WO2017124798A1 - 一种适用于污水脱盐回用的复合膜分离方法 - Google Patents

一种适用于污水脱盐回用的复合膜分离方法 Download PDF

Info

Publication number
WO2017124798A1
WO2017124798A1 PCT/CN2016/103464 CN2016103464W WO2017124798A1 WO 2017124798 A1 WO2017124798 A1 WO 2017124798A1 CN 2016103464 W CN2016103464 W CN 2016103464W WO 2017124798 A1 WO2017124798 A1 WO 2017124798A1
Authority
WO
WIPO (PCT)
Prior art keywords
composite membrane
membrane
cathode
anode
water
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/CN2016/103464
Other languages
English (en)
French (fr)
Inventor
王志伟
李子梦
于鸿光
马金星
吴志超
郑君健
王雪野
潘辰
王巧英
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Tongji University
Original Assignee
Tongji University
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Tongji University filed Critical Tongji University
Priority to JP2018537775A priority Critical patent/JP6583868B2/ja
Priority to AU2016388020A priority patent/AU2016388020B2/en
Publication of WO2017124798A1 publication Critical patent/WO2017124798A1/zh
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Images

Classifications

    • 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
    • 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
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/46—Apparatus for electrochemical processes
    • 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
    • Y02A20/131—Reverse-osmosis

