WO2022165932A1 - 一种电催化氧化-电渗析耦合处理系统及应用 - Google Patents

一种电催化氧化-电渗析耦合处理系统及应用 Download PDF

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WO2022165932A1
WO2022165932A1 PCT/CN2021/081474 CN2021081474W WO2022165932A1 WO 2022165932 A1 WO2022165932 A1 WO 2022165932A1 CN 2021081474 W CN2021081474 W CN 2021081474W WO 2022165932 A1 WO2022165932 A1 WO 2022165932A1
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electrodialysis
electrocatalytic
membrane
membrane stack
electrocatalytic oxidation
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English (en)
French (fr)
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陈勇
刘伟京
徐海波
尤本胜
刘广兵
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江苏省环境科学研究院
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/46104—Devices therefor; Their operating or servicing
    • C02F1/46109—Electrodes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
    • C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/46104—Devices therefor; Their operating or servicing
    • C02F1/46109—Electrodes
    • C02F2001/46133—Electrodes characterised by the material
    • C02F2001/46138—Electrodes comprising a substrate and a coating
    • C02F2001/46142—Catalytic coating
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination

Definitions

  • the invention belongs to the field of industrial sewage treatment, and in particular relates to an electrocatalytic oxidation-electrodialysis coupling treatment system and application.
  • wastewater contains many toxic pollutants that are difficult to degrade, with complex components and complex pollution characteristics, such as phenolic compounds, heterocyclic compounds, organic compounds such as polychlorinated biphenyls, and inorganic compounds such as salt and heavy metals, which will cause natural pollution.
  • complex components and complex pollution characteristics such as phenolic compounds, heterocyclic compounds, organic compounds such as polychlorinated biphenyls, and inorganic compounds such as salt and heavy metals, which will cause natural pollution.
  • the aggravation of water pollution restricts the development of social economy and science and technology.
  • the pretreatment technology for high-salt organic industrial wastewater is generally to directly concentrate and crystallize the salt by evaporation.
  • Electrocatalytic oxidation technology utilizes strongly oxidizing hydroxyl radicals [OH ⁇ ], H 2 O 2 and other organic pollutants generated on the surface of the electrode to oxidatively degrade organic pollutants, and has certain advantages in the treatment of organic industrial wastewater.
  • Electrodialysis technology is based on the selective permeability of ion exchange membrane to anions and cations. Through the action of an external electric field, the anions and cations in the water are directionally migrated, so as to realize the process of desalination.
  • electrocatalytic oxidation has a strong ability to degrade organic matter, high concentration of salt and other complex pollutants will reduce the effect of the oxidant, and easily block the active sites of the electrode surface, reducing the electrocatalytic oxidation performance, and the oxidation efficiency is limited; The capacity is limited, and a large amount of organic matter will cause fouling of the electrodialysis membrane and reduce the electrodialysis performance.
  • the combined technology of electrocatalytic oxidation and electrodialysis is mainly through a two-stage combination, which is only a single series combination, that is, electrodialysis and electrocatalytic oxidation are set as two independent units. exert its coupling synergistic effect.
  • the present invention proposes an electrocatalytic oxidation-electrodialysis coupling treatment system.
  • electrocatalytic oxidation and electrodialysis are formed. They work synergistically with each other, and simultaneously remove high-concentration inorganic salts and refractory organics.
  • the present invention proposes an electrocatalytic oxidation-electrodialysis coupled treatment system
  • the electrocatalytic oxidation-electrodialysis coupled treatment system includes at least three electrocatalytic electrodes and at least two electrodialysis membrane stacks, each Each electrodialysis membrane stack is composed of several pairs of cation exchange membranes and anion exchange membranes arranged in phases, and the three electrocatalytic electrodes include at least one electrocatalytic anode and one electrocatalytic cathode.
  • the membrane stack is arranged between two electrocatalytic electrodes, and one side of the anion exchange membrane of the electrodialysis membrane stack is adjacent to the electrocatalytic cathode, and one side of the cation exchange membrane is adjacent to the electrocatalytic anode, so that the electrocatalytic electrode is connected to the electrocatalytic anode.
  • An electrode area is formed between the electrodialysis membrane stacks, and a membrane stack desalination chamber and a membrane stack concentration chamber are formed inside the electrodialysis membrane stack.
  • the invention aims to organically combine electrocatalytic oxidation and electrodialysis technology to form an integrated unit, and the selection of electrodes in the system, the selection of cation exchange membranes of electrodialysis membrane stacks, the selection of anion exchange membrane types, and the interval between membrane stacks Parameters such as the pole frame between the plate, the electrode plate and the membrane stack can be selected and adjusted by those skilled in the art according to actual needs.
  • the electrocatalytic electrode generates strong oxidizing species in situ.
  • the electrocatalytic electrode is a titanium-based metal oxide electrode.
  • the electrocatalytic electrode is an electrocatalytic titanium-based ruthenium-iridium electrode plate or a titanium-based titanium oxide electrode plate.
  • the cation exchange membrane and the anion exchange membrane are any one of a heterogeneous membrane, a homogeneous membrane or a semi-homogeneous membrane. Antifouling type homogeneous films are preferred.
