超滤-反渗透集成工艺处理玉米酒糟废水

研究了玉米酒精生产过程中产生的玉米酒糟废水的膜分离过程,开发了处理玉米酒糟废水的超滤-反渗透集成工艺。超滤选用截留相对分子质量为6 000的GR81PP膜平板分离器,入口压力控制为0.6 MPa,操作温度为50℃;反渗透选用标准脱盐率为90%的ESNAI-4040卷式膜分离器,入口压力控制为2.2 MPa,操作温度为40℃。反渗透透过液中蛋白质的平均截留率为94.70%,甘油的平均截留率为65.15%,COD值降到1 000 mg/L左右,可作为工艺回用水,而且反渗透浓缩液中可回收甘油等有用物质,超滤浓缩液可浓缩成饲料,节能效果显著。     

商务信息

TPT 0100反渗透阻垢分散剂（8倍浓缩液），TPT 0150反渗透/纳滤膜阻垢分散剂（8倍浓缩液），TPT 0150反渗透/纳滤膜阻垢分散剂（4倍浓缩液），TPT 2000反渗透/纳滤膜阻垢分散剂（4倍浓缩液），TPT 0300反渗透/纳滤膜阻垢分散剂（4倍浓缩液）。     

商务信息

TPP0100反渗透阻垢分散剂（8倍浓缩液），TPT0150反渗透/纳滤膜阻垢分散剂（8倍浓缩液），TPT0150反渗透/纳滤膜阻垢分散剂（4倍浓缩液），TPT2000反渗透/纳滤膜阻垢分散剂（4倍浓缩液），TPT0300反渗透/纳滤膜阻垢分散剂（4倍浓缩液）。[编者按]     

商务信息

TPT0100反渗透阻垢分散剂（8倍浓缩液），TPT0150反渗透/纳滤膜阻垢分散剂（8倍浓缩液），TPT0150反渗透/纳滤膜阻垢分散剂（4倍浓缩液），TPT200反渗透/纳滤膜阻垢分散剂（4倍浓缩液）     

商务信息

TPT 0100反渗透阻垢分散剂（8倍浓缩液）；TPT 0150反渗透/纳滤膜阻垢分散剂（8倍浓缩液）；TPT 0150反渗透/纳滤膜阻垢分散剂（4倍浓缩液）；TPT 2000反渗透/纳滤膜阻垢分散剂（4倍浓缩液）；TPT 0300反渗透/纳滤膜阻垢分散剂（4倍浓缩液）。     

商务信息

TPT 0100反渗透阻垢分散剂（8倍浓缩液）；TPT 0150反渗透/纳滤膜阻垢分散剂（8倍浓缩液）；TPT 0150反渗透/纳滤膜阻垢分散剂（4倍浓缩液）；TPT 2000反渗透/纳滤膜阻垢分散剂（4倍浓缩液）；TPT 0300反渗透/纳滤膜阻垢分散剂（4倍浓缩液）。[编者按]     

商务信息

TPT 0100反渗透阻垢分散剂（8倍浓缩液）;TPT 0150反渗透/纳滤膜阻垢分散剂（8倍浓缩液）;TPT 0150反渗透/纳滤膜阻垢分散剂（4倍浓缩液）;TPT 2000反渗透/纳滤膜阻垢分散剂（4倍浓缩液）;TPT 0300反渗透/纳滤膜阻垢分散剂（4倍浓缩液）……     

反渗透浓缩液的再利用

介绍了反渗透浓缩液再利用的方法,综述了这些方法的原理、特点及应用,重点讨论了脱除反渗透浓缩液过饱和度进行回用以提高系统回收率的方法,以及膜蒸馏技术对浓缩液的回用处理、废水浓缩液处理及海水淡化浓缩液制盐,指出了反渗透浓缩液再利用在经济和环境上的必要性。     

商务信息

TPT 0100反渗透阻垢分散剂（8倍浓缩液）;TPT 0150反渗透/纳滤膜阻垢分散剂（8倍浓缩液）;TPT 0150反渗透/纳滤膜阻垢分散剂（4倍浓缩液）;TPT 2000反渗透/纳滤膜阻垢分散剂（4倍浓缩液）;TPT 0500反渗透/纳滤膜阻垢分散剂（4倍浓缩液）;     

商务信息

TPT0100反渗透阻垢分散剂（8倍浓缩液）;TPT0150反渗透/纳滤腆阻垢分散剂（8倍浓缩液）;TPT0150反渗透/纳滤腆阻垢分散剂（4倍浓缩液）;TPT2000反渗透/纳滤腆阻垢分散剂（4倍浓缩液）;TPT0300反渗透/纳滤腆阻垢分散剂（4倍浓缩液）.     