Definitions

  • the invention relates to a composite membrane separation method suitable for desalination and reuse of sewage.
  • the membrane filtration and electrosorption coupling principle are used to remove ions in the sewage and improve the quality of the effluent water, which belongs to the field of sewage (waste) water treatment.
  • electrosorption technology has received extensive attention due to its unique advantages in terms of removal efficiency and energy consumption.
  • the electro-adsorption technology can remove polluting ions and realize sewage purification.
  • electrosorption technology has the characteristics of simple operation and maintenance, long equipment life, low energy consumption, no secondary pollution, and good removal effect on dissolved pollutants.
  • conventional electrosorption processes are more sensitive to particulate contaminants.
  • the introduction of particulate matter not only reduces the desalination effect, but also blocks the electrodes, increasing the maintenance cost of the equipment. Therefore, in the treatment of salty wastewater containing particulate pollutants, it is usually necessary to set a pretreatment process at the front end of the electrosorption process to intercept particulate matter, increasing the footprint and equipment cost of the electrosorption process. And the operation steps.
  • the membrane separation method is widely used in the field of sewage treatment due to its excellent solid-liquid separation effect.
  • Membrane separation technology is an effective means to effectively solve the problem of particulate pollutant pollution in electrosorption process.
  • the most important problem in limiting the development of membrane separation process is membrane fouling.
  • By applying a DC electric field the surface of the membrane is negatively charged, and the negatively charged particulate contaminants in the sewage are repelled, thereby controlling membrane fouling.
  • a new conductive composite membrane electrosorption desalination process is formed, which can simultaneously realize particle interception and ion removal, and can expand new ideas for the treatment of salty wastewater.
  • Zhang Hongtao a membrane-electrosorption device for desalination systems
  • invention patent publication CN103693718A uses an ion exchange membrane combined with an electrosorption process to desalinate wastewater, which increases the cation exchange membrane.
  • the purpose of the anion exchange membrane is to increase the selective permeability of the cation and the anion, respectively, and the ion exchange membrane does not have the function of sewage filtration; secondly, the system still cannot solve the damage of the particulate pollutant to the device itself, and the ion exchange membrane has a high cost. , running and maintenance is more troublesome.
  • the invention combines membrane separation and electrosorption, and at the same time realizes the function of filtering and separating sewage and removing ions by electrosorption, which can effectively intercept the particulate matter in the sewage, avoid damage to the adsorbent material, and simultaneously remove polluting ions in the sewage, Avoid secondary pollution, save energy and reduce cost.
  • the object of the present invention is to provide a membrane separation technology capable of simultaneously realizing solid-liquid separation and desalination in sewage treatment, which combines membrane separation and electrosorption processes, and simultaneously realizes filtration separation and electrosorption of ions by sewage.
  • the function can effectively retain particulate matter, adsorb ionic pollutants in wastewater, improve desalination effect, no secondary pollution, simple operation, low energy consumption, and is suitable for treatment of low concentration saline wastewater.
  • the invention provides a composite membrane separation method suitable for desalination of sewage, wherein the separation method uses a conductive composite membrane reactor to realize desalination of sewage, and the conductive composite membrane reactor is made of water.
  • System 1, power system 2, membrane reactor 3, water outlet control system 4 and clear water tank 5 the water inlet system 1 is composed of a water inlet and an inflow water flow regulating device, and the inflow water flow rate is adjusted according to the process requirements, and the influent flow rate adjusting device
  • the water outlet of the inlet tank is connected to the membrane reactor through a pipeline.
  • the membrane reactor is composed of a reaction tank, a composite membrane module 6 and a stirring system, and a plurality of composite membrane modules 6 in the reaction tank are respectively passed.
  • the conductive wire 7 having good electrical conductivity is connected to the positive and negative electrodes of the power supply system 2.
  • the membrane reactor adopts a submerged arrangement, the agitator is disposed in the reaction tank, the reaction liquid in the reaction tank is uniformly mixed, and the outlet of the reaction tank of the membrane reactor is connected to the water outlet system through a pipeline;
  • Each of the composite membrane modules is a flat membrane structure composed of a cathode composite membrane 8, an anode composite membrane 9 and a separator layer 10, wherein the cathode composite membrane is formed by bonding a cathode electrode 11 and a cathode current collector 12 through a polymer material, and an anode The composite film is formed by bonding the anode electrode 13 and the anode current collector 14 through a polymer material, the cathode composite film 8 and the anode composite film 9 being separated by a separator layer 10 to prevent short circuit; the cathode current collector is located at the water inlet On one side, the anode current collector is located on the side of the water outlet, that is, the influent water first flows through the cathode current collector and the cathode electrode, passes through the separation layer, passes through the anode electrode and the anode current collector, and discharges the conductive composite membrane reactor in the form of membrane water;
  • the influent water that meets the process requirements is connected into the pool, and the influent flow rate is adjusted by the influent flow regulating device.
  • the effluent from the inlet tank enters the membrane reactor and is operated by constant current or constant pressure, and the influent flows first through the cathode current collector.
  • the cathode electrode, through the separation layer, and then through the anode electrode and the anode current collector discharges the conductive composite membrane reactor in the form of membrane water, and controls the membrane flux range of 8 to 50 L/(m 2 h), and the transmembrane pressure difference range is 0.4. ⁇ 20kPa, turn on the power, start the membrane reactor, and adsorb the ionic pollutants in the salty wastewater.
  • the influent concentration of the control inlet tank is less than 5000 mg/L (in terms of TDS).
  • the applied DC voltage ranges from 0.4 to 2.0V.
  • the power supply system is powered by the regulated DC power supply for the electric adsorption process
  • the cathode composite film is connected to the negative pole of the power supply
  • the anode composite film is connected to the positive pole of the power supply
  • the current monitoring device is arranged in the circuit connecting the power supply system with the cathode or the anode, and the current condition is monitored in real time.
  • the current collector is made of a mesh-like material having good conductivity
  • the material is any one of titanium, titanium alloy material or stainless steel material
  • the electrode is made of carbon-based material, which is carbon cloth, carbon nanotube, activated carbon powder.
  • the high molecular polymer is specifically any one of polyvinylidene fluoride, polyether sulfone, polytetrafluoroethylene or polyacrylonitrile.
  • the separation layer is made of a material having good water permeability, specifically one of a nylon mesh, a nonwoven fabric or a polypropylene material.
  • the cathode composite film and the anode composite film may employ different electrode materials and current collector materials.
  • the principle of the invention is: adopting the form of a flat membrane electrode, a coupling membrane separation and an electrosorption process, and the separation layer intercepts the particulate pollutant under a suitable membrane flux to realize solid-liquid separation of the sewage, and is applied at the yin and yang electrodes.
  • the suitable voltage absorbs the ionic pollutants in the sewage to achieve the purpose of desalination of the sewage.
  • the electrode is saturated, the electrode is regenerated by shorting the external power supply and deactivating the electrode.
  • membrane module reuse can be achieved, reducing operating costs.
  • the present invention has the following advantages:
