纯水体系下纳滤膜分离过程热力学问题研究

采用NF270和GE DK纳滤膜,在不同压力、温度和pH条件进行纯水过滤试验,以测定不同条件下两种纳滤膜的膜通量,并研究不同条件下的纳滤膜渗透系数变化规律;构建纳滤膜渗透系数与热力学参数之间的关系式,计算两种纳滤膜的热力学参数,分析两种纳滤膜分离过程热力学原理.结果表明:两种纳滤膜的膜通量随着温度和压力的增加而增大,两种纳滤膜的渗透系数随着温度升高而增大,并随着压力和pH的变化呈现小幅波动;GE DK纳滤膜的活化能高于NF 270纳滤膜的活化能,分别为16.56kJ/mol和14.22kJ/mol.由此可知,在分离过程中GE DK纳滤膜比NF 270纳滤膜需更高的运行压力.     

可应用于重金属废水处理的纳滤技术

纳滤膜对单价和多价离子具有选择分离性能。实验研究了纳滤膜的截留性能随测试溶液的浓度、温度、pH值和操作压力等纳滤操作条件的变化规律。考察了纳滤膜对重金属离子的截留情况，实验表明纳滤膜能够截留大部分重金属离子。     

有机纳滤膜的制备技术

纳滤膜是近年来发展较快的重要的液体分离膜品种。综述了有机纳滤膜的制备方法和最近研究进展，并介绍了复合纳滤膜的后处理方法，对纳滤膜今后发展作了展望。     

纳滤膜制备的研究进展

对纳滤膜技术进行了简单介绍,包括纳滤膜的特点、种类、应用领域。综述了国内外纳滤膜制备方法的研究进展,主要有L—s相转化法、共混法、荷电化法、复合法等。其中复合法是用的最多的,比较容易得到高性能的纳滤膜。最后,总结了纳滤膜制备方法中存在的问题并对纳滤膜的应用前景进行了展望。     

纳滤膜技术净化饮用水的应用研究进展

纳滤膜技术是制备优质饮用水的有效方法.综述了纳滤膜技术净化饮用水的研究进展,研究表明,纳滤膜可有效降低饮用水的硬度,去除饮用水中砷、氟等有害物质,并且可以改善饮用水口感.纳滤膜在控制饮用水中微量有机污染物、内分泌干扰物及“三致”物质,提高饮用水的生物稳定性等方面也有很好的效果.针对如何提高纳滤膜净化效果和降低膜污染,探讨了未来纳滤膜技术应重点开展的研究工作.     

纳滤水处理应用研究现状与发展前景

纳滤技术作为一种新型的膜分离技术,近年来得到国内外专家学者的广泛关注和深入研究.结合课题组在纳滤水处理领域的研究进展,综述了纳滤膜技术在工业水处理、饮用水净化、医药废水、垃圾渗滤液处理、淋浴水回用、特种水处理及海水淡化等方面的研究现状,并展望了纳滤膜技术的发展前景.     

有机-无机杂化纳滤膜的制备研究进展

作为一种新型纳滤膜,有机-无机杂化纳滤膜结合了传统有机纳滤膜和无机纳滤膜的优点,具有良好的物化稳定性和优异的分离性能,引起了研究者的广泛关注。介绍了近年来有机-无机杂化纳滤膜的原料、制备方法及产品分离性能,展望了这种新型纳滤膜的应用前景。     

无机纳滤膜的应用

无机纳滤膜具有良好的热稳定性和化学稳定性、机械强度高、易再生、抗微生物侵蚀等优点,已成为膜分离技术中一类引人瞩目的膜材料.文章介绍了无机纳滤膜的结构、组成和分离性能;综述了无机纳滤膜在水处理、食品、制药及化工领域的应用;并展望了无机纳滤膜的研究目标和发展前景.     

MBR与NF联用净化微污染水源水研究

对纳滤膜在不同产水率条件下的净水性能和膜通量衰减过程,以及纳滤膜在产水率90％条件下的运行特性进行了分析.采用MBR作为预处理与纳滤膜联用,考察联用工艺对水中氨氮和有机物的去除效果,以及MBR膜和纳滤膜的污染情况.结果表明,相比于额定工况,纳滤膜在90％产水率条件下运行,对有机物的去除率和脱盐率分别降低4％和3.5％,仍具有优越的净水性能;膜通量衰减速度增加17％.研究同时表明,降低纳滤膜进水中有机物的浓度能够有效缓解纳滤膜的污染过程,使纳滤膜能够在90％产水率条件下保持较高的通量.MBR与纳滤膜联用对氨氮和TOC表现出良好的去除效果,在进水浓度为1.5 mg/L、3.5 mg/L时,出水分别降低到0.4 mg/L、0.2 mg/L.MBR通过去除水中的颗粒物和有机物,有效地缓解了纳滤膜的污染过程,在60天的运行中纳滤膜通量仅下降24.7％,但MBR膜TMP增长较快,试验中共进行了6次膜清洗.     