Reverse osmosis and ultrafiltration of stillage solubles from dry-milled corn fractions

Grits, flour, degerminated meal and hominy feed from corn were fermented to make ethyl alcohol. The stillage, remaining after distillation of alcohol, was separated by screening and centrifuging into insoluble and soluble fractions. The stillage solubles contained 0.036 to 0.080% nitrogen and 1.4 to 7.2% total solids. Ultrafiltration (UF) membranes separated stillage solubles into permeate and concentrate fractions. Permeates from stillage solubles accounted for 85 to 95% of the original volume, 44 to 67% of the total solids and 40 to 75% of the total nitrogen. Reverse osmosis (RO) membranes separated the UF permeate into RO permeate and RO concentrate fractions. The RO permeate accounted for 70 to 92% of the original volume, 5 to 15% of the total solids and 5 to 21% of the total nitrogen in the UF permeate. Conductivity of some RO permeate fractions was lower than that of tap water. The combination of UF and RO processing of stillage solubles from corn dry-milled fractions appears to be an attractive method to recover most of the solids and nitrogen in small volumes of concentrate, and produces a final permeate with a low concentration of solids and nitrogen. The RO permeate may be reused as water, treated further or discharged. Presented at the AOCS Annual Meeting, May 1984, Dallas, Texas. Deceased.     

Whey fractionation through the membrane separation process

The aim of this work is to improve the utilisation of fractions of whey through membrane separation processes. From a solution of whey treated by ultrafiltration (UF) associated with diafiltration (DF), two streams were obtained: a concentrate and a permeate. In this process, a purified protein concentrate with about 70% of protein was obtained. Permeate was treated by electrodialysis (ED) to obtain a fraction rich in lactose (90%). The final effluent was treated by reverse osmosis (RO) in order to recover water free of salts. RO made it possible to recover 50% water and retain 85% of the salts.     

An advanced treatment of high-strength opium alkaloid processing industry wastewaters with membrane technology: pretreatment, fouling and retention characteristics of membranes

This paper presents the results of the laboratory and pilot-scale membrane experiments of opium alkaloid processing industry effluents. Different types of ultrafiltration (UF), nanofiltration (NF) and reverse osmosis (RO) membranes were evaluated for membrane fouling, permeate flux and their suitability in separating COD, color and conductivity. Experiments demonstrated that membrane treatment is a very promising advanced treatment option for pollution control for opium alkaloid processing industry effluents. Almost complete color removal was achieved with NF and RO membranes. COD and conductivity removals were also greater than 95% and met the current local standards. Nevertheless, pretreatment was an important factor for the NF and RO membrane applications. Membrane fouling occurred with direct NF membrane applications without UF pretreatment. The total estimated cost of the UF and NF treatment system was calculated as $0.96/m³, excluding the concentrate disposal cost.     

Water Quality Improvement by Combined UF,RO, and Ozone/Hydrogen Peroxide System (HiPOx) in the Water Reclamation Process

Conventional water reclamation processes, such as membrane bioreactors, are not always effective in removal of pharmaceuticals and personal care products (PPCPs), endocrine disrupting chemicals (EDCs) and/or N-nitrosodimethylamine (NDMA), even with the reverse osmosis (RO) membrane process. A study was conducted, at a NEWater factory in Singapore, to compare a conventional ultrafiltration (UF) membrane /RO treatment process with a treatment train having the HiPOx unit, an advanced oxidation process (AOP), which was installed between the UF and the RO unit operations. By incorporating the HiPOx into the UF/RO treatment process, following results were observed; 1) increased removal of PPCPs, EDCs and NDMA, 2) improvement in ultraviolet transmission (UVT) of the RO permeate, 3) enhanced removal of TOC and color, and increased UVT of the RO brine, 4) suppression of the increase in the RO transmembrane pressure by organic fouling.     

Digital textile printing (DTP) wastewater treatment using ozone and membrane filtration

Digital textile printing (DTP) is considered as an environmentally benign process because its wastewater production is relatively small compared with the conventional textile printing system. DTP is usually practiced at building office in an urban area rather than in a textile industrial complex, so that process development for on-site treatment of the DTP wastewater is currently needed. The aim of this study was to propose a DTP wastewater treatment system suitable for operation in building and to verify if the proposed system has a rationale treatment system should be compact and reliable because it should be installed near the DTP system. Thus, a hybrid system consisting of ozone, ultrafiltration (UF) and reverse osmosis (RO) was proposed for treatment of DTP wastewater. Prior to UF and RO, ozone was introduced to the DTP wastewater to reduce organic loadings to membrane filtration as well as to treat the concentrates recycled from UF and RO. When ozone was injected with C-T value of 255 g·s/L, the removal efficiency of COD and color was 63 and 81%, respectively. Ozonation of the DTP wastewater led to aggregation of colloidal particles, so that the cake resistance (R_c) calculated after ozone and UF was lower than that of the control (= without ozonation), suggesting that pre-ozonation is beneficial to not only flux enhancement but also to good permeate water quality. Further treatment of UF permeates using RO was carried out since the UF permeates was not enough for direct discharge or reuse. Final effluents through the whole process of ozonation, UF and RO met the criteria of direct discharge and reuse, suggesting that the proposed hybrid system could be used for DTP wastewater treatment satisfactorily.     