  • the invention adopts the membrane module form of the flat membrane, the technical method of coupling membrane separation and electrosorption, can adsorb the ionic pollutants while solid-liquid separation, and breaks through the limitations of the existing membrane separation and electrosorption processes. Sexuality, enhance the desalination effect, the technology has low energy consumption and convenient operation and management.
  • the outer side of the conductive composite film of the present invention has the function of trapping the particulate matter, reduces the ineffective adsorption and reduces the wear of the inner adsorbent material, and realizes the recycling of the adsorbent material through the "adsorption-desorption" process, thereby improving the electrode material. Use efficiency and reduce equipment maintenance costs.
  • FIG. 1 is a schematic view of a desalination process of coupling membrane separation and electrosorption technology
  • the label is: 1 is the water inlet system, 2 is the power supply system, 3 is the membrane reactor, 4 is the water outlet control system, 5 is the clear water tank, 6 is the composite membrane module, 7 is the wire, 8 is the cathode composite film, 9 is The anode composite film, 10 is a separator layer.
  • FIG. 2 is a schematic view showing the detailed configuration of a monolithic film composite membrane module
  • the number is 7 for the wire, 8 for the cathode composite film, 9 for the anode composite film, and 10 for the separation.
  • Layer, 11 is a cathode current collector, 12 is a cathode electrode, 13 is an anode electrode, and 14 is an anode current collector.
  • the water inlet system 1 is composed of a water inlet tank and an influent flow regulating device, and the saline-based brackish water which has been pretreated according to the process requirements is inserted into the pool, and the influent water contains salt.
  • the amount is 1200 mg/L (in terms of TDS), and the influent flow rate is adjusted to control the flux to be 10 L/m 2 h.
  • the water outlet of the inlet tank is connected to the membrane reactor through a pipeline, and the effluent from the inlet tank enters the membrane reactor.
  • the membrane reactor is composed of a reaction tank, a composite membrane module 6 and a stirring system, and the composite membrane module shown in Fig.
  • the anode composite film is bonded by a titanium mesh and a carbon cloth through PVDF
  • the cathode composite film is bonded by a stainless steel wire mesh and a carbon cloth through PVDF
  • the separator layer is a nonwoven fabric.
  • the cathode composite membrane module is connected to the negative pole of the power supply system 2 through the conductive wire 7 with good electrical conductivity
  • the anode composite membrane is connected to the positive pole of the power source through the wire
  • the membrane reactor is arranged in a submerged manner
  • the agitator is disposed in the reaction tank to make the reaction tank
  • the reaction solution was uniformly mixed and operated in a constant flow mode.
  • the power is turned on, the operating voltage is 2.0V, the membrane reactor is started, the hydraulic retention time is 1h, the operation is 6h, and the transmembrane pressure difference is stable at 0.7kPa during the operation.
  • the reaction tank outlet of the membrane reactor is connected to the water outlet system through the pipeline.
  • the water flow rate is adjusted by the water discharge control system 4, and the system has a salt rejection rate of 65-72%.
  • the water inlet system 1 is composed of a water inlet and an influent flow regulating device, and the biologically treated effluent of the cold-rolled wastewater which has been pretreated according to the process requirements is connected into the pool, and the salt content of the influent water is It was 1000 mg/L (in terms of TDS), the suspended solid concentration was 50 mg/L, and the influent flow rate was adjusted to control the flux to be 40 L/m 2 h.
  • the water outlet of the inlet tank is connected to the membrane reactor through a pipeline, and the effluent from the inlet tank enters the membrane reactor.
  • the membrane reactor is composed of a reaction tank, a composite membrane module 6 and a stirring system, and the composite membrane module shown in Fig.
  • the cathode composite membrane module is connected to the negative pole of the power supply system 2 through the conductive wire 7 with good electrical conductivity, the anode composite membrane is connected to the positive pole of the power source through the wire, the membrane reactor is arranged in a submerged manner, and the agitator is disposed in the reaction tank to make the reaction tank
  • the reaction solution was uniformly mixed and operated in a constant flow mode.
  • the operating voltage is 1.6V
  • start the membrane reactor the hydraulic retention time is 15min
  • run for 4h the transmembrane pressure difference is stable at 2.3kPa during the operation
  • the reaction tank outlet of the membrane reactor is connected to the water outlet system through the pipeline.
  • the water flow rate is adjusted by the water discharge control system 4, the system salt rejection rate is 60-70%, and the suspended solid concentration of the effluent water is lower than the detection limit.
  • the water inlet system 1 is composed of a water inlet tank and an influent flow regulating device, and a certain nitrate-based chemical fertilizer production industrial wastewater which has undergone pretreatment according to the process requirements is inserted into the pool.
  • the water content of the salt is 900 mg/L (in terms of TDS), and the influent flow rate is adjusted to control the flux to be 10 L/m 2 h.
  • the water outlet of the inlet tank is connected to the membrane reactor through a pipeline, and the effluent from the inlet tank enters the membrane reactor.
  • the membrane reactor is composed of a reaction tank, a composite membrane module 6 and a stirring system, and the composite membrane module shown in Fig.
  • the anode composite membrane and the cathode composite membrane are composed of a titanium mesh and a carbon nanotube, and the separation layer is a nylon mesh.
  • the cathode composite membrane module is connected to the negative electrode of the power supply system 2 through the conductive wire 7 with good conductivity, and the anode composite film passes through the wire and the positive electrode of the power supply.
  • the membrane reactor adopts a submerged arrangement, and the agitator is disposed in the reaction tank to uniformly mix the reaction liquid in the reaction tank and operate in a constant current mode.
  • the power is turned on, the operating voltage is 2.0V, the membrane reactor is started, the hydraulic retention time is 1h, the operation is 4h, and the transmembrane pressure difference is stabilized at 2.4kPa during the operation.
  • the reaction tank outlet of the membrane reactor is connected to the water outlet system through the pipeline.
  • the water flow rate is adjusted by the water discharge control system 4, and the system has a salt rejection rate of 57-68%.
  • the water inlet system 1 is composed of a water inlet and an influent flow regulating device, and a certain copper-containing wastewater which has been pretreated according to the process requirements is connected into the pool, and the influent salt content is 500 mg/ L (in terms of TDS), the influent flow rate is adjusted, and the control flux is 25 L/m 2 h.
  • the water outlet of the inlet tank is connected to the membrane reactor through a pipeline, and the effluent from the inlet tank enters the membrane reactor.
  • the membrane reactor is composed of a reaction tank, a composite membrane module 6 and a stirring system, and the composite membrane module shown in Fig.
  • the anode composite membrane and the cathode composite membrane are composed of a titanium mesh and a carbon nanotube, and the separation layer is a nylon mesh.
  • the cathode composite membrane module is connected to the negative electrode of the power supply system 2 through the conductive wire 7 with good conductivity, and the anode composite film passes through the wire and the positive electrode of the power supply.
  • the membrane reactor adopts a submerged arrangement, and the agitator is disposed in the reaction tank to uniformly mix the reaction liquid in the reaction tank and operate in a constant current mode.
  • the operating voltage is 1.6V
  • start the membrane reactor the hydraulic retention time is 24min
  • run for 3h the transmembrane pressure difference during operation is stable at 1.5kPa
  • the reaction tank outlet of the membrane reactor is connected to the water outlet system through the pipeline.
  • the water flow rate is adjusted by the water discharge control system 4, and the system has a salt rejection rate of 45-58%.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Hydrology & Water Resources (AREA)
  • Health & Medical Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Molecular Biology (AREA)
  • Electrochemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