荷电纳滤膜对化机浆混合废水的纳滤效果

在制备一种荷正电纳滤膜的基础上研究了制备过程影响成膜性能的几个因素，并探讨了该纳滤膜对化机浆混合废水的纳滤效果。研究发现，与一般聚丙烯腈纳滤膜比较，荷正电聚丙烯腈纳滤膜更有利于提高化机浆混合废水色度，CODCr,BOD5的去除率和钠截留率。     

Removal of small trihalomethane precursors from aqueous solution by nanofiltration

The removal of small trihalomethane precursors (THMPs) from aqueous solution by two commercial nanofiltration membranes (NF70 and NF270) was investigated. Resorcinol, phloroglucinol, and 3-hydroxybenzoic acid were selected as model compounds of small THMPs, while tannic acid was chosen as a medium molecular disinfection by-product (DBP) precursor for comparison. The performance of nanofiltration membranes were evaluated by introducing polyethylene glycol (PEG) solutions and uncharged saccharides to estimate molecular weight cut-off (MWCO) and membrane pore radii, respectively. The streaming potential was measured to estimate the membrane surface charge at different pH values, which reveals that the NF270 membrane is more pH-sensitive than the NF70 membrane. The rejections of the above selected THMPs were assessed under various pH values, and the removal efficiencies of THMPs for both membranes at high pH values are reasonably well. Charge exclusion is the prevailing mechanism for the selected small model compounds retended by the negatively charged nanofiltration membranes, while size exclusion and adsorption are controlled mechanisms but not sufficient for the rejection of unionized small organic molecules. In general, the NF270 membrane exhibits the superior permeation rate value, which takes an advantage over the NF70 membrane from the aspect of energy conservation.     

纳滤膜对邻苯二甲酸二（2-乙基己基）酯截留行为的研究

采用聚酰胺复合纳滤膜(BDXN-90)处理地表水中微量邻苯二甲酸二(2-乙基己基)酯(DEHP),研究了有机物、离子强度等因素对其截留行为的影响;探讨了在有机物共存的条件下,纳滤膜截留DEHP的机理.结果表明:BDXN-90纳滤膜能有效截留地表水中微量邻苯二甲酸二(2-乙基己基)酯,其截留率在98%以上,并且长时间运行稳定;膜过滤过程中,刚开始由于DEHP与膜表面之间的吸附截留率较高,当吸附趋于饱和截留率下降,最后随着膜污染的逐渐形成导致膜通量下降和截留率上升;影响截留行为的主要因素是离子强度和有机物:离子强度中和膜表面静电将膜基质压实,有机物与膜表面产生吸附导致膜污染.     

聚甲基丙烯酸N,N-二甲氨基乙酯复合纳滤膜的制备

以AIBN为引发剂,采用本体聚合的方法制备了聚甲基丙烯酸N,N-二甲氨基乙酯(PDMAEMA),并采用中空纤维超滤膜技术滤除PDMAEMA水溶液中的低聚物和未反应的单体.以聚砜(PSf)超滤膜为基膜,以所精制的PDMAEMA为水相涂层液,以对二氯苄的正庚烷溶液为有机交联剂,利用界面聚合的方法制备了PDMAEMA/PSf荷正电复合纳滤膜.实验重点研究了PSf基膜和单体浓度、水相pH值及浸涂时间、水相沥干时间、交联反应时间等条件对所制备纳滤膜分离性能的影响,确定了较优的制膜条件.所制备的荷正电纳滤膜对1g/LMgSO4水溶液(0.8MPa,30℃)的截留率为86.7%,水通量为8.4L/(m2.h).     

高硬度水质下纳滤系统的运行状态及分析

介绍了海岛高硬度水质下纳滤系统的工艺特点 ,通过实测计算膜常数A和B ,分析了离子的选择性分离趋势以及相应操作因素的影响 .此外 ,还就LSI和溶度积的变化规律 ,探讨了其对垢的形成、垢型判断和参数调控的有效性 .     

