博士学位论文
湖南大学
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I
离子交换膜化学反应器去除水中铬(Ⅵ)和磷酸盐的研究
II
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南昆山攻略摘 要刘禹锡的古诗
水溶性污染物铬()Ⅵ和磷若超标，会对环境和人体健康产生严重的危害。目前对于水中铬(Ⅵ)去除的研究报道绝大多数是针对工业废水中铬(Ⅵ)的去除，而专门针对饮用水中铬()Ⅵ去除的研究报道则相对较少。污水处理厂出水中总磷以磷酸盐、聚磷酸盐和有机磷的形式存在，而磷酸盐为主要存在形式，对
摘抄赏析二沉池出水中磷酸盐进行深度处理对于控制总磷排放含量有着极其重要的意义。本研究通过构建离子交换膜化学反应器，并用于水中铬(Ⅵ)和磷酸盐的去除。
麦小麦阴离子交换膜分离铬(Ⅵ)和磷酸盐试验结果表明，当原水中铬()Ⅵ初始浓度为1.0mg/L ，pH 值为6.95左右，补偿溶液NaCl 浓度为0.1mol/L ，原水和补偿溶液进水流量为2.5mL/min ，膜两侧溶液搅拌强度为500r/min ，水温为25℃时，阴离子交换膜对铬()Ⅵ的分离去除率为86.4%，相同试验条件下阴离子交换膜对磷酸盐的分离去除率为84.3%。采用Na 2SO 4作为补偿溶液时，阴离子交换膜对铬()Ⅵ和磷酸盐的分离去除率降低，且其对磷酸盐分离效果的影响较大。不同补偿溶液NaCl 浓度条件下阴离子交换膜对铬()Ⅵ和磷酸盐的分离去除率相差不大，但离子通量随NaCl 浓度的增加而增大。当原水pH 值分别为11.0和3.0时，阴离子交换膜对铬()Ⅵ和磷酸盐的分离去除率降低。膜两侧溶液搅拌强度和水温增大时，铬()Ⅵ和磷酸盐的分离效果提高。增加原水进水流量，阴离子交换膜对铬()Ⅵ和磷酸盐的分离去除率降低。二价共存离子SO 42-对铬()Ⅵ和磷酸盐离子竞争作用大于一价共存离子NO 3-和Cl -，共存离子浓度越高，离子交换竞争作用越强。正交试验结果表明，各因素中原水进水流量和补偿溶液种类分别对铬(Ⅵ)和磷酸盐的分离影响最大，其对分离试验结果有显著影响。
在最佳分离运行参数条件下，单位时间内化学反应池铬()Ⅵ和磷酸盐富集含量均随原水初始浓度的增加而增加。铬(Ⅵ)最佳还原剂投加量为FeSO 4·7H 2O: Cr(Ⅵ)= 20: 1，可适当过量投加硫酸亚铁，不调节原水pH 值。投药量系数增加时，磷酸盐化学沉淀去除效果增加。在3种不同运行方式条件下，离
子交换膜化学反应器对铬(Ⅵ)和磷酸盐处理水中浓度均小于或接近于相应的水质标准要求。优秀啊我
铬(Ⅵ)和磷酸盐离子交换动力学试验结果表明，阴离子交换膜对铬()Ⅵ和磷酸盐的饱和交换容量分别为1.59mmol/g(干膜)和0.51mmol/g(干膜)。铬()Ⅵ和磷酸盐离子交换过程均符合颗粒扩散控制(PDC)动力学模型，增加铬()Ⅵ和磷酸盐初始浓度和温度，离子交换表观速率常数和颗粒扩散系数增大。铬(Ⅵ)和磷酸盐离子从给体池通过阴离子交换膜至化学反应池的迁移交换过程从宏观上可分为3步，膜采用NaCl 溶液浸泡预处理和增加补偿Cl -离子浓度，分别促进铬(Ⅵ)和磷酸盐离子的
博士学位论文
III
第1步和第3步迁移交换过程，而铬(Ⅵ)和磷酸盐离子第2步迁移交换过程主要取决于交换离子和阴离子交换膜的基本特性。补偿溶液NaCl 浓度增加时，阴离子交换膜内铬(Ⅵ)和磷酸盐含量明显降低。两层膜试验中，铬(Ⅵ)含量基本都分布在膜1内，膜2内铬(Ⅵ)含量较少；补偿溶液NaCl 浓度较低和较高时，膜内磷酸盐含量的分布由给体池至化学反应池分别呈递增和递减趋势。原水中存在带电胶体颗粒是造成膜污染的主要原因，阴离子交换膜可采用酸碱化学清洗。
离子交换膜化学反应器分离和去除技术在给水、饮用水源铬()Ⅵ突发性应急处理以及污水中磷酸盐的处理等方面，尤其在有自然咸水可利用的地区，具有潜在的应用价值。
关键词：离子交换膜化学反应器；分离去除率；离子通量；补偿离子；交换容量；膜内含量；膜污染
黄山景点有哪些离子交换膜化学反应器去除水中铬(Ⅵ)和磷酸盐的研究
IV
Abstract
When the concentration of water-soluble pollutants such as Cr()Ⅵ and phosphorus exceeds the water standard, there will be a rious danger to the environment and human health. Currently, most of the rearch of Cr()Ⅵ removal was focud on Cr()Ⅵ removing in industrial effluent, while relatively fewer literatures were specially involved in Cr(Ⅵ) uptake in drinking water. Phosphorus exists in the form of phosphate, polyphosphate and organic phosphorus in the wage effluent, while phosphate is the main form. Advanced treatment for phosphate of the effluent of condary dimentation tank has an extremely important significance for the control of total phosphorus discharge to receiving waters. The aim of this study is to develope an ion-exchange membrane chemoreactor, which will be ud for Cr(Ⅵ) and phosphate removal from aqueous solution.铁观音茶叶
The results of our experiments with Cr(Ⅵ) and phosphate paration by anion-exchange membrane
showed that the paration efficiency of Cr(Ⅵ) from feeding chamber reached 86.4% under the conditons of influent Cr(Ⅵ) concentration 1.0mg/L, pH 6.95, NaCl concentration 0.1mol/L in counterion solution, flow rate of feed and counterion solutions 2.5mL/min, stirring speed 500r/min, and pha temperature 25℃. In addition, the paration efficiency of phosphate by anion-exchange membrane could achieve 84.3% under the identical experimental condition. Using Na 2SO 4 as counterion solution, the paration efficiency of Cr(Ⅵ) and phosphate was reduced, and the latter got a comparatively greater decrea. With the different NaCl concentrations in counterion solution, no change was likely to be found in the paration efficiency of Cr(Ⅵ) and phosphate by anion-exchange membrane; however