膜技术分离纯化绿原酸提取液的研究

本实验研究了膜技术分离纯化绿原酸提取液的过程。首先,以透水通量为指标,比较了两种微滤膜MF1和MF2、两种超滤膜UF1和UF2及两种纳滤膜NF1和NF2对绿原酸提取液的过滤特性。结果表明,MF2膜的通量可高达167.7kg/h,UF2膜的通量可达148.8kg/h和NF2膜的通量可达109.8kg/h,分别明显高于MF1(103.6kg/h)、UF1(48.0kg/h)和NF1(45.6kg/h);其次,研究了浓缩液的水洗对绿原酸截留率的影响。结果表明,经一次水洗后,MF2膜的截留率可由12.5%降低到3.4%,UF2膜的截留率可由15%降低到8%;最后,分析了膜分离过程中各物料的成分。结果表明,纳滤浓缩液含绿原酸为17964mg/L,比原提取液提高了24.8倍,绿原酸的纯度由2.8%上升到27%。     

膜集成工艺浓缩灵芝水提液的研究

高效节能的膜集成技术已开始应用于食品和药用植物中有效成分的分离提取。文中针对灵芝提取液的特性,依据微孔过滤(MF)、超滤(UF)、纳滤(NF)各种膜对特定物质的选择分离性能,设计了新型膜集成工艺,即筛网和滤纸粗过滤除杂和MF净化处理,进而用不同切割分子质量(MWCO)膜进行两级UF、最后用NF净化浓缩灵芝水提液的创新技术。在操作压力≤0.20 MPa和15 m/s的高膜面流速,1.0 mL/(cm~2·h)恒通量模式下,灵芝水提液先后经MWCO分别为5万的聚丙烯腈(PAN)膜和1万的醋酸纤维素(CA)膜进行UF批次处理。UF渗透液再经截留分子质量为1 50～300的DK(标准)型聚酰胺(PA)膜进行纳滤浓缩,浓缩倍数达6倍时,渗透通量在0.92～0.33 mL/(cm~2·h),纳滤渗透液的色度在浓缩过程稳定在70～80,有效成分截留率高。     

国内超滤(微滤)膜市场分析及预测

超滤和微滤（UF／MF）是重要的膜过程，在我国仅次于反渗透（RO）；而在国际上，却是最重要的膜过程。     

小孔径陶瓷膜澄清甜叶菊提取液的工艺研究

该文研究了小孔径陶瓷膜澄清甜叶菊提取液的效果。通过比较4、5、8、10 nm孔径的陶瓷膜过滤甜叶菊的甜菊糖提取液时的过滤通量、脱色率和收率的区别,确定较优的陶瓷膜孔径;再优化陶瓷膜操作参数。结果表明,5 nm陶瓷膜较优,在40 ℃时,操作压力5 bar,膜面流速4 m/s,浓缩10倍,加30%原液体积水洗滤效果最佳,陶瓷膜平均过滤通量可达102.6 kg/（m2·h）,甜菊糖收率可达99.2%,陶瓷膜过滤结束后先利用质量分数1%~2%的NaOH清洗1 h,再用0.5%~1%硝酸清洗1 h,陶瓷膜水通量恢复率可以达到99%以上,再生效果比较好,可以重复使用。相比絮凝工艺,陶瓷膜脱色率提高了2.6%,甜菊糖收率提高了6.8%,因此膜法工艺可取代传统絮凝工艺实现对甜叶菊提取液的澄清。     

膜分离技术在页岩气压裂返排液处理中的应用

水力压裂返排液是一种页岩气开采废水,其中含有较高浓度的有机物、盐分等,因此水处理难度较大。膜分离技术是目前应用在返排液处理的主要技术之一,因其具有高效低能、出水水质优良、占地面积小以及自动化程度高等特点而受到大量研究应用。本文主要分析了微滤(MF)、超滤(UF)、纳滤(NF)、正向渗透(FO)、反渗透(RO)以及几种组合膜分离技术的原理和特点,综述了它们在返排液处理中的应用研究现状。结果表明:其中MF和UF一般作为压裂返排液的预处理技术;NF、FO和RO主要作为深度处理技术。然而,膜污染问题阻碍了膜技术在压裂返排液处理方面的发展与应用,研究开发新型膜材料,改进预处理和膜分离工艺以及优化膜清洁技术等方法可以实现膜污染的控制。     

