高温多效膜蒸馏用于处理高盐溶液的实验研究

膜蒸馏通常在温度低于90℃的条件下操作,而对于高盐溶液,由于浓差极化和饱和蒸气压下降比较明显,在通常操作温度下膜通量和热利用率都很低。采用具有内部潜热回收功能的多效膜蒸馏组件在高温操作条件下对以氯化钠为代表的无机盐浓溶液的深度浓缩进行了研究,着重考察了冷进料温度T1,加热后料液温度T3、浓度、流量等操作参数对膜通量、造水比和截留率的影响。结果表明,当料液质量分数为5%,热料液温度T3为100℃时,膜通量和造水比的值分别为3.1 L/(m2·h)和15.2;虽然膜通量和造水比均随料液浓度增大而下降,但是当料液质量浓度为25%,T3为105℃时,膜通量和造水比值仍可达1.53 L/(m2·h)和5.8;且截留率达到99.95%以上。在60 d的连续运行中,膜组件保持了良好的性能稳定性。结果表明高温多效膜蒸馏技术能够有效用于高盐溶液的深度浓缩。     

利用多效膜蒸馏技术浓缩硫酸和磷酸水溶液

利用自制中空纤维气隙式多效膜蒸馏组件进行了多效膜蒸馏过程浓缩稀硫酸和磷酸溶液的研究, 考察了膜入口温度、料液进口浓度和料液流量对渗透通量和造水比的影响。结果表明,膜入口温度升高时渗透通量和造水比增加;料液流量增加,渗透通量增加,而造水比随之降低;料液酸浓度增加,渗透通量和造水比均随之下降,且硫酸的影响更为显著。实验过程中渗透通量和造水比最高可达5.3 L/(m²·h)和11.5。在适当的操作条件下,该过程可将质量分数(下同)为2%的稀硫酸或稀磷酸溶液浓缩至40%以上,且渗透液最大的电导率仍小于200 μS/cm。以10%的硫酸溶液为料液,利用2个不同的膜组件进行了持续30 d的多效膜蒸馏过程稳定性实验研究,实验期间所用膜组件操作性能没有明显下降,没有观察到膜渗漏现象。     

多效膜蒸馏技术用于氢氧化钠稀溶液的浓缩

研究了多效膜蒸馏(MEMD)过程对氢氧化钠稀溶液的浓缩回收。结果表明,该过程可将Na OH稀溶液浓缩至250 g/L以上,且截留率维持在99.9%以上;虽然Na OH溶液的黏度和沸点随着浓度上升而急剧上升使得膜通量和造水比都显著下降,但是当Na OH质量浓度达到200 g/L时膜通量和造水比仍可达3.05 L/(m2·h)、5.04,达到相当于7效蒸发器的节能效果。膜组件在连续运行的60 d内保持了良好的操作稳定性。     

新型气隙式膜蒸馏组件盐水浓缩的试验研究

利用新型气隙式膜蒸馏组件对氯化钠溶液进行膜蒸馏试验研究。考察了进料温度、流速、浓度对膜通量、造水比和截留率的影响。结果表明,膜通量和造水比随着进料温度T3升高而增大,随着进料浓度的增加而减小;料液流量增加时膜通量增大,造水比降低;试验过程中截留率基本保持不变,稳定在99.8%以上。当料液浓度为3.0%,进料温度T1为30.0℃,T3为95.0℃、流量为7.0 L/h时,膜通量为4.1 L/(m2·h),造水比为7.0,截留率可达99.8%,经过60 d浓缩试验后,膜通量、造水比和截留率均保持稳定。     

基于低温蒸馏-喷雾蒸发集成工艺的海水淡化

考察了利用低温蒸馏-喷雾蒸发集成工艺进行海水深度淡化的可行性,使用喷雾蒸发技术深度浓缩蒸馏淡化过程排出的浓盐水,并将余热用于驱动蒸馏过程。考察了蒸馏柱进液量、浓盐水喷雾量、加热空气温度及流速对淡水产量的影响。结果表明,较高的加热空气温度有利于淡水产量的提高,而为获得较高的淡水产量,加热空气流速、浓盐水喷雾量以及蒸馏柱进液量则应控制在一定的范围之内,即10—15 m3/h,0.4—0.6 kg/h和0.8—1 kg/h。对于该集成装置,蒸馏柱淡水产量、总淡水产量及淡水产量与输入淡化系统的蒸汽当量之比(造水比)分别可达5 kg/(h.m2),1 kg/h及1.2,回收率可以达到70%以上。     

