气隙式膜蒸馏技术研究现状和应用

doi:10.16085/j.issn.1000-6613.2023-0715

化工进展 ›› 2024, Vol. 43 ›› Issue (4): 1655-1666.DOI: 10.16085/j.issn.1000-6613.2023-0715

• 化工过程与装备 • 上一篇

气隙式膜蒸馏技术研究现状和应用

杜永亮¹^,²(), 梁卓彬¹^,², 龚耀煦¹^,², 毕豪杰¹^,², 徐志远¹^,², 苑宏英¹^,²^,³()

^1.天津城建大学环境与市政工程学院，天津 300384
^2.天津市水质科学与技术重点实验室，天津 300384
^3.基础设施防护和环境绿色生物科技国际联合研究中心，天津 300384

收稿日期:2023-05-04 修回日期:2023-08-29 出版日期:2024-04-15 发布日期:2024-05-13
通讯作者: 苑宏英
作者简介:杜永亮（1985—），男，博士，讲师，研究方向为污水污泥处理、固废资源化处置。E-mail：du.smile@163.com。
基金资助:
国家重点研发计划“政府间国际创新合作”专项项目(2019YFE0122400);国家级大学生创新创业训练计划(202210792008)

Air gap membrane distillation research status and applications

DU Yongliang¹^,²(), LIANG Zhuobin¹^,², GONG Yaoxu¹^,², BI Haojie¹^,², XU Zhiyuan¹^,², YUAN Hongying¹^,²^,³()

^1.School of Environmental and Municipal Engineering, Tianjin Chengjian University, Tianjin 300384, China
^2.Tianjin Key Laboratory of Aquatic Science and Technology, Tianjin 300384, China
^3.International Joint Research Center for Infrastructure Protection and Environmental Green Biotechnology, Tianjin 300384, China

Received:2023-05-04 Revised:2023-08-29 Online:2024-04-15 Published:2024-05-13
Contact: YUAN Hongying

摘要/Abstract

摘要：

在低碳经济的发展背景下，膜蒸馏技术作为一种兼具优异分离性能和节能潜力的新型分离技术而备受重视。气隙式膜蒸馏作为一种高热效率的膜蒸馏形式，其节能优势更为显著。本文总结了国内外与气隙式膜蒸馏技术相关的研究进展，从传质传热模型、数值模拟和膜组件结构几个方面指出了膜蒸馏技术的主要研究方向。重点介绍了膜蒸馏过程优化的研究和技术应用现状。膜蒸馏过程优化包括通过膜组件结构设计优化、使用改性膜、外加物理场等方式以提高膜通量或减小膜污染。在应用方面，气隙式膜蒸馏技术主要应用于海水淡化、高浓度工业废水处理和浓缩加工等领域。

关键词: 气隙式膜蒸馏, 膜组件, 膜分离, 数值模拟, 结构优化, 废水处理

Abstract:

As a new separation technology with excellent separation performance and energy saving potential, membrane distillation has attracted much attention under the background of the low-carbon economy. As a form of the membrane distillation with high thermal efficiency, air gap membrane distillation has more significant energy saving advantages. This paper summarized the domestic and international research progress related to air-gap membrane distillation, and the main research directions of membrane distillation technology were pointed out from the mass and heat transfer model, numerical simulation and membrane module structure. The current status of research and technology application for membrane distillation process optimization was highlighted. Membrane distillation process optimization included improving membrane flux or reducing membrane contamination through membrane module structural design optimization, the use of modified membranes, and the application of physical fields. In terms of technology application, air-gap membrane distillation technology could be applied mainly in the fields of seawater desalination, high concentration industrial wastewater treatment and concentration processing.

Key words: air gap membrane distillation, membrane module, membrane separation, numerical simulation, structural optimization, wastewater treatment

中图分类号:

TQ028.8

杜永亮, 梁卓彬, 龚耀煦, 毕豪杰, 徐志远, 苑宏英. 气隙式膜蒸馏技术研究现状和应用[J]. 化工进展, 2024, 43(4): 1655-1666.

DU Yongliang, LIANG Zhuobin, GONG Yaoxu, BI Haojie, XU Zhiyuan, YUAN Hongying. Air gap membrane distillation research status and applications[J]. Chemical Industry and Engineering Progress, 2024, 43(4): 1655-1666.