海水淡化预处理技术的现状及发展

针对传统海水淡化预处理技术存在的问题，指出微滤（MF）、超滤（UF）、纳滤（NF）和纳滤集成技术将逐渐补充和取代传统海水淡化预处理，而且MF、UF、NF和反渗透（RO）组合起来的新型的海水淡化集成技术将成为该领域的发展趋势。     

膜技术分离纯化燕麦蛋白的工艺研究

根据酶法提取燕麦中的燕麦蛋白,将浸提液过滤后通过膜设备工作过程进行除杂浓缩。经过实验得出,微滤膜、超滤膜和纳滤膜分别选用MF1、UF2和NF1作为最佳膜设备。对燕麦提取液进行除杂浓缩,能够去除大部分的固形杂质,并将水提液浓缩11.88倍,将测定得到燕麦蛋白的含量达到92.76%。     

陶瓷膜过滤万古霉素的研究

以预处理后万古霉素发酵液为料液,连续洗滤（CFD）过滤的效果更佳,表现在较高通量和收率。考察了陶瓷膜过滤万古霉素发酵液的分离效果,结果表明,通量与黏度成负相关性,50 nm陶瓷膜较优,且设定操作压力290 kPa,膜面流速5 m/s,温度20～30 ℃,浓缩1.66倍,连续洗滤2.5 BV,CFD过滤的平均通量可达78.9 kg/（h·m2）,收率可达99.1%,与数学模型的理论值相近。采用质量分数为2%～3% NaOH与0.5%～1.0% NaClO混合清洗的方法,清洗后陶瓷膜的水通量重复恢复率可达98%以上,再生性较好。     

海水淡化预处理技术的现状及发展

针对传统海水淡化预处理技术存在的问题,指出微滤(MF)、超滤(UF)、纳滤(NF)和纳滤集成技术将逐渐补充和取代传统海水淡化预处理,而且MF、UF、NF和反渗透(RO)组合起来的新型的海水淡化集成技术将成为该领域的发展趋势.     

膜分离技术提取枸杞多糖的工艺

采用微滤、超滤操作对枸杞多糖提取液进行了处理,结果表明：操作压力、操作时间及料液温度对膜通量有很大的影响．由微滤和超滤相结合对枸杞多糖的截留率可达到90．4％．枸杞多糖的定量测定采用硫酸-苯酚显色法;枸杞多糖的相对分子量测定采用凝胶渗透色谱法。     

Purification of Steviosides by Membrane and Ion Exchange Processes

An ultrafiltration (UF) process removed more than 96% of the pigments and recovered 45% of steviosides non-nutritive sweetener from an extract of leaves. UF retentate was further processed by diafiltration (DF), and the permeate was concentrated by reverse osmosis (RO). The membrane processes (UF, DF, RO) achieved an overall steviosides recovery of more than 90% with product purity 46%. Final purification was conducted by two consecutive mixed bed ion exchange processes. The ion exchangers improved purity of the final product to 90%.     

采用膜分离技术高效分离提取L-亮氨酸

为提高L-亮氨酸提取得率,文中采用微滤、离交、超滤和反渗透技术对亮氨酸发酵液进行处理,重点研究了有机膜分离提取亮氨酸的工艺。确定膜分离工艺为:进料温度控制在45℃,pH调节至4.0;微滤压力0.1MPa,超滤压力0.25MPa,反渗透压力1.5MPa;反渗透浓缩倍数3～4效果最好。应用有机膜技术提取亮氨酸,其收率可达86.75%,产品纯度达98.58%。     

Recovery and purification of potato proteins from potato starch wastewater by hollow fiber separation membrane integrated process