一种适用于污水脱盐回用的复合膜分离方法，该方法通过导电复合膜反应器的过滤及吸附作用实现污水脱盐，导电复合膜反应器由进水系统(1)、电源系统(2)、膜反应器(3)、出水控制系统(4)和清水池(5)组成；膜反应器(3)由反应池、复合膜组件(6)和搅拌系统组成；复合膜组件(6)为平板膜结构，由阴极复合膜(8)、阳极复合膜(9)和分隔层(10)组成，其中：阴极复合膜(8)由阴极电极(12)和阴极集流体(11)通过聚合物材料粘合而成，阳极复合膜(9)由阳极电极(13)和阳极集流体(14)通过聚合物材料粘合而成，阴极复合膜(8)和阳极复合膜(9)通过分隔层(10)隔开，以防止短路；阴极集流体(11)位于进水口一侧，阳极集流体(14)位于出水口一侧，进水先流经阴极集流体(11)和阴极电极(12)，经过分隔层(10)，再通过阳极电极(13)和阳极集流体(14)，以膜出水的形式排出导电复合膜反应器。

Description

一种适用于污水脱盐回用的复合膜分离方法 技术领域
本项发明涉及一种适用于污水脱盐回用的复合膜分离方法，运用膜过滤与电吸附耦合原理去除污水中的离子，提高出水水质，属于污(废)水处理领域。
背景技术
随着社会经济的高速发展，环境形势也愈发严峻，在众多环境问题中，水资源短缺日益严重，已经成了制约社会经济可持续发展的重大瓶颈问题。在此形势下，仅仅提倡节约用水也已不足以满足当前的用水需求，亟待进行非常规水源的开发利用，例如苦咸水的淡化、工业废水循环利用以及市政废水深度处理回用等，但某些农村地区的地下水，沿海城市混合海水的生活污水，以及化工、印染、食品加工等行业的工业废水中，均含有较高浓度的离子，例如Cl-、NO3 -、SO4 2-以及各种金属离子等，其处理不当可能会引起严重的水体污染问题。此外，重金属离子一旦进入水体，会影响居民生活饮用水安全，危害人体健康，比如铅会诱发贫血症，汞的富集可引发水俣病，镉可导致骨痛病，铜摄入过量会损害肝脏，而砷的化合物剧毒，有致癌作用。因此要实现对这些非常规水源的利用，还需要对其进行脱盐处理，以达到高标准排放或有效回用的目的，成为当前的研究热点之一。
近年来电吸附技术凭借其在去除效果和能耗等方面的独特的优势，受到了广泛的关注。通过外加低电压直流供电，电吸附技术可以去除污染性离子，实现污水净化。与其他水处理技术相比，电吸附技术具有操作维护简便、设备寿命长、能耗低、无二次污染等特点，对溶解性污染物具有良好的去除效果。然而，传统的电吸附工艺对颗粒态的污染物较为敏感。颗粒物的引入不仅降低了脱盐效果，而且堵塞电极，增加了设备维护成本。因此，在处理含有颗粒污染物的含盐废水中，通常需要在电吸附工艺前端设置预处理流程以拦截颗粒物，增加了电吸附工艺的占地面积、设备成本 及操作步骤。
另一方面，膜分离方法由于其优良的固液分离效果而广泛应用于污水处理领域。膜分离技术是有效解决电吸附工艺中的颗粒污染物污染问题的有效手段。限制膜分离工艺发展的最主要问题是膜污染，通过外加直流电场，使膜表面带负电荷，排斥污水中同带负电荷的颗粒污染物，从而起到控制膜污染的作用。通过耦合电吸附与膜分离工艺，形成新型导电复合膜电吸附脱盐工艺，可以同步实现颗粒物拦截与离子脱除，可以为含盐废水的处理拓展新思路。然而，现有的研究成果以及文献报道主要集中于电吸附工艺的优化，且国内专利中涉及脱盐的成果也都集中在膜分离和电吸附单独运行的工况，如木内崇文(膜分离装置以及膜分离方法，发明专利公布号CN103052437A)，常铮(一种通过电吸附技术从工业废水中选择性去除Fe2+和/或Fe3+的方法，发明专利公布号CN104609518A)，关于膜分离和电吸附耦合的工艺却鲜有报道。为数不多的将二者结合的工艺，如张鸿涛(一种用于脱盐系统的膜-电吸附装置，发明专利公布号CN103693718A)运用离子交换膜结合电吸附工艺对废水脱盐，其增加阳离子交换膜和阴离子交换膜的目的是分别增加阳离子与阴离子的选择透过性，离子交换膜不起污水过滤作用；其次，该系统依旧无法解决颗粒污染物对装置本身的损害，且离子交换膜成本较高，运行维护较为麻烦。
本发明将膜分离与电吸附结合，同时实现污水的过滤分离与电吸附脱除离子的功能，可有效截留污水中的颗粒物，避免其对吸附材料的损害，同时去除污水中的污染性离子，避免二次污染，节省能耗，降低造价。
发明内容
本发明的目的在于提供一种在污水处理中能将固液分离与脱盐功能同时实现的膜分离技术，该技术方法耦合膜分离与电吸附工艺，同时实现污水的过滤分离与电吸附脱除离子的功能，可有效截留颗粒物，吸附废水中的离子型污染物，提高脱盐的效果，无二次污染，且操作简便，能耗较低，适用于低浓度的含盐废水的处理。
本发明提出的一种适用于污水脱盐回用的复合膜分离方法，所述分离方法采用导电复合膜反应器实现污水脱盐，所述导电复合膜反应器由进水 系统1、电源系统2、膜反应器3、出水控制系统4和清水池5组成，进水系统1由进水池和进水流量调节装置组成，根据工艺要求调节进水流量，进水流量调节装置设置于进水池的进水口，进水池的出水口通过管道与膜反应器连接，膜反应器由反应池、复合膜组件6和搅拌系统组成，位于反应池中的若干片复合膜组件6分别通过导电性能良好的导线7与电源系统2的正负极相连。膜反应器采用浸没式的布置方式，搅拌器设置于反应池内，使反应池内的反应液混合均匀，膜反应器的反应池出水口通过管道与出水系统连接；
每组复合膜组件为平板膜结构，由阴极复合膜8、阳极复合膜9和分隔层10组成，其中：阴极复合膜由阴极电极11和阴极集流体12通过聚合物材料粘合而成，阳极复合膜由阳极电极13和阳极集流体14通过聚合物材料粘合而成，所述阴极复合膜8和阳极复合膜9通过分隔层10隔开，以防止短路；所述阴极集流体位于进水口一侧，阳极集流体位于出水口一侧，即进水先流经阴极集流体和阴极电极，经过分隔层，再通过阳极电极和阳极集流体，以膜出水的形式排出导电复合膜反应器；
具体步骤如下：
将符合工艺要求的进水接入进水池，通过进水流量调节装置调节进水流量，进水池的出水进入膜反应器，采用恒流或恒压的方式运行，进水先流经阴极集流体和阴极电极，经过分隔层，再通过阳极电极和阳极集流体，以膜出水的形式排出导电复合膜反应器，控制膜通量范围8～50L/(m2h)，跨膜压差范围0.4～20kPa，接通电源，启动膜反应器，吸附含盐废水中的离子型污染物。
本发明中，控制进水池的进水浓度低于5000mg/L(以TDS计)。
本发明中，外加直流电压范围为0.4～2.0V。