  • the present invention further proposes the application of the above-mentioned electrocatalytic oxidation-electrodialysis coupling treatment system in the simultaneous removal of high-concentration inorganic salts and refractory organics in wastewater.
  • the raw water of the wastewater to be treated enters the electrode area and the membrane stack desalination chamber at the same time, and the electrocatalytic oxidation and electrodialysis migration work together to form fresh water discharge.
  • the salty water enters the membrane stack concentration chamber, the electrode area and the membrane stack desalination chamber.
  • the inorganic salt ions enter the membrane stack concentration chamber under the action of electrodialysis to form concentrated water.
  • the concentrated water in the membrane stack concentration chamber generates a salt accumulation cycle, the concentrated water is evaporated and desalted, and the evaporated condensed water is used to supplement the salt water.
  • Brine water can be prepared by evaporative desalination condensed water and added salt.
  • the initial salt concentration of the salty water is 0.8-8 g/L
  • the prepared salt component is any one of sodium sulfate, sodium chloride, magnesium chloride or sodium sulfite.
  • conditions such as current density, voltage, time of cyclic electrolysis, flow rate of raw water of waste water, and flow rate of saline water can be selected and adjusted by those skilled in the art according to the actual situation.
  • the present invention constructs an integrated technical system of electrocatalytic oxidation-electrodialysis coupling to form an integrated unit device without adding chemicals such as acid, alkali, sodium sulfate, hydrogen peroxide or ion exchanger in the electrode area;
  • Oxidation and electrodialysis technologies complement each other's advantages.
  • Electrodialysis is used to regulate electrocatalytic oxidation and degradation of organic compounds under the condition of high concentration of salt and refractory organic compounds, so as to alleviate the blocking of electrode surface active points by high-salt pollutants, and to enhance the efficiency of electrocatalytic oxidation and degradation of organic compounds.
  • the electrodialysis performance is improved, the desalination efficiency is enhanced, and a significant coupling synergistic effect is formed, which is conducive to the efficient and simultaneous removal of high-concentration inorganic salts and refractory organics in industrial wastewater, and enhances the anti-pollution ability of electrodes and ion exchange membranes; and ,
  • the concentrated water produced by this system has a significantly lower organic concentration than industrial wastewater raw water, and a higher inorganic salt concentration than wastewater raw water, which is conducive to the subsequent evaporative desalination treatment of high-salt concentrated water.
  • Figure 1 is a schematic diagram of an integrated unit of an electrocatalytic oxidation-electrodialysis coupling treatment system
  • COD chemical oxygen demand
  • Total Salt Total Salt
  • Fig. 4 is the schematic diagram of electrodialysis treatment system unit
  • the invention proposes an electrocatalytic oxidation-electrodialysis coupling treatment system.
  • electrocatalytic oxidation-electrodialysis coupling treatment system By organically combining the electrocatalytic oxidation and electrodialysis technologies, the synergistic effect of electrocatalytic oxidation and electrodialysis is formed, and high-concentration inorganic salts and refractory degradation are simultaneously removed. organic matter.
  • the electrocatalytic oxidation-electrodialysis coupling treatment system includes at least three electrocatalytic electrodes and at least two electrodialysis membrane stacks, each electrodialysis membrane stack is composed of several pairs of cation exchange membranes and anion exchange membranes arranged alternately, three
  • the electrocatalytic electrode includes at least one electrocatalytic anode and one electrocatalytic cathode, wherein the electrocatalytic electrodes are arranged alternately in polarity, the electrodialysis membrane stack is arranged between the two electrocatalytic electrodes, and the anion exchange membrane of the electrodialysis membrane stack is One side of the membrane is adjacent to the electrocatalytic cathode, and one side of the cation exchange membrane is adjacent to the electrocatalytic anode, so that an electrode area is formed between the electrocatalytic electrode and the electrodialysis membrane stack, and a membrane stack desalination chamber is formed inside the electrodialysis membrane stack. and membrane stack enrichment chamber.
  • the raw water of the wastewater to be treated enters the electrode area and the membrane stack desalination chamber at the same time, and the electrocatalytic oxidation and electrodialysis migration work together to form fresh water discharge.
  • the salty water enters the membrane stack concentration chamber, and the electrode area and the membrane stack desalination
  • the inorganic salt ions in the room enter the membrane stack concentration chamber under the action of electrodialysis to form concentrated water.
  • the concentrated water in the membrane stack concentration chamber generates a salt accumulation cycle, the concentrated water is evaporated and desalinated, and the condensed water is used to supplement the salt water. .
  • the raw water of industrial wastewater is taken from a high-concentration pesticide production wastewater in Jiangsu, with a salt content of about 5.0% (total salt 51.5g/L, COD 20100mg/L), and a composite electrochemical combination of multiple groups of electrocatalytic electrodes and electrodialysis membrane stacks is constructed alternately.
  • the coupling technology system organically combines electrocatalytic oxidation and electrodialysis technology.
  • the number of electrocatalytic titanium-based ruthenium-iridium electrode plates is 1 anode and 2 cathodes, and the number of electrodialysis membrane stacks is 2, and each membrane stack is 20 Sheets of anti-fouling homogeneous cation exchange membranes and 20 anti-fouling homogeneous anion exchange membranes are arranged alternately, as shown in Figure 1 (the electrodialysis membrane stack is simplified to consist of two cation exchange membranes and anion exchange membranes).