Electrodialysis Application of the Ultrafiltration Permeate of Milk Before and After Reverse Osmosis

Ultrafiltered (UF) milk permeate was concentrated by reverse osmosis (RO). UF and UF + RO samples were then desalted by electrodialysis (ED) to three levels of desalination: 1, 2.5, and 4 % of ash in the dry matter. Ions were analyzed by a new high‐performance liquid chromatography method, which enables simultaneous estimation of cations and anions. ED of UF permeate has some advantages over that of UF + RO samples, including a shorter ED time and a higher average salt flow rate, but RO treatment of UF permeate before ED enables the processing of larger volumes of UF permeate. Therefore, ED of milk permeate, particularly after RO, improves the handling characteristics and may offer advantages for further processing of secondary dairy products.     

Grey water treatment and simultaneous surfactant recovery using UF and RO process

The membrane-based grey water treatment for grey water reuse and surfactant recovery is presented in this research paper. Grey water from washing machine discharges having turbidity and used surfactant was processed through the polymeric ultrafiltration (UF) membrane to remove the turbidity. The UF treated grey water is further purified by reverse osmosis (RO) membrane for surfactant recovery and water reuse. The surfactant trapped inside the RO spiral wound membrane module is recovered through various membrane physical regeneration techniques such as backwashing, simultaneous backwash–back-flush and ozone back-flush. Among this, backwash–back-flush is found to be effective process for surfactant recovery. The methodology for optimising surfactant recovery is captured by studying effect of various operating parameters such as feed detergent concentration, backwash pressure, backwash temperature and back-flush flow rate. By implementing optimal process conditions, the integrated UF and RO membrane process is able to produce 300 L of reusable pure water and 80 L of concentrated detergent solution and 20 L of turbid water while treating 400 L of grey water discharges. Maximum surfactant recovery of 82% is obtained while treating grey water which consists of 720 ppm of total dissolved solids (detergent) and 45 ppm of surfactant. The extent of UF and RO membrane fouling is determined by measuring the pure water flux before and after the grey water treatment. The membrane performance is found to be stable when membrane is regenerated by backwash–back-flush technique for RO and gravity backwash for UF membrane.     

Optimization of PACl dose to reduce RO cleaning in an IMS

In order to ensure stable treated water quality and to reduce chemical costs in any treatment plant it is necessary to study and optimize the coagulant dosing control (CDC). This research focused on the affects of coagulant in the integrated membrane (UF & RO) system employed for industrial water production. The dose of coagulant (PACl) might be associated (partly) with the frequency of cleaning in the RO units, and a value of 20 abs/m in the UF permeate is the control of the dosage process. This could suggest that organic fouling is directly and indirectly (inducing biofouling as well) the cause of fouling of the RO membranes. Nevertheless, high doses of PACl could produce scaling of aluminium and, in this work minimizing PACl to prevent operational problems in RO membranes was focused.

The approach involved the study of the treatment processes, determination of the optimum dose of coagulant, evaluation of the removal efficiency of UV and DOC by coagulation. The available data, which comprised monthly/weekly measurements for a period of six years of operation, was studied and analyzed and an attempt was made to draw some conclusions for the plant regarding the coagulant dosage and the link with UV absorbance as control.

The study of the coagulant dosing control revealed that the use of simple and robust online sensors like UV measurement allows an automatic dosing control although this parameter is not found to be sufficient to fully characterize nor predict fouling during membrane operation and there is no link between UV after the UF and the cleaning frequency of the RO. Parameters, as the added value allowed to verify the doses efficiencies in UV and DOC removal. Coagulant dose depends on the level of UV absorbance in the UF permeate and it should never be higher than 20 abs/m to ensure a RO cleaning frequency as long as possible. However, it was found that the target value of 20 abs/m produced substantial over dose of coagulant — 90% of the time – when UV removal is considered only. In the same way, for coagulant doses in excess of 5 mg/L, the additional removal of UV is less than 2.5% per mg coagulant/L, which suggests that the current dose is on the high side.

Furthermore, a coagulant dose in excess of 5 mg/L did not produce significant additional UV removal, and thus a reduction from 14 mg/L (2005 dose) to ca. 7 mg/L could be considered.     

微纳米气泡对超滤膜过滤腐植酸污染影响研究

为有效解决超滤过程中因有机物堵塞膜孔导致的膜污染和渗透通量下降问题，提出在对腐植酸（HA）溶液超滤传输及反洗过程中引入微纳米气泡水处理工艺，以强化超滤过程，实验研究了微纳米气泡对超滤膜渗透通量和截留效率的影响以及膜污染去除效果。结果表明在纯水和HA溶液中鼓入微纳米气泡后其归一化通量增大到1.1~1.3，截留效率提高了2.5%~22.0%，微纳米气泡水清洗和反洗后膜通量恢复分别高于纯水21%和25%。