本发明中，电源系统由稳压直流电源为电吸附过程供电，阴极复合膜接电源负极，阳极复合膜接电源正极，电源系统与阴极或阳极连接的电路中设置电流监测装置，实时监测电流情况。
本发明中，集流体采用导电性佳的网孔状材料，所述材料为钛、钛合金材料或不锈钢材料等中任一种，电极采用碳基材料，为碳布、碳纳米管、活性炭粉末或纤维、碳气凝胶、石墨烯或炭黑中任一种，聚合物材料采用 高分子聚合物，具体为聚偏氟乙烯、聚醚砜、聚四氟乙烯或聚丙烯腈中任一种。
本发明中，所述分隔层采用透水性较好的材料，具体为尼龙网、无纺布或聚丙烯材料中的一种。
本发明中，所述阴极复合膜和阳极复合膜可采用不同的电极材料和集流体材料。
本发明的原理是：采用平板膜电极的形式，耦合膜分离和电吸附过程，在适合的膜通量下，分离层对颗粒污染物进行截留，实现对污水的固液分离，在阴阳电极施加适合的电压，吸附污水中的离子型污染物，实现污水脱盐的目的。当电极吸附饱和后，通过短接外加电源开始解吸，将电极再生。通过吸附-解吸循环，可实现膜组件的重复利用，降低运行成本。
与现有技术相比，本发明具有以下优点：
(1)本发明采用平板膜的膜组件形式，耦合膜分离和电吸附的技术方法，可在固液分离的同时对离子型污染物进行吸附，突破现有的膜分离和电吸附工艺的局限性，提升脱盐效果，该技术运行能耗较低，运行管理方便。
(2)本发明中的导电复合膜外侧具有截留颗粒物的功能，减少无效吸附的同时可减少对内侧吸附材料的磨损，经“吸附-脱附”过程，实现吸附材料的循环使用，提高电极材料使用效率，降低装置维护成本。
(3)外加直流电场使膜表面带负电荷，排斥污水中同带负电荷的颗粒、胶体等污染物，控制膜污染，延长膜清洗周期和膜的使用寿命，减少膜清洗的能耗，降低运行成本。
附图说明
图1为耦合膜分离与电吸附技术的脱盐工艺的示意图；
图中标号：1为进水系统，2为电源系统，3为膜反应器，4为出水控制系统，5为清水池，6为复合膜组件，7为导线，8为阴极复合膜，9为阳极复合膜，10为分隔层。
图2为单片膜复合膜组件的详细构成示意图；
图中标号：7为导线，8为阴极复合膜，9为阳极复合膜，10为分隔 层，11为阴极集流体，12为阴极电极，13为阳极电极，14为阳极集流体。
具体实施方式
下面通过实施例结合附图进一步说明本发明。
实施例1：
采用图1中所示的工艺装置，进水系统1由进水池和进水流量调节装置组成，将经过预处理符合工艺要求的以NaCl为主的苦咸水接入进水池，进水含盐量为1200mg/L(以TDS计)，调节进水流量，控制通量为10L/m2h。进水池的出水口通过管道与膜反应器连接，进水池的出水进入膜反应器，膜反应器由反应池、复合膜组件6和搅拌系统组成，采用图2中所示的复合膜组件，其中阳极复合膜由钛网与碳布通过PVDF粘结，阴极复合膜由不锈钢丝网与碳布通过PVDF粘结，分隔层为无纺布。阴极复合膜组件通过导电性能良好的导线7与电源系统2的负极相连，阳极复合膜通过导线与电源正极相连，膜反应器采用浸没式的布置方式，搅拌器设置于反应池内，使反应池内的反应液混合均匀，采用恒流方式运行。接通电源，运行电压为2.0V，启动膜反应器，水力停留时间为1h，运行6h，运行过程中跨膜压差稳定在0.7kPa，膜反应器的反应池出水口通过管道与出水系统连接，通过出水控制系统4调节出水流量，系统的脱盐率为65-72％。
实施例2：
采用图1中所示的工艺装置，进水系统1由进水池和进水流量调节装置组成，将经过预处理符合工艺要求的冷轧废水的生物处理出水接入进水池，进水含盐量为1000mg/L(以TDS计)，悬浮固体浓度为50mg/L，调节进水流量，控制通量为40L/m2h。进水池的出水口通过管道与膜反应器连接，进水池的出水进入膜反应器，膜反应器由反应池、复合膜组件6和搅拌系统组成，采用图2中所示的复合膜组件，其中阳极复合膜和阴极复合膜均由钛网与碳布通过PAN粘结，分隔层为尼龙网。阴极复合膜组件通过导电性能良好的导线7与电源系统2的负极相连，阳极复合膜通过导线与电源正极相连，膜反应器采用浸没式的布置方式，搅拌器设置于反 应池内，使反应池内的反应液混合均匀，采用恒流方式运行。接通电源，运行电压为1.6V，启动膜反应器，水力停留时间为15min，运行4h，运行过程中跨膜压差稳定在2.3kPa，膜反应器的反应池出水口通过管道与出水系统连接，通过出水控制系统4调节出水流量，系统的脱盐率为60-70％，出水的悬浮固体浓度低于检测限。
实施例3：
采用图1中所示的工艺装置，进水系统1由进水池和进水流量调节装置组成，将经过预处理符合工艺要求的以硝酸盐为主的某化肥生产工业废水接入进水池，进水含盐量为900mg/L(以TDS计)，调节进水流量，控制通量为10L/m2h。进水池的出水口通过管道与膜反应器连接，进水池的出水进入膜反应器，膜反应器由反应池、复合膜组件6和搅拌系统组成，采用图2中所示的复合膜组件，其中阳极复合膜和阴极复合膜均由钛网与碳纳米管组成，分隔层为尼龙网，阴极复合膜组件通过导电性能良好的导线7与电源系统2的负极相连，阳极复合膜通过导线与电源正极相连，膜反应器采用浸没式的布置方式，搅拌器设置于反应池内，使反应池内的反应液混合均匀，采用恒流方式运行。接通电源，运行电压为2.0V，启动膜反应器，水力停留时间为1h，运行4h，运行过程中跨膜压差稳定在2.4kPa，膜反应器的反应池出水口通过管道与出水系统连接，通过出水控制系统4调节出水流量，系统的脱盐率为57-68％。
实施例4：
采用图1中所示的工艺装置，进水系统1由进水池和进水流量调节装置组成，将经过预处理符合工艺要求的某含铜废水接入进水池，进水含盐量为500mg/L(以TDS计)，调节进水流量，控制通量为25L/m2h。进水池的出水口通过管道与膜反应器连接，进水池的出水进入膜反应器，膜反应器由反应池、复合膜组件6和搅拌系统组成，采用图2中所示的复合膜组件，其中阳极复合膜和阴极复合膜均由钛网与碳纳米管组成，分隔层为尼龙网，阴极复合膜组件通过导电性能良好的导线7与电源系统2的负极相连，阳极复合膜通过导线与电源正极相连，膜反应器采用浸没式的布 置方式，搅拌器设置于反应池内，使反应池内的反应液混合均匀，采用恒流方式运行。接通电源，运行电压为1.6V，启动膜反应器，水力停留时间为24min，运行3h，运行过程中跨膜压差稳定在1.5kPa，膜反应器的反应池出水口通过管道与出水系统连接，通过出水控制系统4调节出水流量，系统的脱盐率为45-58％。