  • Wastewater raw water (4L) enters the electrode area and one end of the desalination chamber of the electrodialysis membrane stack at the same time at a circulating flow rate of 120L/h, resulting in the simultaneous synergy of electrocatalytic oxidation and electrodialysis migration, and the formed fresh water is discharged from the other end.
  • the membrane stack concentration chamber 2L, the initial salt concentration is 4g/L of sodium chloride
  • the membrane stack concentration chamber 2L, the initial salt concentration is 4g/L of sodium chloride
  • the inorganic salt ions in the electrode area and the membrane stack desalination chamber enter the membrane stack for concentration under the action of electrodialysis
  • the concentrated water in the membrane stack concentration chamber produces a salt accumulation cycle
  • the concentrated water is evaporated and desalted, and the evaporated condensed water is used to supplement the salty water.
  • the electrocatalytic oxidation-electrodialysis coupling treatment system can remove 3750mg/L of organic matter in industrial wastewater, as shown in Figure 2, which is higher than the following Comparative Example 1 electrocatalysis
  • the sum of oxidation (removal amount is 702mg/L) and electrodialysis (removal amount is 1550mg/L) in Comparative Example 2 and at the same time, the total salt (Total Salt) removal rate of the electrocatalytic oxidation-electrodialysis coupling treatment system for industrial wastewater is 90.3 %, as shown in Figure 3, its removal rate is higher than the sum of the electrocatalytic oxidation of Comparative Example 1 (removal rate of 3.3%) and the electrodialysis of Comparative Example 2 (removal rate of 72.5%), achieving significant electrocatalytic oxidation and
  • the synergistic effect of electrodialysis is coupled to efficiently and synchronously remove high-concentration inorganic salts and re
  • the COD of concentrated water produced after 2 hours of reaction is only 3970mg/L, the salt content reaches 83.2g/L, the COD concentration of organic matter is significantly lower than that of industrial wastewater raw water, and the salt concentration is much higher than that of raw water, which is conducive to the subsequent evaporation of high-salt concentrated water.
  • Desalination treatment After the wastewater was repeatedly treated by this electro-composite electrochemical coupling technology for ten times (each electrolysis was 2 hours), the removal of organic matter COD and the total salt removal rate of fresh water to industrial wastewater were 3520 mg/L and 88.5%, respectively.
  • Example 1 the processing capacity decreased very little, again proving that the coupled system of electrocatalytic oxidation and electrodialysis has low damage to the electrode and to the membrane, which enhances the anti-fouling of the electrode and ion exchange membrane. ability.
  • the raw water of industrial wastewater was taken from a high-concentration pesticide production wastewater in Jiangsu, with a salt content of about 5.0% (Total Salt 51.5g/L, COD 20100mg/L), and a composite electrochemical combination of multiple groups of electrocatalytic electrodes and electrodialysis membrane stacks was constructed alternately.
  • the coupling technology system organically combines electrocatalytic oxidation and electrodialysis technology.
  • the number of electrocatalytic titanium-based ruthenium-iridium electrode plates is 2 anodes and 2 cathodes, and the number of electrodialysis membrane stacks is 3, and each membrane stack is 15 One anti-fouling type homogeneous cation exchange membrane and 15 anti-fouling type homogeneous anion exchange membranes are arranged alternately.
  • Wastewater raw water (5L) enters the electrode area and the membrane stack desalination chamber at a circulating flow rate of 150L/h, and the synergistic effect of electrocatalytic oxidation and electrodialysis migration occurs, forming fresh water discharge, salty clear water (2.5L, the initial salt concentration is chlorinated Sodium 4g/L) enters the membrane stack concentration chamber at a circulating flow rate of 150 L/h.
  • salty clear water (2.5L, the initial salt concentration is chlorinated Sodium 4g/L) enters the membrane stack concentration chamber at a circulating flow rate of 150 L/h.
  • the inorganic salt ions in the electrode area and the membrane stack desalination chamber enter the concentration chamber under the action of electrodialysis to form concentrated water.
  • the concentrated water in the membrane stack concentration chamber After the salt accumulation cycle is generated, the concentrated water is subjected to evaporative desalination treatment, and the evaporative condensed water is used to supplement the salty water.
  • the COD removal of fresh water from the electrocatalytic oxidation-electrodialysis coupling treatment system to industrial wastewater was 4630 mg/L.
  • the total salt removal rate was 92.8%, achieving a significant synergistic effect of electrocatalytic oxidation and electrodialysis coupling, and efficiently and simultaneously removing high-concentration inorganic salts and refractory organics in industrial wastewater.
  • the COD of the concentrated water produced after the reaction for 2 hours is only 4820mg/L, the salt content reaches 85.2g/L, the COD concentration of organic matter is significantly lower than that of the industrial wastewater raw water, and the salt concentration is much higher than that of the raw water, which is conducive to the subsequent evaporation of the high-salt concentrated water. Desalination treatment.
  • the raw water of industrial wastewater is taken from a high-concentration pesticide production wastewater in Jiangsu, with a salt content of about 5.0% (total salt 51.5g/L, COD 20100mg/L), and a composite electrochemical combination of multiple groups of electrocatalytic electrodes and electrodialysis membrane stacks is constructed alternately.