Potato starch wastewater contains high-concentration potato proteins which have great potential in the fields of food and health care. Most researches on potato protein recovery by membrane separation technique are focused on flat sheet or tubular ultrafiltration (UF) and reverse osmosis (RO) membranes and lack the further protein purification and the in-depth discussions on the fouling behavior. In this laboratory-scale study, potato proteins were recovered and purified from the simulated potato starch wastewater by the self-made hollow fiber (HF) UF and nanofiltration (NF) separation membrane integrated process. 85.62% potato proteins with high molecular weight in the potato starch wastewater could be retained by UF membrane and 92.1% potato proteins with low molecular weight were rejected by NF membrane. The concentrated solution after UF and NF filtration was desalinated and purified by diluting the solution eight times and filtering the diluted solution with UF membrane. Both types of HF membranes, UF and NF, suffered the inevitable membrane fouling. After the traditional physical washing and chemical cleaning, water flux of UF and NF membranes can be effectively recovered. The corresponding recovery rates of UF and NF membranes can reach 93.5% and 84.7%, respectively. The hollow fiber UF-NF separation membrane integrated process was proved to be a promising technique of high-purity potato protein recovery from potato starch wastewater.     

Membrane Clarification of Black Tea Extracts

Microfiltration (MF; 200 and 450 nm) and ultrafiltration (UF; 25, 50, 100 and 500 kDa) membranes were assessed for the clarification of black tea extracts. Rejection of tea components including cream components increased with decrease in membrane pore size. Clarity of membrane processed extracts was excellent (～4 Nephelometric Turbidity Units) even after 30 days of refrigerated storage. UF-500 and MF membranes resulted in greater retention of original colour, besides greater recovery of tea solids including polyphenols in the clarified extract. Increase in feed concentration affected the recovery while diafiltration improved the solids recovery including polyphenols and theaflavins. Highest productivity was achieved at 2 % feed concentration followed by 0.6 %. Solids and polyphenols recoveries obtained with 0.6 % feed concentration and MF-450 membrane combination were unmatched with any other combination. The results favoured employing MF as a means of clarification of tea extracts, preferably at low feed concentration which provided greater recovery and productivity, adequately meeting the quality requirements of ready-to-drink tea beverages.     

Production efficiency of micellar casein concentrate using polymeric spiral-wound microfiltration membranes

Most current research has focused on using ceramic microfiltration (MF) membranes for micellar casein concentrate production, but little research has focused on the use of polymeric spiral-wound (SW) MF membranes. A method for the production of a serum protein (SP)-reduced micellar casein concentrate using SW MF was compared with a ceramic MF membrane. Pasteurized (79°C, 18s) skim milk (1,100 kg) was microfiltered at 50°C [about 3 × concentration] using a 0.3-μm polyvinylidene fluoride spiral-wound membrane, bleed-and-feed, 3-stage process, using 2 diafiltration stages, where the retentate was diluted 1:2 with reverse osmosis water. Skim milk, permeate, and retentate were analyzed for SP content, and the reduction of SP from skim milk was determined. Theoretically, 68% of the SP content of skim milk can be removed using a single-stage 3× MF. If 2 subsequent water diafiltration stages are used, an additional 22% and 7% of the SP can be removed, respectively, giving a total SP removal of 97%. Removal of SP greater than 95% has been achieved using a 0.1-μm pore size ceramic uniform transmembrane pressure (UTP) MF membrane after a 3-stage MF with diafiltration process. One stage of MF plus 2 stages of diafiltration of 50°C skim milk using a polyvinylidene fluoride polymeric SW 0.3-μm membrane yielded a total SP reduction of only 70.3% (stages 1, 2, and 3: 38.6, 20.8, and 10.9%, respectively). The SP removal rate for the polymeric SW MF membrane was lower in all 3 stages of processing (stages 1, 2, and 3: 0.05, 0.04, and 0.03 kg/m² per hour, respectively) than that of the comparable ceramic UTP MF membrane (stages 1, 2, and 3: 0.30, 0.11, and 0.06 kg/m² per hour, respectively), indicating that SW MF is less efficient at removing SP from 50°C skim milk than the ceramic UTP system. To estimate the number of steps required for the SW system to reach 95% SP removal, the third-stage SP removal rate (27.4% of the starting material SP content) was used to extrapolate that an additional 5 water diafiltration stages would be necessary, for a total of 8 stages, to remove 95% of the SP from skim milk. The 8-plus stages necessary to remove >95% SP for the SW MF membrane would create more permeate and a lengthier process than required with ceramic membranes.     