图/表 12

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基膜	强化形式	优化结果	参考文献
PSF（聚砜）膜	将吐温80或磺化聚砜（SPSF）加入聚砜-聚乙二醇400-二甲基乙酰胺体系中用浸入沉淀相转化法制备PS中空纤维膜	SPSF对膜的亲水性改善比吐温80好；SPSF质量分数为1.5%时可将膜通量提升一倍以上，可达302L/(m²·h)	[20]
PP膜	用共沉积法让亲水性聚多巴胺/聚乙烯亚胺在PP中空纤维膜管腔内沉积制成Janus膜	使用2g/L的聚多巴胺/聚乙烯亚胺共沉积液在60℃下沉积6h约提升85%，70℃下沉积6h约提升100%，80℃下沉积6h可使得通量提升120%，且具有良好的耐盐和抗污染性	[21]
PVDF膜	通过多巴胺的自附着行为对PTFE中空纤维膜进行表面改性	用2g/L的多巴胺对PTFE中空纤维膜进行表面改性8h后得到的膜丝的纯水通量为原膜的1.5倍	[22]
PVDF膜	用热致相分离法制备PVDF/SMA共混中空纤维膜	PVDF/SMA共混膜的膜通量由19.23L/(m²·h)提升到了62.39L/(m²·h)，水接触角由93.4°降低到66.9°	[23]
PVDF膜	双喷头对喷的静电纺织制备PVDF-PH-PET交织型的多级纤维复合膜（tHFC）	在温差为40℃、PET/PH为0.8/1.5、膜厚为80μm的条件下，膜通量可达65.86L/(m²·h)	[24]
PVDF膜	蚀刻-电喷雾协同技术使用Al₂O₃纳米颗粒对PVDF膜改性制成有微/纳凹结构的亲/疏水Janus膜	相较PVDF膜和双疏膜处理高盐含油废水时30min就被污染，Janus膜可连续稳定运行45h仍未被污染	[19]

基膜	强化形式	优化结果	参考文献
PSF（聚砜）膜	将吐温80或磺化聚砜（SPSF）加入聚砜-聚乙二醇400-二甲基乙酰胺体系中用浸入沉淀相转化法制备PS中空纤维膜	SPSF对膜的亲水性改善比吐温80好；SPSF质量分数为1.5%时可将膜通量提升一倍以上，可达302L/(m²·h)	[20]
PP膜	用共沉积法让亲水性聚多巴胺/聚乙烯亚胺在PP中空纤维膜管腔内沉积制成Janus膜	使用2g/L的聚多巴胺/聚乙烯亚胺共沉积液在60℃下沉积6h约提升85%，70℃下沉积6h约提升100%，80℃下沉积6h可使得通量提升120%，且具有良好的耐盐和抗污染性	[21]
PVDF膜	通过多巴胺的自附着行为对PTFE中空纤维膜进行表面改性	用2g/L的多巴胺对PTFE中空纤维膜进行表面改性8h后得到的膜丝的纯水通量为原膜的1.5倍	[22]
PVDF膜	用热致相分离法制备PVDF/SMA共混中空纤维膜	PVDF/SMA共混膜的膜通量由19.23L/(m²·h)提升到了62.39L/(m²·h)，水接触角由93.4°降低到66.9°	[23]
PVDF膜	双喷头对喷的静电纺织制备PVDF-PH-PET交织型的多级纤维复合膜（tHFC）	在温差为40℃、PET/PH为0.8/1.5、膜厚为80μm的条件下，膜通量可达65.86L/(m²·h)	[24]
PVDF膜	蚀刻-电喷雾协同技术使用Al₂O₃纳米颗粒对PVDF膜改性制成有微/纳凹结构的亲/疏水Janus膜	相较PVDF膜和双疏膜处理高盐含油废水时30min就被污染，Janus膜可连续稳定运行45h仍未被污染	[19]