  • the coupling technology system organically combines electrocatalytic oxidation and electrodialysis technology.
  • the number of electrocatalytic titanium-based titania electrode plates is 2 anodes and 3 cathodes, the number of electrodialysis membrane stacks is 4, and each membrane stack is 10 anti-pollution homogeneous cation exchange membranes and 10 anti-pollution homogeneous anion exchange membranes are arranged alternately.
  • Wastewater raw water (6L) enters the electrode area and the membrane stack desalination chamber at a circulating flow rate of 135L/h, and the synergistic effect of electrocatalytic oxidation and electrodialysis migration occurs, forming fresh water discharge, salty clear water (3L, the initial salt concentration of the preparation is chlorinated Sodium 4g/L) enters the membrane stack concentration chamber at a circulating flow rate of 135 L/h.
  • the inorganic salt ions in the electrode area and the membrane stack desalination chamber enter the concentration chamber under the action of electrodialysis to form concentrated water.
  • the concentrated water in the membrane stack concentration chamber Create a salt accumulation cycle.
  • the COD removal amount of fresh water from the electrocatalytic oxidation-electrodialysis coupling treatment system to industrial wastewater was 5280 mg/L.
  • the total salt removal rate was 91.2%, achieving a significant synergistic effect of electrocatalytic oxidation and electrodialysis coupling, and efficiently and simultaneously removing high-concentration inorganic salts and refractory organics in industrial wastewater.
  • the COD of the concentrated water produced after the reaction for 2 hours is only 5390mg/L, and the salt content reaches 84.8g/L.
  • the COD concentration of organic matter is significantly lower than that of the industrial wastewater raw water, and the salt concentration is much higher than that of the raw water, which is conducive to the subsequent evaporation of the high-salt concentrated water. Desalination treatment.
  • the raw water of industrial wastewater is taken from a high-concentration pesticide production wastewater in Jiangsu, with a salt content of about 5.0% (Total Salt 51.5g/L, COD 20100mg/L). 1 anode and 2 cathodes, the wastewater raw water (4L) enters the electrode area for treatment at a circulating flow rate of 120L/h. After 2 hours of cyclic electrolysis reaction under the condition of 13V, the removal amount of COD in the industrial wastewater by the electrocatalytic oxidation system was 702 mg/L, and the removal rate of the total salt (Total Salt) of the industrial wastewater was only 3.3%.
  • the raw water of industrial wastewater is taken from a high-concentration pesticide production wastewater in Jiangsu, with a salt content of about 5.0% (Total Salt 51.5g/L, COD 20100mg/L), and an electrodialysis technology system is constructed.
  • the number of titanium-based ruthenium-iridium electrode plates is 1 anode And 1 cathode, the number of electrodialysis membrane stacks is 1, which are 40 anti-pollution homogeneous cation exchange membranes and 40 anti-pollution homogeneous anion exchange membranes.
  • Wastewater raw water (4L) enters the membrane stack desalination chamber at a circulating flow rate of 120L/h to produce electrodialysis migration, resulting in fresh water discharge.
  • Sodium sulfate containing 8g/L enters the electrode area for a separate closed-circuit cycle, and the concentrated water in the membrane stack concentration chamber produces a salt accumulation cycle.
  • the removal of organic COD from the industrial wastewater by the fresh water of the electrodialysis system was 1550 mg/L, and the removal rate of the total salt (Total Salt) of the industrial wastewater was only 72.5%.
  • the COD of concentrated water produced after the reaction for 2 hours was 22800 mg/L, and the salt content was 115.6 g/L.
  • the present invention provides an idea and method for an electrocatalytic oxidation-electrodialysis coupling treatment system.
  • the above are only the preferred embodiments of the present invention. It should be pointed out that for the technical field, without departing from the principle of the present invention, several improvements and modifications can also be made, and these improvements and modifications should also be regarded as the protection scope of the present invention. All components not specified in this embodiment can be implemented by existing technologies.