the ion flux rid dramatically with the increa of NaCl concentration in counterion solution. When initial pH of feed solution was 11.0 and 3.0, the paration efficiency of Cr(Ⅵ) and phosphate dropped. It was also found that the paration efficiency of Cr() and phosphate Ⅵwas greatly improved with the increa of stirring speed and pha temperature in feed and counterion solutions. The paration efficiency of Cr(Ⅵ) and phosphate decread significantly with increasing the flow rate of feed solution. The competitive removal experiments indicated that the divalent ion (SO 42-) had a profound interfering effect compared to monovalent ions (NO 3- and Cl -), and the higher the concentration of coexisting ions, the more stronger
博士学位论文
V of the competitive effect. Orthogonal experiments showed that the flow rate of feed solution and counterion solution species mostly affected the paration of Cr(Ⅵ) and phosphate, respectively, which had a significant impact on the results of paration experiments of Cr(Ⅵ) and phosphate by anion-exchange membrane.
In the optimum operating parameters of paration, the enrichment content of both Cr(Ⅵ) and phosphate in chemoreactor per unit time were incread with the increa of influent concentration in feed solution. The optimum dosage of FeSO 4·7H 2O: Cr(Ⅵ) was found to be 20:1 with reductant removal of Cr(Ⅵ), and appropriately excessive dosage of FeSO 4 could be added without adjustment of pH in raw water. Increasing dosage coefficient with the ratio of PFS to P, the removal efficiency of phosphate by chemical precipitation was enhanced. Effluent concentrations of Cr(Ⅵ) and phosphate treated by ion-exchange membrane chemoreactor were less than or clo to the corresponding water quality standards under three different operation conditions.
Ion exchange kinetics of Cr() Ⅵand phosphate were also specially investigated. The experimental results showed that the saturated exchange capacity of Cr(Ⅵ) and phosphate with anion-exchange
membrane were 1.59mmol/g(dry membrance) and 0.51mmol/g(dry membrance), respectively. The ion exchange process of both Cr() Ⅵand phosphate could be described by the Particle Diffusion Control(PDC) kinetic model. With the increa of initial concentration and pha temperature of Cr(Ⅵ) and phosphate, the apparent rate constant and particle diffusion coefficient of the two ions incread. The transport process of Cr(Ⅵ) and phosphate ions transferred from feeding chamber to chemoreactor through the anion-exchange membrane could be divided into three steps on the whole. Using pretreated anion-exchange membrane immersing in NaCl solution and increasing Cl - concentration in counterion solution could efficiently promote the first and third transport process of Cr(Ⅵ) and phosphate ions, respectively. However, the cond transport process of Cr(Ⅵ) and phosphate ions was mainly depended on the basic characteristic of exchange ion and anion-exchange membrane. When NaCl concentration in counterion solution was incread, the content of Cr() Ⅵand phosphate ions in anion-exchange membrane decread significantly. In the experiments with two overlapping membranes, Cr(Ⅵ) ions mainly distributed in membrane 1, and fewer were found in membrance 2. With lower and higher NaCl concentration in counterion solution, the content of phosphate ions distribution in two overlapping membranes prented increasing and descending trend from side of feeding chamber to side of chemoreactor respectively. The charged
