离子交换树脂电再生实验研究
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摘要
离子交换树脂电再生法是利用电渗析过程中浓差极化现象和双极膜水解离等基本原理，在电场作用下将离子交换树脂再生。本文首先在理论上研究了混床、复床电再生机理，其次分静态和动态两步研究了电再生过程。
通过静态电再生实验，研究了各工艺参数对再生效果的影响。结果表明：再生电压和再生时间是影响再生效果的主要参数；同时，降低淡水室进水含盐量、适当提高进水水温，淡室流速控制在0.1～0.5cm／s，浓室流速控制在0.5～1.0cm／s有利于电再生。本实验装置(三级三段)混床再生电压50V，复床再生电压60V，再生时间60分钟时，显示了良好的再生效果，再生度达到80％以上。
动态实验表明：本实验装置混床再生电压60V，复床再生电压90V，再生时间均为60分钟，再生效果良好，达到了酸碱再生的水平。
在实验基础上，结合相关理论建立了电再生的电流密度、膜对电压和工艺设计计算经验公式，对工业性试验具有极大的指导价值。
研制了一种新型的树脂室隔板，较好地解决了树脂在装置内的流动性；将双极膜水解离技术应用到阴、阳离子交换树脂的单独再生是本研究的最大的创新。
Combined with concentration difference and biopolar membrane water decomposition, ion-exchange resin would be regeneration in eletrodialysis. Firstly, the theory of electroregeneration in mixed bed and multiple bed were analy/cd. Secondly, static and dynamic electroregeneration process were studied.
Suing static experiment, the affects of technological parameters on eletroregeneration were investigated. The results showed: regenerative voltage and time were mostly parameter; at the same time, reducing the salt concentration of influent water and increasing temperature of influent water were benefit to regeneration. Flow rate is also an important factor. Suitable flow rate were between 0.1~0.5 cm/s in the freshwater room and from 0.5 ~ 1.0 cm/s in the concentrate room. Good eletroregenerative effect were obtained, its regenerative degree can beyond 80 percent, when regeneration voltage was 50V in mixed bed and 60V in multiple. Regenerative effect is good and it reaches level of chemical regeneration when regeneration voltage of mixed bed is 60v; voltage of multiple bed is 90v and regenerative time is 60 minutes.
On the base of experiment, The experiential formula of electroregeneration was set up with relational theory. There is a great guiding value to industry experiment.
Resinous fluidity in set was solved with new resinous room. It is a great innovation that biopolar membrane water decomposition is used in separate regeneration of anion-cation exchange resin.
通过静态电再生实验，研究了各工艺参数对再生效果的影响。结果表明：再生电压和再生时间是影响再生效果的主要参数；同时，降低淡水室进水含盐量、适当提高进水水温，淡室流速控制在0.1～0.5cm／s，浓室流速控制在0.5～1.0cm／s有利于电再生。本实验装置(三级三段)混床再生电压50V，复床再生电压60V，再生时间60分钟时，显示了良好的再生效果，再生度达到80％以上。
动态实验表明：本实验装置混床再生电压60V，复床再生电压90V，再生时间均为60分钟，再生效果良好，达到了酸碱再生的水平。
在实验基础上，结合相关理论建立了电再生的电流密度、膜对电压和工艺设计计算经验公式，对工业性试验具有极大的指导价值。
研制了一种新型的树脂室隔板，较好地解决了树脂在装置内的流动性；将双极膜水解离技术应用到阴、阳离子交换树脂的单独再生是本研究的最大的创新。
Combined with concentration difference and biopolar membrane water decomposition, ion-exchange resin would be regeneration in eletrodialysis. Firstly, the theory of electroregeneration in mixed bed and multiple bed were analy/cd. Secondly, static and dynamic electroregeneration process were studied.
Suing static experiment, the affects of technological parameters on eletroregeneration were investigated. The results showed: regenerative voltage and time were mostly parameter; at the same time, reducing the salt concentration of influent water and increasing temperature of influent water were benefit to regeneration. Flow rate is also an important factor. Suitable flow rate were between 0.1~0.5 cm/s in the freshwater room and from 0.5 ~ 1.0 cm/s in the concentrate room. Good eletroregenerative effect were obtained, its regenerative degree can beyond 80 percent, when regeneration voltage was 50V in mixed bed and 60V in multiple. Regenerative effect is good and it reaches level of chemical regeneration when regeneration voltage of mixed bed is 60v; voltage of multiple bed is 90v and regenerative time is 60 minutes.
On the base of experiment, The experiential formula of electroregeneration was set up with relational theory. There is a great guiding value to industry experiment.
Resinous fluidity in set was solved with new resinous room. It is a great innovation that biopolar membrane water decomposition is used in separate regeneration of anion-cation exchange resin.