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Abstract

本发明公开一种电催化氧化-电渗析耦合处理系统，通过构建多组电催化电极和电渗析膜堆交替组合的复合电化学耦合技术体系，将电催化氧化和电渗析技术有机组合成一体，形成一体化单元，废水原水同时进入电极区和膜堆淡化室产生电催化氧化和电渗析迁移同步协同作用，形成淡水排出，含盐清水则进入膜堆浓缩室，电极区和膜堆淡化室内的无机盐离子在电渗析作用下进入到浓缩室形成浓水，膜堆浓缩室的浓水产生盐分累积循环后，浓水去蒸发脱盐处理，冷凝水用于补充到含盐清水中。本发明形成电催化氧化和电渗析相互协同作用，强化电催化氧化降解有机物效率，同时通过电催化氧化提高电渗析性能，高效同步去除工业废水中的高浓无机盐和难降解有机物。

Description

一种电催化氧化-电渗析耦合处理系统及应用 技术领域
本发明属于工业污水处理领域，具体涉及一种电催化氧化-电渗析耦合处理系统及应用。
背景技术
伴随着工业经济的持续高速发展，工业生产过程中产生了大量废水，这对环境安全造成了极大的压力。而废水中含有许多较难降解的毒性污染物，成分复杂，呈现复合污染特征，如酚类化合物，杂环类化合物，多氯联苯等有机化合物，以及盐分、重金属等无机化合物，会造成天然水体污染的加剧，制约社会经济和科技的发展。针对高含盐有机工业废水的预处理技术普遍是直接采用蒸发的方式将盐浓缩结晶出来，而在蒸发过程中这些高浓有机物和无机盐往往形成复合聚合物，导致蒸发结晶环节出现粘结、堵塞等问题。电催化氧化技术是利用电极表面产生强氧化性的羟基自由基[OH·]、H 2O 2等将有机污染物氧化降解，在处理有机工业废水方面具有一定优势。电渗析技术是基于离子交换膜对于阴阳离子的选择透过性，通过外加电场的作用，使水中的阴阳离子发生定向迁移，从而实现脱盐的过程，电渗析技术具有能量消耗低，对原水含盐量变化适应性强，易于实现机械化和自动化等优点。虽然电催化氧化降解有机物能力强，但是高浓度盐分等复合污染物会削减氧化剂效果，并易阻塞电极表面活性点，降低电催化氧化性能，氧化效能受到限制；电渗析脱盐能力强，但去除有机物能力有限，且大量有机物会造成电渗析膜污染，降低电渗析性能。目前，电催化氧化与电渗析联合技术主要是通过两段组合的方式，只是单一的串联组合，即电渗析和电催化氧化被设置为两个独立的单元，未能形成一体化单元，没有充分发挥其耦合协同效应。
发明内容
发明目的：为解决现有技术中存在的技术问题，本发明提出一种电催化氧化-电渗析耦合处理系统，通过将电催化氧化和电渗析技术有机组合成一体，形成电催化氧化和电渗析相互协同作用，并同步去除高浓无机盐和难降解有机物。
为实现上述技术目的，本发明提出了一种电催化氧化-电渗析耦合处理系统，所述电催化氧化-电渗析耦合处理系统包括至少三个电催化电极和至少两个电渗析膜堆，每 个电渗析膜堆由若干对阳离子交换膜和阴离子交换膜相间排列构成，三个电催化电极中至少包括一个电催化阳极和一个电催化阴极，其中，电催化电极按照极性相间排列，电渗析膜堆设置于两个电催化电极之间，且电渗析膜堆的阴离子交换膜的一侧与电催化阴极相邻，阳离子交换膜的一侧与电催化阳极相邻，从而在电催化电极与电渗析膜堆之间形成电极区，在电渗析膜堆内部形成膜堆淡化室和膜堆浓缩室。
本发明旨在将电催化氧化和电渗析技术有机组合成一体，形成一体化单元，而该系统中电极的选择、电渗析膜堆的阳离子交换膜、阴离子交换膜类型的选择、膜堆之间隔板、电极板和膜堆之间的极框等参数，本领域技术人员均可以根据实际需求进行选择和调整。
优选地，所述电催化电极在原位产生强氧化性物质。
在本发明的一种实施方式中，所述电催化电极为钛基金属氧化物电极。
在本发明的一种实施方式中，电催化电极为电催化钛基钌铱电极板或钛基亚氧化钛电极板。
优选地，所述阳离子交换膜和阴离子交换膜均为异相膜、均相膜或半均相膜中的任意一种。优选抗污染型均相膜。
本发明进一步提出了上述电催化氧化-电渗析耦合处理系统在同步去除废水中的高浓无机盐和难降解有机物上的应用。
具体地，将待处理废水原水同时进入电极区和膜堆淡化室，电催化氧化和电渗析迁移同步协同作用，形成淡水排出，含盐清水则进入膜堆浓缩室，电极区和膜堆淡化室内的无机盐离子在电渗析作用下进入到膜堆浓缩室形成浓水，膜堆浓缩室的浓水产生盐分累积循环后，浓水去蒸发脱盐处理，蒸发冷凝水用于补充到含盐清水中。含盐清水可以采用蒸发脱盐冷凝后的水和添加盐来配制。
含盐清水的初始盐浓度为0.8～8g/L，配制盐成分为硫酸钠、氯化钠、氯化镁或亚硫酸钠中的任意一种。
对于处理过程中，电流密度、电压、循环电解的时间、废水原水的流速、含盐清水的流速等条件可以由本领域技术人员根据实际情况进行选择和调整。
有益效果：本发明构建了电催化氧化-电渗析耦合一体化技术体系，形成一体化单元装置，无需在电极区加入酸、碱、硫酸钠、双氧水或离子交换剂等化学药剂；并将 电催化氧化和电渗析技术优势互补，通过电渗析调控高浓度盐分和难降解有机物复合污染条件下的电催化氧化降解有机物，缓解高盐分污染物阻塞电极表面活性点，强化电催化氧化降解有机物效率，同时通过电催化氧化提高电渗析性能，强化脱盐效率，形成显著的耦合协同效应，有利于高效同步去除工业废水中的高浓无机盐和难降解有机物，增强电极和离子交换膜的抗污染能力；并且，本系统产生的浓水，其有机物浓度明显低于工业废水原水，无机盐浓度则高于废水原水，有利于高盐浓水后续的蒸发脱盐处理。