膜蒸馏形式	强化形式	结果	参考文献
DCMD	基于三周期极小曲面（TPMS）的具有横向交联结构（tCLP）的聚丙烯垫片	以1900mg/L的硫酸钙为料液，温差为30℃条件下，效果较好的tCLP垫片能使得通量增加50%，但会增加压降	[27]
DCMD	基于TPMS的tCLP和Gyroid垫片	tCLP和Gyroid垫片都可以显著提升MD的性能，但都不可避免地使压降变大；Gyroid垫片具有更好的缓解有机污染性能，但tCLP对通量的提升效果更显著	[28]
DCMD	无纺布网隔板	在较高的流速下，填充的无纺布隔板使通量增加7%~19%。增加垫片对进料通道的通量增强可达21%~33%。在更高的温度下，垫片对温度极化的改善更明显	[29]
DCMD	六种有不同流动攻角和格栅夹角三维扰流层	曲线型攻角为45°和夹角为90°的扰流层强化效果最好，能使膜通量提升73.99%	[30]
AGMD	螺旋式和波浪式中空纤维膜	50℃时可分别提升7%和4%的通量；75℃时可分别提升40%和36%的通量	[31]

膜蒸馏形式	强化形式	结果	参考文献
DCMD	基于三周期极小曲面（TPMS）的具有横向交联结构（tCLP）的聚丙烯垫片	以1900mg/L的硫酸钙为料液，温差为30℃条件下，效果较好的tCLP垫片能使得通量增加50%，但会增加压降	[27]
DCMD	基于TPMS的tCLP和Gyroid垫片	tCLP和Gyroid垫片都可以显著提升MD的性能，但都不可避免地使压降变大；Gyroid垫片具有更好的缓解有机污染性能，但tCLP对通量的提升效果更显著	[28]
DCMD	无纺布网隔板	在较高的流速下，填充的无纺布隔板使通量增加7%~19%。增加垫片对进料通道的通量增强可达21%~33%。在更高的温度下，垫片对温度极化的改善更明显	[29]
DCMD	六种有不同流动攻角和格栅夹角三维扰流层	曲线型攻角为45°和夹角为90°的扰流层强化效果最好，能使膜通量提升73.99%	[30]
AGMD	螺旋式和波浪式中空纤维膜	50℃时可分别提升7%和4%的通量；75℃时可分别提升40%和36%的通量	[31]

工艺	能量回收形式	参数	膜通量/L·m^-2·h^-1	造水比	其他	参考文献
三级并联和三级串联AGMD	内部回收	热料液温度90℃，原料液温度20℃，气隙厚度4.0mm	并联时为单级的3倍；串联时为单级的2.6倍	—	并联的能量利用率为0.6，串联为0.45	[38]
能量回收AGMD组件	内部回收	热料液温度90℃，原料液温度40℃，气隙厚度0.5mm，中空纤维膜/换热管为2/1	3.1	4.3	热效率80%以上	[39]
用于海水深度浓缩的多效膜蒸馏	内部回收	热料液温度95℃，原料液温度30℃，进料流量40L/h，料液浓度34g/L	3.61~6.07	4.96~13.2	截留率99.9%	[40]
多效膜蒸馏用于氢氧化钠溶液浓缩	内部回收	热料液温度95℃，原料液温度30℃，进料流量30L/h，料液浓度200g/L	3.05	5.04	截留率99.9%	[41]
耦合热泵型三级减压多效膜蒸馏	外部回收	热料液温度70℃，原料液温度30℃，料液流量104L/h，冷却水流量54L/h，热泵COP为3.11	2.26	3.65	—	[42]

气隙式膜蒸馏技术研究现状和应用

Air gap membrane distillation research status and applications

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案例	参数	膜通量/L·m^-2·h^-1	造水比	脱盐率/%	参考文献
太阳能AGMD海水淡化系统	料液、冷却液流速：15~20L/min 料液温度：40~85℃ 冷凝液温度：20~80℃	最高6.5	0.28~0.79	>99	[37]
螺旋缠绕式气隙膜蒸馏组件（SW-AGMD-HF）用于海水淡化	料液温度：70~90℃ 冷却液温度：25~45℃ 料液流量：20~50L/h	5.87	5.37	>99	[52]
太阳能中空纤维AGMD海水淡化装置	料液温度：50~80℃ 冷却液温度：25℃ 料液流量：50L/h 太阳能集热面积：2.38m² 膜面积：0.6m²	晴天最大5.1 多云最大2.4	1.1~3.2	>99	[53]
有隔网的螺旋缠绕式中空纤维膜蒸馏组件用于海水淡化	料液温度：30~80℃ 冷却液温度：25℃	最高6.1	5.8	>99	[54]
内部换热式多效气隙式膜蒸馏组件用于海水淡化	料液温度：90℃ 冷却温度：30℃ NaCl质量分数：3%	最大6.8	6.2~12.5	>99	[55]

