电渗析法脱除氨法烟气脱硫浆液中的氟离子

利用异相膜电渗析装置去除氨法烟气脱硫浆液中的F~-。考察了脱硫浆液p H、F~-初始质量浓度、Cl~-初始质量浓度、膜堆两端电压、浓缩室和淡化室循环流量等操作参数对F~-去除效果的影响。实验结果表明:在酸性条件下,F~-去除率更高;脱硫浆液中F~-初始质量浓度越高,F~-去除率越高;Cl~-初始质量浓度较低时会增加F~-去除率,过高时又会降低F~-去除率。优化的操作条件为:膜堆两端电压25 V,浓缩室和淡化室循环流量300 L/h。一级电渗析进行100 min后,Cl~-去除率接近100%,F~-去除率只有47.3%。二级电渗析进行100 min时,F~-去除率达92.2%。一、二级电渗析F~-累积去除率达96.1%。     

油田钻井废水深度处理技术

采用化学混凝-铁炭微电解-电渗析技术对钻井废水进行了深度处理实验。实验结果表明：废水pH和反应时间是影响铁炭微电解处理效果的重要因素,当废水pH为1．5,反应时间为120min时,COD去除率为50％;在电渗析除Clˉ过程中,采取直流方式出水时,在进水流量为20L／h、操作电压为30V、运行时间为15min的条件下,Clˉ去除率可达75％;而采取循环方式出水时,运行时间是影响电渗析除Clˉ效果的主要因素,当运行时间大于等于60min时,出水中Clˉ的质量浓度低于350mg/L,达到DB51／190-1993（四川省污水排放标准》中的三级排放标准。     

一种电镀废液中酸分离与重金属回收的方法

正该专利涉及一种电镀废液中酸分离与重金属回收的方法。先利用电渗析集成技术快速分离电镀废液中的酸,通过对电渗析过程中阴、阳离子膜的选择可以很好地将电镀废液中的酸分离,同时重金属离子仍留在电镀废液中。分离出来的酸进入浓缩池,回收后可用于电镀或镀件清洗工序。处理后的电镀废液中pH达3以上。利用硫化氢气体和射流工艺集成技术能够快速回收电镀废液中的有价重金     

高含盐废水脱盐处理技术研究进展

综述了几种常见的高含盐废水脱盐处理技术的发展历程、工艺原理、优缺点及目前的研究进展,分析了热分离、膜分离、电渗析、离子交换、电吸附、微生物脱盐等方法的优缺点,展望了未来废水脱盐工艺的发展方向。指出：脱盐方法将根据各类水体的水质特点更加精细化;多种脱盐技术联合应用也是今后废水脱盐的发展方向。     

不锈钢酸洗废液的处理与回收技术综述

介绍了不锈钢酸洗废液的来源、组成和危害.综述了酸洗废液中酸及金属的回收方法、原理及优缺点,着重介绍了酸的扩散渗析、双极膜电渗析、蒸酸和焙烧回收技术,以及金属盐的中和沉淀、析晶、离子交换树脂和萃取回收技术.指出将多种技术进行组合,可实现酸洗废液中金属盐和酸的双重回收.     

钽铌冶炼厂含氟废水资源化治理技术

采用合金膜电渗析法分离富集钽铌冶炼厂含氟废水中的F^-和SO₄^2-。最优的工艺运行条件为：膜对电压0.500 V,膜面流速4.09 cm/s。在此条件下电渗析30 min,F^-去除率达97.53%,SO₄^2-去除率接近100%。优化条件下运行电渗析器,一段淡水中大部分的F^-和SO₄^2-均被去除,可以直接回用。一段电渗析的浓水再经多段电渗析浓缩,以LiOH·H₂O沉淀F^-得到LiF产品,该LiF产品纯度达99.06%,满足GB/T 22666—2008标准的3级品要求。LiF收率为84.92%,F^-整体回收率为79.45%。     

双极膜电渗析法回收丙烯酸丁酯废水中的有机酸

采用三隔室型双极膜电渗析装置将丙烯酸丁酯废水中的丙烯酸钠和对甲基苯磺酸钠转化为丙烯酸和对甲基苯磺酸并回收有机酸溶液,研究了料室与酸室初始溶液体积比对转化过程的影响.实验结果表明:当料室与酸室初始溶液体积比为5时,回收的有机酸溶液中丙烯酸和对甲基苯磺酸的质量浓度分别达161.5 g/L和25.0 g/L;整个电渗析过程的...     

电渗析分离硫酸钠溶液的研究

工业生产中经常遇到含酸、碱、盐的废水,尤其是低浓度废水,直接排放既浪费资源又污染环境,如果加以处理则可以回收工业原料并将水净化。采用常规的方法处理低浓度的废水比较困难且成本较高,而用电渗析方法提浓后,再用常规的方法处理则可以大大降低成本。我们对电渗析分离硫酸钠水溶液过程中极限电流密度与浓度、流量、温度等因素的关系进行了研究。１　试验部分１１　原料无水硫酸钠,无水亚硫酸钠（分析纯）。１２　装置电渗析器：２００×４００ｍｍ（一级一段）;隔板：无回路聚丙烯编织网;膜类：均相阴、阳离子交换膜;电极：…     