附图说明
图1为电催化氧化-电渗析耦合处理系统一体化单元示意图；
图2为实施例中电催化氧化-电渗析耦合处理系统对工业废水的化学需氧量(COD)浓度随电解反应时间降解图；
图3为实施例中电催化氧化-电渗析耦合处理系统对工业废水的总盐分(Total Salt)浓度随电解反应时间降解图。
图4为电渗析处理系统单元示意图；
具体实施方式
本发明提出一种电催化氧化-电渗析耦合处理系统，通过将电催化氧化和电渗析技术有机组合成一体，形成电催化氧化和电渗析相互协同作用，并同步去除高浓无机盐和难降解有机物。
具体地，电催化氧化-电渗析耦合处理系统包括至少三个电催化电极和至少两个电渗析膜堆，每个电渗析膜堆由若干对阳离子交换膜和阴离子交换膜相间排列构成，三个电催化电极中至少包括一个电催化阳极和一个电催化阴极，其中，电催化电极按照极性相间排列，电渗析膜堆设置于两个电催化电极之间，且电渗析膜堆的阴离子交换膜的一侧与电催化阴极相邻，阳离子交换膜的一侧与电催化阳极相邻，从而在电催化电极与电渗析膜堆之间形成电极区，在电渗析膜堆内部形成膜堆淡化室和膜堆浓缩室。
在处理时，将待处理废水原水同时进入电极区和膜堆淡化室，电催化氧化和电渗析迁移同步协同作用，形成淡水排出，含盐清水则进入膜堆浓缩室，电极区和膜堆淡化室内的无机盐离子在电渗析作用下进入到膜堆浓缩室形成浓水，膜堆浓缩室的浓水产生盐分累积循环后，浓水去蒸发脱盐处理，冷凝水用于补充到含盐清水中。
下面结合具体实施例对本发明做进一步详细说明。给出了详细的实施方式和具体的操作过程，实施例将有助于理解本发明，但是本发明的保护范围不限于下述的实施例。下述实施例中，电流密度、电压、循环电解的时间、废水原水的流速、含盐清水的流速等条件仅为一种实施方式，各项参数可以由本领域技术人员根据实际情况进行选择和调整。
实施例1
工业废水原水取自江苏某农药高浓度生产废水，含盐量约5.0％(总盐51.5g/L，COD 20100mg/L)，构建多组电催化电极和电渗析膜堆交替组合的复合电化学耦合技术体系，将电催化氧化和电渗析技术有机组合成一体，电催化钛基钌铱电极板数量为1块阳极和2块阴极，电渗析膜堆数量为2个，每个膜堆为20片抗污染型均相阳离子交换膜和20片抗污染型均相阴离子交换膜相间排列，见图1所示(其中电渗析膜堆为简化为由两片阳离子交换膜和阴离子交换膜构成)。废水原水(4L)以120L/h的循环流速同时进入电极区和电渗析膜堆的淡化室的一端，产生电催化氧化和电渗析迁移同步协同作用，形成的淡水自另一端排出，含盐清水(2L，初始的盐浓度为氯化钠4g/L)则以120L/h的循环流速进入膜堆浓缩室，电极区和膜堆淡化室内的无机盐离子在电渗析作用下进入到膜堆浓缩室形成浓水，膜堆浓缩室的浓水产生盐分累积循环后，浓水去蒸发脱盐处理，蒸发冷凝水用于补充到含盐清水中。13V条件下循环电解反应2小时后，电催化氧化-电渗析耦合处理系统对工业废水有机物COD的去除量为3750mg/L，见图2所示，其去除量高于下述对比例1电催化氧化(去除量702mg/L)和对比例2电渗析(去除量为1550mg/L)之和，同时，电催化氧化-电渗析耦合处理系统对工业废水的总盐分(Total Salt)去除率为90.3％，见图3所示，其去除率高于对比例1电催化氧化(去除率为3.3％)和对比例2电渗析(去除率为72.5％)之和，实现了显著的电催化氧化和电渗析耦合协同效应，高效同步去除工业废水中的高浓无机盐和难降解有机物。并且，反应2小时后产生的浓水COD仅为3970mg/L，盐分达到83.2g/L，有机物COD浓度明显低于工业废水原水，盐分浓度大大高于原水，有利于高盐浓水后续的蒸发脱盐处理。采用本电复合电化学耦合技术反复处理此废水十次(每次电解2小时)后，淡水对工业废水有机物COD的去除量和总盐分的去除率分别为3520mg/L和88.5％，相比对比例1和对比例2，其处理能力下降得很少，再次证明了电催化氧化和电渗析耦 合体系，对电极的损伤和对膜的损伤都很低，增强了电极和离子交换膜的抗污染能力。
实施例2
工业废水原水取自江苏某农药高浓度生产废水，含盐量约5.0％(Total Salt 51.5g/L，COD 20100mg/L)，构建多组电催化电极和电渗析膜堆交替组合的复合电化学耦合技术体系，将电催化氧化和电渗析技术有机组合成一体，电催化钛基钌铱电极板数量为2块阳极和2块阴极，电渗析膜堆数量为3个，每个膜堆为15片抗污染型均相阳离子交换膜和15片抗污染型均相阴离子交换膜相间排列。废水原水(5L)以150L/h的循环流速进入电极区和膜堆淡化室产生电催化氧化和电渗析迁移同步协同作用，形成淡水排出，含盐清水(2.5L，初始的盐浓度为氯化钠4g/L)则以150L/h的循环流速进入膜堆浓缩室，电极区和膜堆淡化室内的无机盐离子在电渗析作用下进入到浓缩室形成浓水，膜堆浓缩室的浓水产生盐分累积循环后，浓水去蒸发脱盐处理，蒸发冷凝水用于补充到含盐清水中。13V条件下循环电解反应2小时后，电催化氧化-电渗析耦合处理系统淡水对工业废水有机物COD的去除量为4630mg/L，同时，电催化氧化-电渗析耦合处理系统淡水对工业废水的总盐分(Total Salt)去除率为92.8％，实现了显著的电催化氧化和电渗析耦合协同效应，高效同步去除工业废水中的高浓无机盐和难降解有机物。并且，反应2小时后产生的浓水COD仅为4820mg/L，盐分达到85.2g/L，有机物COD浓度明显低于工业废水原水，盐分浓度大大高于原水，有利于高盐浓水后续的蒸发脱盐处理。