多效膜蒸馏技术用于果汁浓缩

利用自制的具有高效内部热量回收功能的多效膜蒸馏组件对西瓜汁、梨汁、柚子汁和苹果汁4种果汁进行了浓缩试验,考察了进料温度、浓度和料液流量对膜通量和造水比的影响。浓缩试验中选用温度为75℃的热水作为低品位热源以保障果汁经历的最高温度不超过70℃。在浓缩过程中膜平均通量约为3 L/（m2.h）,造水比约为7.5,相当于九效蒸发器的节能效果。选取苹果汁为料液,利用上述单因素、浓缩试验后的膜组件进行了周期为2个月的多效膜蒸馏浓缩操作稳定性试验,试验期间所用膜组件的操作性能没有明显下降。     

太阳能空气隙膜蒸馏海水淡化的试验

基于自主设计的新型空气隙膜蒸馏组件,建立了一套具有内部热量回收的太阳能空气隙膜蒸馏海水淡化系统,研究了料液流量、中空纤维缠绕角度、太阳辐照量以及天气对太阳能膜蒸馏系统产水性能的影响。结果表明:料液流量的增加在提高膜通量的同时,会牺牲一定的造水比;在一定范围内,中空纤维缠绕角度的减小有利于膜通量和造水比的提高;系统的日产水量随季节变化幅度较大,且晴天的日产水量明显高于阴天;日产水量和日造水比与太阳辐照量的变化趋势一致。当太阳能集热面积为2.38 m~2、膜面积为0.6 m~2、料液流量为50 L/h时,最大膜通量为5.1 kg/(m~2·h),最大日造水比为3.2,最大日产水量为21.7 L/d,产水电导率稳定在20.0μS/cm以下。太阳能膜蒸馏系统运行稳定,性能可靠,在电能和淡水资源短缺的偏远地区具有很好的应用价值。     

阻垢剂对海水淡化膜蒸馏试验的影响

采用直接接触式膜蒸馏技术进行海水淡化试验研究。在海水温度为55℃,循环水温度为20℃的条件下,考察了不同阻垢剂用量对膜蒸馏海水淡化的影响、工艺连续运行过程中膜通量和产水电导率随时间的变化情况,确定了膜蒸馏过程稳定运行的最优浓缩倍率。结果表明,阻垢剂的加入可明显提高淡水的产水率,产水率可达到85%以上,减少了高盐度海水浓缩液的排放,膜通量稳定,产水水质好,其电导率不超过10μS/cm,膜蒸馏海水淡化具有一定的技术可行性和可操作性。     

新型中空纤维空气隙式膜蒸馏用于海水淡化

利用自制的添加隔热管状隔网并呈螺旋缠绕结构编排的中空纤维膜组件进行了空气隙式膜蒸馏(AGMD)海水淡化过程性能研究, 实验以模拟标准海水(质量分数3.5%, 总溶解性固体含量35000 mg·L^-1)为热料液进水, 考察了热料液进水温度、热料液流量、冷凝液进水温度和冷凝液流量对膜通量、造水比和热效率的影响。结果表明, 随着热料液进水温度增加, 膜通量、造水比和热效率均增加;冷凝液进水温度增加, 膜通量下降而造水比和热效率增加;热料液流量增加, 膜通量上升而造水比和热效率明显下降;冷凝液进水流量对膜蒸馏过程性能影响较小。实验过程中产水TDS始终保持在3.0 mg·L^-1以下, 相应的离子去除率高于99.99%, 膜通量、造水比和热效率最高可分别达5.87 L·m^-2·h^-1、5.37和0.943。研究表明, 引入清洁能源取代传统电加热驱动热源将进一步突出膜蒸馏技术的实际应用潜力。     

真空膜蒸馏浓缩反渗透浓盐水的工艺研究

分别采用聚乙烯、聚丙烯微孔膜对反渗透海水淡化浓盐水进行真空膜蒸馏的研究。考察了膜下游真空度、浓盐水温度、浓度、流速对膜通量及截留率的影响。结果表明,真空度增大,膜通量和截留率呈增长趋势。料液温度升高,膜通量增加,截留率呈减少趋势。料液流速增加会使通量增加,截留率呈减少趋势,但影响相对不大。随着料液浓度的增加,膜的通量下降,截留率基本保持不变。本实验条件下最大截留率可达99．99％,表明利用真空膜蒸馏技术可有效实现反渗透海水淡化浓盐水的浓缩。     