层层自组装PDADMAC/PSS纳滤膜的制备

以荷负电的聚砜超滤膜为基膜,采用静态层层自组装技术,制备了PDADMAC/PSS多层聚电解质纳滤膜.考察了支撑盐的种类、浓度、自组装层数对膜的分离性能、荷电性能、亲水性等的影响.研究结果表明,以NaCl为支撑电解质制得的膜具有较高的性能,聚合电解质溶液中支撑电解质的浓度以0.5mol/L为宜;在较优的条件下所制备的(PDADMAC/PSS)5对2g/L Na2SO4的截留率可达93%,通量在1.0MPa下接近60L/(m2.h),对NaCl的截留率仅为9%～13%,通量可达80L/(m2.h).膜表面的荷电量和接触角的变化均反映了聚电解质的交替自组装.以PSS为最外层的膜表面具有很好的负电性和很低的接触角.随着双层数的增加,膜表面的负电荷量的绝对值先逐渐增大,达到一个极大值后又逐渐减少,说明层数并非越多越好;以PSS作为最外层的膜具有很好的亲水性.     

纳滤膜难溶盐污染过程的介电监测方法

模拟了难溶盐对纳滤膜的污染过程并对其进行了介电谱解析,探讨了介电谱作为一种监测膜内部或表面污染层信息的方法之可行性.测量了NF90、NF270、NF-3种商用纳滤膜分别被4种难溶盐(CaCO3、CaSO4、BaSO4、SrSO4)污染前后膜/液体系的介电谱,介电谱的差异是来自于因膜孔径的不同而分别在膜孔内和膜表面形成的...     

A membrane-based co-treatment strategy for the recovery of print- and beck-dyeing textile effluents

This paper describes the final part of a study on the recovery of print- and beck-dyeing wastewaters of the carpet manufacturing industry by membrane processes. These wastewaters had been previously treated separately where the print dyeing wastewaters were recovered by chemical precipitation followed by nanofiltration (NF) and beck-dyeing wastewaters were subjected to microfiltration (MF) and pH neutralization prior to NF. In this study, a co-treatment scheme after separate pre-treatment stages was adopted to simplify the overall process. The effect of mixing ratio on membrane fouling was also investigated. The co-treatment strategy was found advantageous since the number of NF units was minimized and the pH neutralization step in separate treatment of beck-dyeing wastewaters was eliminated, providing a reduction of chemical usage.     

The role of pH in nanofiltration of atrazine and dimethoate from aqueous solution

This study examined the performance of nanofiltration membranes to retain atrazine and dimethoate in aqueous solution under different pH conditions. Four nanofiltration membranes, NF90, NF200, NF270 and DK are selected to be examined. The operating pressure, feed pesticide and stirring rate were kept constant at 6x10(5) Pa, 10 mg/L and 1000 rpm. It was found that increasing the solution's pH increased atrazine and dimethoate rejection but reduced the permeate flux performance for NF200, NF270 and DK. However, NF90 showed somewhat consistent performance in both rejection and permeate flux regardless of the solution's pH. NF90 maintained above 90% of atrazine rejection and approximately 80% of dimethoate rejection regardless of the changes in solution's pH. Thus, NF90 is deemed the more suitable nanofiltration membrane for atrazine and dimethoate retention from aqueous solution compared to NF200, NF270 and DK.     

高分子纳滤膜材料研究进展

纳滤膜是介于反渗透膜和超滤膜之间的一种新型分离膜,其截留分子量范围相对较窄（200-1000）且孔径较小,膜材质的选择日益成为制备出高性能纳滤膜的关键。本文综述了国内外高分子纳滤膜材料发展、应用和改良的最新研究进展,并在此基础上展望了纳滤膜材料未来发展趋势。     

Integration of microfiltration and nanofiltration to promote textile effluent reuse

This study investigates the application of a hybrid microfiltration–nanofiltration (MF–NF) process for textile wastewater reclamation. Indigo blue dye was efficiently retained by an MF membrane, allowing its recovery from the concentrated stream. NF technology was successfully applied to polish textile effluent. The NF membrane was evaluated under different transmembrane pressure (8–15 bars), crossflow velocities (0.21–0.84 cm s^?1), pH (7–11), and feed temperature (20–40 °C). The best NF performance was provided at a pressure of 12 bar and a crossflow rate of 0.63 cm s^?1. The NF performance (in terms of COD, conductivity, colour, and nitrogen removal) was not influenced by pH; however, higher feed pH values resulted in increased membrane fouling. The principal cause of flux decline was due to concentration polarization. Membrane chemical cleaning was sufficient to regain the initial permeability. The NF permeate met the quality requirements for all water demands within the textile industry, while the NF concentrate could be used to wash equipment, print work screens, print paste containers, and floors. The total capital cost (CapEx) of the MF–NF system was estimated at 58,362.50 US dollars and the total operational cost (OpEx) at 0.31 US dollars per cubic metre of effluent.