实施例3
工业废水原水取自江苏某农药高浓度生产废水，含盐量约5.0％(总盐51.5g/L，COD 20100mg/L)，构建多组电催化电极和电渗析膜堆交替组合的复合电化学耦合技术体系，将电催化氧化和电渗析技术有机组合成一体，电催化钛基亚氧化钛电极板数量为2块阳极和3块阴极，电渗析膜堆数量为4个，每个膜堆为10片抗污染型均相阳离子交换膜和10片抗污染型均相阴离子交换膜相间排列。废水原水(6L)以135L/h的循环流速进入电极区和膜堆淡化室产生电催化氧化和电渗析迁移同步协同作用，形成淡水排出，含盐清水(3L，配制的初始盐浓度为氯化钠4g/L)则以135L/h的循环流速进入膜堆浓缩室，电极区和膜堆淡化室内的无机盐离子在电渗析作用下进入到浓缩室形成浓水，膜堆浓缩室的浓水产生盐分累积循环。13V条件下循环电解反应2小时后， 电催化氧化-电渗析耦合处理系统淡水对工业废水有机物COD的去除量为5280mg/L，同时，电催化氧化-电渗析耦合处理系统淡水对工业废水的总盐分(Total Salt)去除率为91.2％，实现了显著的电催化氧化和电渗析耦合协同效应，高效同步去除工业废水中的高浓无机盐和难降解有机物。并且，反应2小时后产生的浓水COD仅为5390mg/L，盐分达到84.8g/L，有机物COD浓度明显低于工业废水原水，盐分浓度大大高于原水，有利于高盐浓水后续的蒸发脱盐处理。
对比例1
工业废水原水取自江苏某农药高浓度生产废水，含盐量约5.0％(Total Salt 51.5g/L，COD 20100mg/L)，构建电催化氧化技术体系，电催化钛基钌铱电极板数量为1块阳极和2块阴极，废水原水(4L)以120L/h的循环流速进入电极区处理。13V条件下循环电解反应2小时后，电催化氧化系统对工业废水有机物COD的去除量为702mg/L，对工业废水的总盐分(Total Salt)去除率仅为3.3％。采用本电催化氧化体系反复处理此废水十次(每次电解2小时)后，对工业废水有机物COD的去除量仅为320mg/L，对工业废水的总盐分(Total Salt)去除率仅为1.7％，电极性能大大降低。
对比例2
工业废水原水取自江苏某农药高浓度生产废水，含盐量约5.0％(Total Salt 51.5g/L，COD 20100mg/L)，构建电渗析技术体系，钛基钌铱电极板数量为1块阳极和1块阴极，电渗析膜堆数量为1个，为40片抗污染型均相阳离子交换膜和40片抗污染型均相阴离子交换膜相间排列。废水原水(4L)以120L/h的循环流速进入膜堆淡化室产生电渗析迁移作用，形成淡水排出，一部废水原水(2L)则以120L/的循环流速进入膜堆浓缩室，极水(含硫酸钠8g/L)则进入电极区单独闭路循环，膜堆浓缩室的浓水产生盐分累积循环。13V条件下循环电解反应2小时后，电渗析系统淡水对工业废水有机物COD的去除量为1550mg/L，对工业废水的总盐分(Total Salt)去除率仅为72.5％。反应2小时后产生的浓水COD为22800mg/L，盐分为115.6g/L。采用本电渗析技术体系反复处理此废水十次(每次电解2小时)后，淡水对工业废水有机物COD的去除量仅为620mg/L，对工业废水的总盐分(Total Salt)去除率仅为39.6％，膜性能大大降低。
本发明提供了一种电催化氧化-电渗析耦合处理系统的思路及方法，具体实现该技术方案的方法和途径很多，以上所述仅是本发明的优选实施方式，应当指出，对于本 技术领域的普通技术人员来说，在不脱离本发明原理的前提下，还可以做出若干改进和润饰，这些改进和润饰也应视为本发明的保护范围。本实施例中未明确的各组成部分均可用现有技术加以实现。

Claims (8)

  1. 一种电催化氧化-电渗析耦合处理系统，其特征在于，所述电催化氧化-电渗析耦合处理系统包括至少三个电催化电极和至少两个电渗析膜堆，每个电渗析膜堆由若干对阳离子交换膜和阴离子交换膜相间排列构成，三个电催化电极中至少包括一个电催化阳极和一个电催化阴极，其中，电催化电极按照极性相间排列，每个电渗析膜堆设置于两个电催化电极之间，且电渗析膜堆的阴离子交换膜的一侧与电催化阴极相邻，阳离子交换膜的一侧与电催化阳极相邻，在电催化电极与电渗析膜堆之间构成电极区，在电渗析膜堆内部自靠近电催化电极侧依次构成相间的膜堆浓缩室和膜堆淡化室。
  2. 根据权利要求1所述的电催化氧化-电渗析耦合处理系统，其特征在于，所述电催化电极在原位产生强氧化性物质。