Claims (7)

  1. 一种适用于污水脱盐回用的复合膜分离方法，其特征在于，所述分离方法采用导电复合膜反应器实现污水脱盐，所述导电复合膜反应器由进水系统(1)、电源系统(2)、膜反应器(3)、出水控制系统(4)和清水池(5)组成；
    所述的进水系统(1)由进水池和进水流量调节装置组成，根据工艺要求调节进水流量，进水流量调节装置设置于进水池的进水口，进水池的出水口通过管道与膜反应器连接，膜反应器由反应池、复合膜组件(6)和搅拌系统组成，位于反应池中的若干片复合膜组件(6)分别通过导电性能良好的导线(7)与电源系统(2)的正负极相连，膜反应器采用浸没式的布置方式，搅拌器设置于反应池内，使反应池内的反应液混合均匀，膜反应器的反应池出水口通过管道与出水系统连接；
    每组复合膜组件为平板膜结构，由阴极复合膜(8)、阳极复合膜(9)和分隔层(10)组成，其中：阴极复合膜由阴极电极(11)和阴极集流体(12)通过聚合物材料粘合而成，阳极复合膜由阳极电极(13)和阳极集流体(14)通过聚合物材料粘合而成，所述阴极复合膜(8)和阳极复合膜(9)通过分隔层(10)隔开，以防止短路；所述阴极集流体位于进水口一侧，阳极集流体位于出水口一侧，即进水先流经阴极集流体和阴极电极，经过分隔层，再通过阳极电极和阳极集流体，以膜出水的形式排出导电复合膜反应器；
    具体步骤如下：
    将符合工艺要求的进水接入进水池，通过进水流量调节装置调节进水流量，进水池的出水进入膜反应器，采用恒流或恒压的方式运行，进水先流经阴极集流体和阴极电极，经过分隔层，再通过阳极电极和阳极集流体，以膜出水的形式排出导电复合膜反应器，控制膜通量为8～50L/(m2h)，跨膜压差为0.4～20kPa，接通电源，启动膜反应器，吸附含盐废水中的离子型污染物。
  2. 根据权利要求1所述的适用于污水脱盐回用的复合膜分离方法，其特征在于，控制进水池的进水浓度低于5000mg/L(以TDS计)。
  3. 根据权利要求1所述的适用于污水脱盐回用的复合膜分离方法，其特 征在于，外加直流电压范围为0.4～2.0V。
  4. 根据权利要求1所述的适用于污水脱盐回用的复合膜分离方法，其特征在于，电源系统由稳压直流电源为电吸附过程供电，阴极复合膜接电源负极，阳极复合膜接电源正极，电源系统与阴极或阳极连接的电路中设置电流监测装置，实时监测电流情况。
  5. 根据权利要求1所述的适用于污水脱盐回用的复合膜分离方法，其特征在于，阴极集流体或阳极集流体采用导电性佳的网孔状材料，所述材料为钛、钛合金材料或不锈钢材料中任一种，阴极电极或阳极电极采用碳基材料，为碳布、碳纳米管、活性炭粉末或纤维、碳气凝胶、石墨烯或炭黑中任一种，聚合物材料采用高分子聚合物，具体为聚偏氟乙烯、聚醚砜、聚四氟乙烯或聚丙烯腈中任一种。
  6. 根据权利要求5所述的适用于污水脱盐回用的复合膜分离方法，其特征在于，所述阴极复合膜和阳极复合膜可采用不同的电极材料和集流体材料。
  7. 根据权利要求1所述的适用于污水脱盐回用的复合膜分离方法，其特征在于，所述分隔层采用透水性较好的材料，具体为尼龙网、无纺布或聚丙烯材料中任一种。
PCT/CN2016/103464 2016-01-22 2016-10-27 一种适用于污水脱盐回用的复合膜分离方法 Ceased WO2017124798A1 (zh)