引文
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[2]王方．当代离子交换技术．北京：化学工业出版社，1993
[3]王方．国际通用离子交换技术手册．北京：科学技术方献出版社，2000
[4]Ganzi G C.Ionpure CDI Electrodeionization Systems:New Product and Process Developments for High-purity Water.Process of the international conference on Ion Exchange ICIE 91.ToKyo:Kodansha ,1991,317—322
[5]黄奕普，陈朝．树脂填充床电渗析制高纯水的脱盐机理．水处理技术，1981(2)：17—21
[6]杨洪渊，用填充床电渗析直接处理废水同时制取纯水，水处理技术，1985(5)：53—57
[7]国营七四二厂，等．填充床电渗析制各高纯水的实验研究．水处理技术，1981(3)：29—34
[8]国营七四二厂，等．高纯电渗析实验概况．北京：中国建筑工业出版社，1975，187—194
[9]徐新，林载祁．填充床电渗析器制备纯水的研究．水处理技术，1996，22(6)：336—341
[10]王方．混床离子交换树脂的电再生法．工业水处理，1997，17(2)：1—3
[11]谭永文，罗菊芬，曲敬绪，等．双极膜法制酸工艺参数的实验研究．水处理技术，1995，21(6)：320—323
[12]廖尚志，莫剑雄．双极膜制酸碱的实验．水处理技术，1998，24(2)：78-81
[13]熊杰明，余立新，林爱光，等．双极膜制酸碱电流效率的测定．水处理技术，1996，22(1)：15—18
[14]Kani K M,Chlanda F P,Byszewski C H.Aquatech Membrane
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[15] Simons, R.Preparation of a High Perforrmance Bipolar Membrane.Journal of Membrance Science, 1993, 78(1-2):13-23
[16] Mafe, S. Electrochemical Characterization of Polymer Ion-exchange Bipolar Membranes, Acta Polymerica 1997,48(7):234—250
[17] Triredi, G.S. Studieson Bipolar Membranes. Reaetive and Funetional Polymers, 1996, 28(3)243—251
[18] 廖尚志，莫剑雄．双极膜的发展与应用．水处理技术，1995，21(6)：311—317
[19] 徐铜文，汪志武．双极膜的理论及应用展望．水处理技术，1998，24(1)：20—24
[20] 钱庭宝．离子交换剂应用技术．天津：天津科学技术出版社，1984
[21] 夏笃纬．离子交换树脂．北京：化学工业出版社，1983
[22] 邵林．水处理用离子交换树脂．北京：水利电力出版社，1989
[23] 姜志新，等．离子交换分离工程，天津：天津大学出版社，1992
[24] 何炳林，黄文强，离子交换与吸附树脂．上海：上海科技教育出版社，1995
[25] 许保玖，给水处理理论，北京：建筑工业出版社，2000：498～576
[26] 王方，国际通用离子交换技术手册．北京：科学技术文献出版社，2000，10—31
[27] 华东建筑设计院．给水排水设计手册第四册，北京：中国建筑工业出版社，1986
[28] 张维润，电渗析工程学，北京：科学出版社，1995
[29] 张根生，等．电渗析水处理技术，北京：科学出版社，1981
[30] 徐梅生．我国电渗析技术发展浅析．膜科学与技
术，1990，2：113—118
[31]马成良．我国电渗析技术发展浅析，膜科学与技术，1998，24(4)：58-60
[32]山内昭．日本电渗析技术研究与开发过程．水处理技术，1995，21(4)：2013—206
[33]华河林，等．电渗析技术的新发展．环境污染治理技术与设备．2001，2(3)：44—47
[34]李福勤，杨云龙，电渗析技术发展方向探讨．科技情报开发与经济，2001，11(4)：56—57
[35]刘苿娥，膜分离技术．北京：化学工业出版社，1998
[36][德]R Rautenbach著，王禾夫 译，膜工艺——组件和装置设计基础．北京：化学工业出版社，1998
[37]给水工程．北京：中国建筑工业出版社，19
[38]沈晓鲤，等．EDI原理及在纯水清洁生产中的应用．环境科学与技术，2000，2：3(3)：41—43
[39]Walter, W. R., D. W. Weiser, and J. L. Marek. Concentration of
Radioactive Aqueous Wastes-Electromigration through Ion-exchange Membranes. Ind. Eng. Chem.1955, 47(1):61—67
[40]Glueckauf, E. Electro-deionization Through a Packed Bed.British Chemicl Engineering, 1959, (6):46-51
[41]UK Patent No. 815154 (June 17, 1959)
[42]US Patent No. 2794777 (June 4, 1957)
[43]US Patent No. 2923674 (Feb 2, 1960)
[44]US Patent No. 3149061 (Sept 15, 1964)
[45]Thomas A. Davis.Electro-regenration of Ion-exchang Resins. PB201734(1971)
[46]Thomas A. Davis.Electro-regenration of Ion-exchang Resins. PB210163(1972)
[47]E.Korngold. Electrodialysis Processes Using Ion Exchang Resins Between Membranes.Desalination, 1975,16:225—233
[48] O. Kedem, Y. Maoz . Ion Conducting Spacer for Improved Electrodialysis . Desalination, 1976, 19:465-470
[49] Thomas A.Davis .Electro-regenerated Ion-exchange Deionization of Drinking Water . PB270910(1977)
[50] Govindan,K.P, Narayanan, P. K. Deminoralization by Electrodialysis Using Ampholytit: Ion-Conducting Spacers. Desalination. 1981, 38:517-527
[51] Demkin, V. I. Tubashov, Y. A . Panteleev, V. I. el al. Cleaning Low Mineral Water by Electrodialysis. Desalination. 1987,64:367-374
[52] Lysenko, L. V, Karplyuk, A. I. Electric Ion Exchange Apparatus for the Preparation of High Purity Water. Vopr. Khim. Teknol. 1981,314-319
[53] Millipore Corporation . Depletion Compartment and Spacer Construction for Electrodeioniation Apparatus. US Patent 4,747,929． 1988-05-31
[54] Millipore Corporation . Depletion Compartment for deionization Apparatus and Methods. US Patent 4,804,451． 1989-02-14
[55] Ionics Incorporated . Introducing and Removing Ion-exchange and other Particulates from an Assembled Electrodeioniation Stack. US Patent 5,066,375． 1991-11-19
[56] Millipore Corporation . Electrodeioniation Apparatus and Methods. EP Application 0379 116A2． 1990-07-25
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