Ultrafiltration membrane cleaning technology and mechanism based on seawater desalination pilot equipment

In order to clean the ultrafiltration membrane in the process of seawater desalination, this paper studied the cleaning effects of backwash water and chemical agents on the ultrafiltration membrane by using the ultrafiltration pilot equipment. Effects of different backwash water on the transmembrane pressure difference were studied. The results showed that the cleaning effect was in the order of fresh water (tap water) > ultrafiltration water > reverse osmosis concentrated water. In addition, cleaning effect was as follows: citric acid > oxalate > hydrochloric acid > sodium hypochlorite > sodium hydroxide. Citric acid had the best cleaning effect, and the pure water penetration rate could be restored from 283.24 L/(m²·h) to 571.56 L/(m²·h). Moreover, the effect of alkali washing and acid washing together is better than that of cleaning alone. After cleaning with sodium hydroxide and then citric acid, the pure water transmission rate can recover from 283.24 L/(m²·h) to 818.81 L/(m²·h). The results of this study have a good application prospect for the maintenance of ultrafiltration membrane in seawater desalination.     

基于海水淡化中试的超滤膜清洗工艺及机理

为了对海水淡化过程中的超滤膜进行清洗,利用超滤中试设备研究了反洗水和清洗药剂对超滤膜清洗的效果。分别研究了不同的反洗用水对于跨膜压差的影响,结果表明,清洗效果：淡水（自来水）>超滤产水>反渗透浓水。另选用不同的酸性清洗剂与碱性清洗剂进行清洗,结果表明,清洗效果：柠檬酸>草酸>盐酸>次氯酸钠>氢氧化钠,柠檬酸清洗效果最好,纯水透过速率可从283.24 L/(m²·h)恢复至571.56 L/(m²·h)。此外,实验证明碱洗+酸洗效果优于单独清洗效果,先用氢氧化钠清洗,再用柠檬酸清洗,纯水透过速率可从283.24 L/(m²·h)恢复至818.81 L/(m²·h)。本研究成果对于海水淡化过程中超滤膜的维护具有较好的应用前景。     

Utilization of solar energy for direct contact membrane distillation process: An experimental study for desalination of real seawater

Membrane distillation (MD), a non-isothermal membrane separation process, is based on the phenomenon that pure water in its vapor state can be extracted from aqueous solutions by passing vapor through a hydrophobic microporous membrane when a temperature difference is established across it. We used three commercially available hydrophobic microporous membranes (C02, C07 and C12; based on the pore size 0.2, 0.7 and 1.2 μm respectively) for desalination via direct contact MD (DCMD). The effects of operating parameters on permeation flux were studied. In addition, the desalination of seawater by solar assisted DCMD process was experimentally investigated. First, using solar power only short-term (one day), successful desalination of real seawater was achieved without temperature control under the following conditions: feed inlet temperature 65.0 °C, permeate inlet temperature 25.0 °C, and a flow rate of 2.5 L/min. The developed system also worked well in the long-term (150 days) for seawater desalination using both solar and electric power. Long-term test flux was reduced from 28.48 to only 26.50 L/m²hr, indicating system feasibility.     

Determination of the total iodide content in desalinated seawater permeate

An investigation was conducted to determine the iodide content of permeate collected from several operating facilities reliant upon synthetic membrane processes for seawater desalination. A possible, yet unintentional impact for communities that employ synthetic membrane processes for seawater desalination is the introduction of permeate streams containing iodide into their water supply, that then may result in the formation of iodinated disinfection by-products. To evaluate this potential, the iodide content of desalinated seawater permeate streams were measured using an analytical procedure based on the catalytic reduction of ceric sulfate by arsenious acid in a sulfuric acid solution. It was determined that iodide concentrations in permeate samples collected from seawater desalination facilities were less than the catalytic reduction method detection limit of 4.0 μg/L for membrane feed seawaters that ranged between 51.1 μg/L and 35.8 μg/L of total iodide. Results of this investigation indicated that synthetic membrane processes can remove greater than 89% of the total iodide from the feedwater of seawater based on an iodide detection limit of 4.0 μg/L.