Priority Applications (2)

Application Number Priority Date Filing Date Title
JP2018537775A JP6583868B2 (ja) 2016-01-22 2016-10-27 汚水の脱塩回収に適用する複合膜分離方法
AU2016388020A AU2016388020B2 (en) 2016-01-22 2016-10-27 Composite membrane separation method applicable to desalting and recycling of sewage

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN201610041958.4 2016-01-22
CN201610041958.4A CN105692817B (zh) 2016-01-22 2016-01-22 一种适用于污水脱盐回用的复合膜分离方法

Publications (1)

Publication Number Publication Date
WO2017124798A1 true WO2017124798A1 (zh) 2017-07-27

Family

ID=56228549

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2016/103464 Ceased WO2017124798A1 (zh) 2016-01-22 2016-10-27 一种适用于污水脱盐回用的复合膜分离方法

Country Status (4)

Country Link
JP (1) JP6583868B2 (zh)
CN (1) CN105692817B (zh)
AU (1) AU2016388020B2 (zh)
WO (1) WO2017124798A1 (zh)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109987755A (zh) * 2017-12-29 2019-07-09 宁波方太厨具有限公司 一种水过滤系统
CN110526349A (zh) * 2018-05-24 2019-12-03 华东理工大学 一种电辅助膜分离方法
CN115676986A (zh) * 2022-11-01 2023-02-03 河南师范大学 一种三维孔结构Fe2O3/rGO/泡沫镍复合电容脱盐电极的制备及应用
CN115818791A (zh) * 2022-11-30 2023-03-21 江苏美淼环保科技有限公司 钟摆式电吸附水处理装置
CN116835790A (zh) * 2023-06-15 2023-10-03 艾培克环保科技(上海)有限公司 一种丙烯酸丁酯废水的处理工艺
CN118324268A (zh) * 2024-06-12 2024-07-12 中科合肥技术创新工程院 一种多组电极cdi模块水处理装置及处理方法

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105692817B (zh) * 2016-01-22 2018-02-09 同济大学 一种适用于污水脱盐回用的复合膜分离方法
CN107441950B (zh) * 2017-08-02 2020-05-05 同济大学 一种电化学耦合陶瓷滤膜及其应用
CN110182906B (zh) * 2019-07-12 2022-01-11 山东大学 一种导电有机膜耦合过滤系统降解有机废水的处理工艺
CN110498491B (zh) * 2019-08-28 2021-03-16 山东大学 一种电化学膜过滤耦合系统降解抗生素废水的处理工艺
CN111359449B (zh) * 2020-03-03 2021-05-18 清华大学 电活性膜及其制备方法
CN112358097B (zh) * 2020-11-13 2022-10-25 昆明理工大学 一种多物理场强化高电解质废水处理的方法和装置
CN114149075B (zh) * 2021-12-09 2024-04-09 吉林省电力科学研究院有限公司 一种具有除盐能力的膜生物反应系统

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6309532B1 (en) * 1994-05-20 2001-10-30 Regents Of The University Of California Method and apparatus for capacitive deionization and electrochemical purification and regeneration of electrodes
CN101615512A (zh) * 2008-06-24 2009-12-30 通用电气公司 超级电容装置及其制造方法
CN101891286A (zh) * 2010-04-02 2010-11-24 广州天至环保科技有限公司 一种在线净化并回用电镀和化学镀废水的系统
CN102574708A (zh) * 2009-07-29 2012-07-11 通用电气公司 双极性电极和超级电容器脱盐装置以及制造方法
CN105692817A (zh) * 2016-01-22 2016-06-22 同济大学 一种适用于污水脱盐回用的复合膜分离方法

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH03234016A (ja) * 1990-02-09 1991-10-18 Isuzu Motors Ltd 電気二重層コンデンサ
JPH0688271A (ja) * 1991-07-03 1994-03-29 Konica Corp 炭素質電極式電解槽
JP4212856B2 (ja) * 2002-09-06 2009-01-21 野村マイクロ・サイエンス株式会社 電気脱塩方法及び電気脱塩装置
US7813106B2 (en) * 2006-12-19 2010-10-12 General Electric Company High current efficiency supercapacitor desalination devices and methods of making the same
WO2010150534A1 (ja) * 2009-06-23 2010-12-29 クラレケミカル株式会社 通液型キャパシタ、脱イオン水の製造方法、及び脱イオン水製造装置
CN104211141B (zh) * 2014-09-11 2016-07-06 北京今大禹环保技术有限公司 一种spe电解槽的布水结构及其布水方法

