular composite membrane. The mem
brane can be purchased at a low price, from which PV will benefit.
Key words: pervaporation, tubular membrane, composite membrane, preparation,
dip-coating and atmosphere-drying, membrane performance
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