  3. 根据权利要求2所述的电催化氧化-电渗析耦合处理系统，其特征在于，所述电催化电极为钛基金属氧化物电极。
  4. 根据权利要求3所述的电催化氧化-电渗析耦合处理系统，其特征在于，所述电催化电极为电催化钛基钌铱电极板或钛基亚氧化钛电极板。
  5. 根据权利要求1所述的电催化氧化-电渗析耦合处理系统，其特征在于，所述阳离子交换膜和阴离子交换膜均为异相膜、均相膜或半均相膜中的任意一种。
  6. 权利要求1所述的电催化氧化-电渗析耦合处理系统在同步去除废水中的高浓无机盐和难降解有机物上的应用。
  7. 根据权利要求6所述的应用，其特征在于，将待处理废水原水同时通入电极区和膜堆淡化室的一端，经电催化氧化和电渗析迁移同步协同作用，形成的淡水自电极区和膜堆淡化室的另一端排出，另外将含盐清水通入膜堆浓缩室，电极区和膜堆淡化室内的无机盐离子在电渗析作用下进入到膜堆浓缩室形成浓水，浓水产生盐分累积循环后，浓水去蒸发脱盐处理，蒸发冷凝水用于补充到含盐清水中。
  8. 根据权利要求7所述的应用，其特征在于，含盐清水的初始盐浓度为0.8～8g/L，配制盐成分为硫酸钠、氯化钠、氯化镁或亚硫酸钠中的任意一种。
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CN114230441A (zh) * 2021-11-26 2022-03-25 南通百川新材料有限公司 一种三羟甲基丙烷中甲酸钠的电渗析膜分离方法
CN114212859B (zh) * 2021-12-10 2023-11-03 国家能源投资集团有限责任公司 一种两段电化学交联电渗析脱盐处理系统及其应用
CN114751492B (zh) * 2022-04-21 2024-03-19 中国科学院生态环境研究中心 一种大通量选择性目标去除电渗析设备与方法
CN115020757A (zh) * 2022-06-09 2022-09-06 四川星明能源环保科技有限公司 一种基于电渗析的强酸性钒溶液中有机物去除方法
CN115140811A (zh) * 2022-06-30 2022-10-04 温州大学 一种电渗析海水脱盐协同电催化降解有机污水并产h2o2装置
CN116401905B (zh) * 2023-02-10 2024-02-06 华能湖北新能源有限责任公司 基于电渗析效率提升的结构优化方法及装置

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104341029A (zh) * 2014-11-28 2015-02-11 陕西科技大学 电去离子电催化一体反应器及去除硝酸盐的方法
JP2015123401A (ja) * 2013-12-26 2015-07-06 栗田工業株式会社 水回収方法及び装置
CN205204884U (zh) * 2015-11-27 2016-05-04 福建创源环保有限公司 一种处理高盐工业废水的多电极多隔膜电解槽
CN205838763U (zh) * 2016-07-25 2016-12-28 大连佳瑞环保科技有限公司 一种循环冷却水处理装置
CN206337064U (zh) * 2016-12-21 2017-07-18 新疆融通利和水处理技术有限公司 一种带有中间极板的电渗析水处理装置

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105236527B (zh) * 2015-10-30 2017-08-04 中山大学 一种废水同步连续脱盐除有机污染物的三维电极装置及方法
CN107129011B (zh) * 2017-04-13 2020-12-15 西安优瑞卡环保科技有限公司 一种电解—离子膜耦合处理高氯盐有机废水的装置及方法
CN112209540A (zh) * 2020-08-28 2021-01-12 浙江工业大学 一种高盐高cod废水的零排放耦合工艺

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2015123401A (ja) * 2013-12-26 2015-07-06 栗田工業株式会社 水回収方法及び装置
CN104341029A (zh) * 2014-11-28 2015-02-11 陕西科技大学 电去离子电催化一体反应器及去除硝酸盐的方法
CN205204884U (zh) * 2015-11-27 2016-05-04 福建创源环保有限公司 一种处理高盐工业废水的多电极多隔膜电解槽
CN205838763U (zh) * 2016-07-25 2016-12-28 大连佳瑞环保科技有限公司 一种循环冷却水处理装置
CN206337064U (zh) * 2016-12-21 2017-07-18 新疆融通利和水处理技术有限公司 一种带有中间极板的电渗析水处理装置

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