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6309532B1 (en) * 1994-05-20 2001-10-30 Regents Of The University Of California Method and apparatus for capacitive deionization and electrochemical purification and regeneration of electrodes
CN101615512A (zh) * 2008-06-24 2009-12-30 通用电气公司 超级电容装置及其制造方法
CN102574708A (zh) * 2009-07-29 2012-07-11 通用电气公司 双极性电极和超级电容器脱盐装置以及制造方法
CN101891286A (zh) * 2010-04-02 2010-11-24 广州天至环保科技有限公司 一种在线净化并回用电镀和化学镀废水的系统
CN105692817A (zh) * 2016-01-22 2016-06-22 同济大学 一种适用于污水脱盐回用的复合膜分离方法

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109987755A (zh) * 2017-12-29 2019-07-09 宁波方太厨具有限公司 一种水过滤系统
CN109987755B (zh) * 2017-12-29 2024-01-19 宁波方太厨具有限公司 一种水过滤系统
CN110526349A (zh) * 2018-05-24 2019-12-03 华东理工大学 一种电辅助膜分离方法
CN115676986A (zh) * 2022-11-01 2023-02-03 河南师范大学 一种三维孔结构Fe2O3/rGO/泡沫镍复合电容脱盐电极的制备及应用
CN115818791A (zh) * 2022-11-30 2023-03-21 江苏美淼环保科技有限公司 钟摆式电吸附水处理装置
CN116835790A (zh) * 2023-06-15 2023-10-03 艾培克环保科技(上海)有限公司 一种丙烯酸丁酯废水的处理工艺
CN116835790B (zh) * 2023-06-15 2024-03-08 艾培克环保科技(上海)有限公司 一种丙烯酸丁酯废水的处理工艺
CN118324268A (zh) * 2024-06-12 2024-07-12 中科合肥技术创新工程院 一种多组电极cdi模块水处理装置及处理方法

Also Published As

Publication number Publication date
AU2016388020B2 (en) 2019-10-10
CN105692817B (zh) 2018-02-09
JP2019506292A (ja) 2019-03-07
CN105692817A (zh) 2016-06-22
JP6583868B2 (ja) 2019-10-02
AU2016388020A1 (en) 2018-08-09

Similar Documents

Publication Publication Date Title
AU2016388020B2 (en) Composite membrane separation method applicable to desalting and recycling of sewage
CN104478045B (zh) 一种用于焦化废水的高效电渗析脱盐装置与方法
CN102674632B (zh) 垃圾渗滤液零排放回用处理方法
CN100581640C (zh) 一种同步浓缩和纯化重金属废水的电去离子方法与装置
JP2010514555A (ja) 極性物質の物理的分離装置
CN108394960B (zh) 一种适用于水源水污染物去除的阴极电化学微滤膜耦合反应器
US20210171369A1 (en) Methods of removing contaminants from a solution, and related systems
CN102329029A (zh) 电凝聚-吸附去除水中氟离子的方法
CN102603039A (zh) 耦合脱盐方法及装置
CN105540953A (zh) 一种电解-电渗析复合水处理装置
CN108793346A (zh) 一种电吸附耦合扩展活性炭处理微污染苦咸水的装置与方法
JP2004537411A (ja) 可動電極フロースルー・キャパシター
CN112321034A (zh) 一种同步电解/膜分离/高级氧化协同处理含硫酸铵废水及有机废水的装置和方法
KR20120133229A (ko) Ｃｄｉ를 이용한 상수처리방법 및 이의 장치
CN104591466B (zh) 一种电厂脱硫废水零排放处理的方法
CN209397045U (zh) 一种一体化过滤电吸附水处理装置
CN107224999A (zh) 一种基于电渗析技术的树脂脱附液处置方法
CN103819036B (zh) 一种电厂脱硫废水处理方法
CN113105036A (zh) 一种基于电吸附技术的高盐水体除盐系统
CN111204904A (zh) 一种基于流动电极的废水资源化处理系统及其处理方法
CN114314737B (zh) 光电协同强化同步脱盐降解有机物的污水处理方法和装置
CN113149158B (zh) 一种使用纯电容去离子技术淡化苦咸水的系统及其淡化苦咸水的方法
CN117342648A (zh) 一种基于流动电极电吸附脱盐的复杂废水处理及资源回收装置
CN204550323U (zh) 一种垃圾渗滤液浓缩液处理装置
CN212127829U (zh) 一种反渗透浓缩液电解回收装置

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 16886058

Country of ref document: EP

Kind code of ref document: A1

ENP Entry into the national phase

Ref document number: 2018537775

Country of ref document: JP

Kind code of ref document: A

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 2016388020

Country of ref document: AU

Date of ref document: 20161027

Kind code of ref document: A

122 Ep: pct application non-entry in european phase

Ref document number: 16886058

Country of ref document: EP

Kind code of ref document: A1

32PN Ep: public notification in the ep bulletin as address of the adressee cannot be established

Free format text: NOTING OF LOSS OF RIGHTS PURSUANT TO RULE 112(1) EPC (EPO FORM 1205A DATED 21/12/2018)

122 Ep: pct application non-entry in european phase

Ref document number: 16886058

Country of ref document: EP

Kind code of ref document: A1