案例	参数	膜通量/L·m^-2·h^-1	处理效果	参考文献
AGMD处理含酸浓缩废水	料液温度：40~65℃ 冷却温度：21℃	2.5以上	总体截留率：99.68% 水回收率：75%	[56]
AGMD处理含铀废水	料液温度：50~70℃ 冷却温度：20℃±1℃	3.0~9.0	铀截留率：99% 氟截留率：98%	[57]
AGMD处理电厂脱硫废水	进料温度：60~78℃ 进料流速：30L/h	1.64~4.22	盐截留率：99.8%~100%	[58]
AGMD模拟处理印染废水	料液温度：70℃ 冷却温度：20℃	11.7~12.6	日落黄、玫瑰红染料以及十二烷基硫酸钠表面活性剂的去除率达100%且可将颜色完全去除	[59]
AGMD处理模拟含放射性废水（Cs⁺、Sr²⁺、Co²⁺、UO₂²⁺）	料液温度：60~90℃ 料液流速：80~180L/h 气隙厚度：3~15mm	4.79~16.24	各种操作条件下的Cs⁺、Sr²⁺、Co²⁺、UO₂²⁺去除率均能达到99%以上。在72h浓缩实验中，膜通量呈先升后降低趋势，但是对各种离子的去除率都稳定在99.99%	[60]
多效膜蒸馏处理预处理后的炼油废水浓水	外部热源为97℃热水进料流量：40L/h 进料温度：25℃	4.5~6.5	淡水回收率达95%，出水电导率仅有5.9~7.2μS/cm且COD_Cr小于45mg/L，造水比为6.8~10.2	[61]
多效膜蒸馏处理电镀反渗透浓水	料液温度：65~85℃ 料液流速：15~55L/h 冷却液温度：25~45℃ 冷却液流速：25~45L/h	最高5.136	产水电导率<50μS/cm，浊度<15mg/L，色度<2NTU，脱盐率>99%，出水能达到国家污水综合排放二级标准	[62]

案例	参数	膜通量和造水比	处理效果	参考文献
多效膜蒸馏装置浓缩硫酸盐、盐酸盐等16种无机盐水溶液	料液温度：90℃ 冷凝液温度：30℃ 冷凝液流速：30L/h 料液浓度：0.5%~40%	膜通量和造水比最高达 4.5L/(m²·h)和11.0，但均随着处理时间的升高而下降	实验全程截留率在99.99%以上，电导率保持在200μS/cm以下，当料液浓度达到18%时16种溶液的膜通量和造水比都可保持在2.30L/(m²·h)和6.9以上	[64]
多效膜蒸馏处理预处理后的炼油废水浓水	外部热源为97℃热水进料流量：40L/h 进料温度：25℃	膜通量：4.5~6.5L/(m²·h) 造水比：6.8~10.2	可将废水浓缩19倍以上	[61]
AGMD浓缩西瓜汁、梨汁、苹果汁和柚子汁	进料温度：70℃	膜通量：3L/(m²·h) 造水比：8.0	可将果汁从8°Brix浓缩到55°Brix且果汁风味成分保存良好	[65]
AGMD浓缩氢氧化钠溶液	进料温度：70~95℃ 冷却液温度：20~45℃ 料液流量：6~26L/h	膜通量：3.9~7.7L/(m²·h) 造水比：1.7~2.7	可将NaOH溶液浓缩9.5倍，截留率可达99.9%，但在浓缩过程中膜通量和造水比会逐渐下降	[66]
多效膜蒸馏浓缩中药提取液	热料液温度：70℃ 冷料液温度：30℃ 料液流量：30L/h	膜通量：3L/(m²·h) 造水比：7.0	长期操作稳定性良好，可将各种重要提取液浓缩16倍以上，膜通量和造水比仍可达到1.6L/(m²·h)和5~5.55，且有效成分保留完整	[67]

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