从含铬铝泥中回收铝的新工艺

采用"打浆水洗除Cr(Ⅵ)—电渗析除Cr(Ⅵ)—碱浸提铝—碳酸化分解法精制Al_2O_3"的新工艺处理含铬铝泥(以下简称铝泥),并回收Al_2O_3。实验结果表明:铝泥在70℃下经3次打浆水洗后,w(Na_2CrO_4)(以干铝泥计)降至5.0%;采用电渗析除Cr(Ⅵ)工艺可有效去除铝泥中以结合态和结晶态形式存在的Na_2CrO_4,在55 V直流电压下电渗析6h后铝泥中的w(Na_2CrO_4)降至0.98%;在碱浸温度为100℃、碱浸时间为3 h、NaOH质量浓度为150 g/L的优化碱浸条件下,铝浸出率(以Al_2O_3计)高达90.0%;经3次碳酸化分解处理后,Al_2O_3产品的纯度达98.65%,满足GB/T 24487-2009《氧化铝》中的一级标准,Al_2O_3回收率为96.37%。     

螺旋式电除盐器—不用酸碱再生的去离子设备

离子交换技术的应用历史悠久 ,离子交换器已成为工业水处理中不可缺少的设备。然而 ,离子交换器运行一定时间后 ,必须用大量酸碱对树脂进行再生。所以 ,使用这种设备酸碱费用较高 ,劳动强度较大 ,对排放的废水必须处理 ,设备和下水道必须防腐。长期以来 ,人们不断研究不用酸碱和无公害的再生离子交换树脂的方法 ,国外最近开发成功的电去离子法 ( EDI) ,是一种将电渗析技术和离子交换技术结合在一起的脱盐新工艺。由于它能够连续不断地去除水中的离子 ,因此又称为连续去离子法( CDI)。1　EDI的应用和 DCJ的问世图 1　 DCJ纵截面结构示…     

Electrodialysis for NaCl/EG solution using ion-exchange membranes

A new concept for the recycling of poly(vinyl chloride) (PVC) has been introduced, including the dehydrochlorination of PVC in ethylene glycol (EG) with NaOH as a reactant, the subsequent separation of NaCl from EG by electrodialysis, and the recovery of chlorine for the synthesis of new PVC. In this work, the separation of NaCl by electrodialysis was investigated. About 98 % of the salt were recovered from EG, with less than 10 % of the EG permeating the membranes after 5 h.     

电渗析法处理低浓度乙酸废液的研究

用电渗析法处理配制的乙酸质量分类为２．５％左右的乙酸水溶液，浓缩液乙酸质量分数达到２０％，稀相出水乙酸质量分数至０．０２％；对影响处理过程的因素进行了探讨。     

Removal of chloride from ethylene glycol solution using alumina/zeolite membrane as a physical boundary between the organic and aqueous phases

The permeation of Cl^? ions from a NaCl/ethylene glycol (EG) solution during electrodialysis was investigated using alumina and alumina/zeolite membranes. Voltage changes had very little effect on Cl^? permeation through the alumina membrane, suggesting that the driving force for the permeation was concentration-gradient-induced diffusion, and not the electric field. Solvation of the Na⁺ ions by EG resulted in EG migration through the membrane. Replacement of the deionized water (electrolyte) in the anodic cell with NaOH resulted in increased Cl^? permeation, although a greater amount of EG migrated into the NaOH solution as well. No notable difference was observed in Cl^? permeation through the alumina and alumina/zeolite membranes, but EG migration decreased when using the latter membrane, suggesting that EG migration was prevented by the zeolite layer. The proposed alumina/zeolite membrane is, hence, useful for solvent recovery by electrodialysis, but its mechanical stability must be improved for industrial applications.     

Electro and Baromembrane Methods of Petrochemical Enterprises' Wastewater Treatment

The paper focuses on the development of production methods for new ion‐exchange membranes on the basis of ED‐20 industrial epoxide resin, resorcinol diglycidyl ether (RDGE), vinyl ether of monoethanolamine (VEMEA), and different di‐ and polyamines (polyethylenepolyamine (PEPA), polyethyleneimine (PEI), and hexamethylenediamine (HMDA)) in the presence of polyvinyl chloride (PVC) as a thermoplastic polymer binder. With the purpose to establish optimum conditions for synthesis of interpolymer membranes, the influence of reactants' concentration, of the temperature, of the nature and the quantity of the solvent, and of the process duration, was studied. It was found that when the VEMEA content in the reaction mixture is increased, the static exchange capacity (SEC) of the membrane increases in the presence of: PEI in the range of 1.2 to 4.7 mEq/L; PEPA: 1.0 to 4.0 mEq/L; and, HMDA: 1.4 to 5.2 mEq/L. It was shown that the optimum synthesis conditions are heating the reaction mixture to 60 °C to 70 °C for six to seven hours with constant stirring. For increasing the basicity of membranes, N‐alkylation was carried out using known alkylating agents (methyl iodide, dimethyl sulfate, and epichlorohydrin (ECH)). The primary electrochemical and physic‐mechanic properties of the obtained membranes were studied on pilot electrodialysis cells. The process flow diagram of the electrodialysis plant, as well as the engineering design documentation thereof were developed, and a pilot electrodialysis plant was constructed. The maximum production capacity of the pilot plant was 600 L/hr with a 30 percent desalinization rate. To increase the desalinization rate up to 75 percent, circulation of the solution and a decrease of production capacity was suggested. For meeting the treated water requirements in terms of salt content, a partial recirculation mode was introduced. In the course of the studies conducted, a process flow diagram was developed, and an experimental installation and a pilot reverse osmosis plant were fabricated for phenol and ammonium nitrogen purification. The pilot plant was tested using process condensate from the Pavlodar Petrochemical Plant. It was found that prior oxidation of the condensate with ozone in alkali medium resulted in phenol purification up to 85 percent and ammonium nitrogen up to 93 percent. ©2015 Wiley Periodicals, Inc.