膜分离在蛋白质分离纯化中的应用

以压力差为推动力膜分离过程（过滤，超滤，纳滤，反渗透）的分离性能由透过通量和截留率表征，其操作模式分浓缩和渗滤两种。膜分离技术用于分离，纯化，回收和浓缩蛋白质，如乳清蛋白，血清白蛋白，蛋清蛋白，西蒙德木蛋白，重组白细胞介素－2包涵体以及二元蛋白质混合物等。     

The ultrafiltration molecular weight cut-off has a limited effect on the concentration and protein profile during preparation of human milk protein concentrates

Optimizing protein intake for very low birth weight (<1,500 g) infants is fundamental to prevent faltering postnatal growth with the potential association of impaired neurodevelopment. The protein content of human milk is not sufficient to support the growth of very low birth weight infants. To meet their elevated protein requirements, human milk is currently fortified using typically bovine milk-based protein isolates (>85% on a dry basis). However, these products have several limitations for use in this vulnerable population. To overcome the shortcomings of bovine milk-based protein supplement, a human milk protein concentrate (HMPC) was developed. In preliminary attempts using 10 kDa ultrafiltration (UF) membranes, it was not possible to reach the protein content of commercial protein isolates, presumably due to the retention of human milk oligosaccharides (HMO). Consequently, it was hypothesized that the use of a UF membrane with a higher molecular weight cut-off (50 kDa rather than 10 kDa) could improve the transmission of carbohydrates, including HMO, in the permeate, thus increasing the protein purity of the subsequent HMPC. The results showed that permeate fluxes during the concentration step were similar to either UF molecular weight cut-off, but the 50-kDa membrane had a higher permeate flux during the diafiltration sequence. However, it was not sufficient to increase the protein purity of the human milk retentate, as both membranes generated HMPC with similar protein contents of 48.8% (10 kDa) and 50% (50 kDa) on a dry basis. This result was related to the high retention of HMO, mainly during the concentration step, although the diafiltration step was efficient to decrease their content in the HMPC. As the major bioactive proteins (lactoferrin, lysozyme, bile salt stimulated lipase, and α1-antitrypsin) in human milk were detected in both HMPC, the 50-kDa membrane seems the most appropriate to the preparation of HMPC in terms of permeation flux values. However, improving the separation of HMO from proteins is essential to increase the protein purity of HMPC.     

Membrane Fractionation Processes for Removing 90% to 95% of the Lactose and Sodium from Skim Milk and for Preparing Lactose and Sodium‐Reduced Skim Milk

ABSTRACT: Pilot‐scale microfiltration (MF), microfiltration‐diafiltration (MDF), ultrafiltration (UF), ultrafiltration‐diafiltration (UDF), and nanofilration (NF) membrane fractionation processes were designed and evaluated for removing 90% to 95% of the lactose and sodium from skim milk. The study was designed to evaluate several membrane fractionation schemes as a function of: (1) membrane types with and without diafiltration; (2) fractionation process temperatures ranging from 17 to 45 °C; (3) sources of commercial drinking water used as diafiltrant; and (4) final mass concentration ratios (MCR) ranging from about 2 to 5. MF and MDF membranes provided highest flux values, but were unsatisfactory because they failed to retain all of the whey proteins. UDF fractionation processes removed more than 90% to 95% of the lactose and sodium from skim milk. NF permeate prepared from UDF cumulative permeate contained sodium and other mineral concentrations that would make them unsuitable for use as a diafiltrant for UDF applications. A method was devised for preparing simulated milk permeate (SMP) formulated with calcium, magnesium, and potassium hydroxides, and phosphoric and citric acids for use as UDF diafiltrant or for preparing lactose and sodium reduced skim milk (L‐RSM). MF retentates with MCR values of 4.7 to 5.0 exhibited extremely poor frozen storage stabilities of less than 1 wk at ?20 °C, whereas MCR 1.77 to 2.95 MDF and UDF retentates and skim milk control exhibited frozen storage stabilities of more than 16 wk. L‐RSM exhibited a whiter appearance and a lower viscosity than skim milk, lacked natural milk flavor, and exhibited a metallic off‐flavor.