WO2019033936A1 - 一种用于水处理、物料分离的装置及其分离方法 - Google Patents

一种用于水处理、物料分离的装置及其分离方法 Download PDF

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WO2019033936A1
WO2019033936A1 PCT/CN2018/098460 CN2018098460W WO2019033936A1 WO 2019033936 A1 WO2019033936 A1 WO 2019033936A1 CN 2018098460 W CN2018098460 W CN 2018098460W WO 2019033936 A1 WO2019033936 A1 WO 2019033936A1
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water
membrane
unit
water supply
material separation
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PCT/CN2018/098460
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English (en)
French (fr)
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张杨
颜丙花
萨毅夫
郎巧霖
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中国科学院青岛生物能源与过程研究所
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Publication of WO2019033936A1 publication Critical patent/WO2019033936A1/zh

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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
    • C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
    • C02F1/4698—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electro-osmosis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/427—Electro-osmosis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • B01D61/46—Apparatus therefor
    • B01D61/48—Apparatus therefor having one or more compartments filled with ion-exchange material, e.g. electrodeionisation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • B01D61/46—Apparatus therefor
    • B01D61/48—Apparatus therefor having one or more compartments filled with ion-exchange material, e.g. electrodeionisation
    • B01D61/485—Specific features relating to the ion-exchange material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • B01D61/52—Accessories; Auxiliary operation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • B01D61/54—Controlling or regulating
    • 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
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/46—Apparatus for electrochemical processes
    • 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
    • C02F2201/48—Devices for applying magnetic or electric fields

Definitions

  • the invention belongs to the technical field of membrane separation and application, in particular to an apparatus and method for water treatment and material separation by an electric field enhanced membrane permeation water treatment and material separation technology.
  • Membrane separation technology is widely used in water treatment fields such as desalination, wastewater treatment, and in energy, agriculture, pharmaceutical, and food processing industries due to its high efficiency and unique separation characteristics.
  • pressure membranes such as reverse osmosis (RO)
  • RO reverse osmosis
  • positive permeation does not require external pressure as the separation driving force, but promotes the positive permeation separation process by the osmotic pressure difference of the solution on both sides of the selective membrane. It is one of the hotspots in the field of membrane separation in the world. .
  • Forward osmosis technology has broad application prospects in the fields of desalination, concentration and water purification.
  • the driving force of positive osmosis is the osmotic pressure difference between the two solutions. Therefore, it is usually necessary to use a very high concentration of the squirting liquid when working with the forward osmosis technique, and theoretically, the osmotic pressure on both sides of the membrane reaches equilibrium, and the osmosis cannot continue. jobs.
  • the positively osmotic draw liquid consumes a large amount of energy because of its high salt content.
  • the forward osmosis membrane in order to block the back diffusion of the salt, generally has a membrane pore size of less than 1 nm, and the concentration polarization in the membrane is an important factor that can not be ignored in the osmotic pressure during the forward osmosis process and causes a decrease in flux.
  • the present invention provides an apparatus and method for osmotic water treatment and material separation of an electric field reinforced membrane, and the purpose of positive osmosis separation is achieved by a water supply unit and a water producing unit composed of a water permeable membrane.
  • the present invention provides the following technical solutions:
  • the utility model relates to a water treatment and material separation device, wherein the device is a power source 1, an anode chamber 2, a cathode chamber 3 and a membrane unit 4; wherein a positive pole of the power source is connected with the anode chamber, a cathode is connected with the cathode chamber, and a membrane is formed between the two pole chambers.
  • the membrane unit is composed of an ion exchange membrane and a water permeable membrane.
  • the membrane unit is divided into a water supply unit and a water production unit; wherein the water supply membrane unit is composed of a cation exchange membrane, an anion exchange membrane and a water permeable membrane in sequence, and the water production unit is composed of a water permeable membrane and a cation exchange membrane in the water supply membrane unit.
  • the water supply membrane unit sequentially forms two chambers by a cation exchange membrane, an anion exchange membrane and a water permeable membrane; the D1 chamber is composed of a cation exchange membrane and an anion exchange membrane, and the D2 chamber is composed of an anion exchange membrane and a water permeable membrane.
  • the water supply units D1 and D2 can be fed with the same or different water supply.
  • the water producing unit is a water producing unit chamber R composed of a water permeable membrane in the water supply membrane unit and a cation exchange membrane close to the negative electrode of the power source.
  • the water permeable membrane has a pore diameter of from 0.1 to 50,000 nm.
  • the anion and cation exchange membranes may be ion exchange membranes of various materials.
  • a method for separating materials by using a water treatment and material separation device injecting a sample to be treated into a water producing unit, and injecting the electrolyte into a water supply unit, respectively forming an ion depletion on both sides of the water permeable membrane under the action of an electric field Layer (water supply unit) and ion enrichment layer (water production unit), under the action of electron osmotic pressure, water in the water supply unit is transported through the water permeable membrane to the water producing unit, and at the same time, the role of the electric field, the water producing unit The ions migrate to the water supply unit through the water permeable membrane to achieve separation.
  • an electric field Layer water supply unit
  • ion enrichment layer water production unit
  • the electrolyte of the water supply unit is a monovalent or multivalent salt solution having electrical conductivity.
  • the electric field enhances the membrane penetration, does not require a pumping liquid during the working process, and even the ion concentration of the water supply unit can be higher than the water producing unit, and the ion concentration of the water producing unit can be as low as near zero.
  • the water supply is passed through the pipeline to the water supply membrane unit, and the low salt concentration produced water is connected to the water producing membrane unit through the pipeline.
  • the two cavities formed in the water supply unit can supply the same or different water supply into them separately or through a single pipe, thereby forming two chambers for separate use or communication for the whole.
  • the above apparatus and method can be applied in the fields of water treatment and material separation, such as product concentration, dilution, sample purification, etc., and can also be used to generate electricity using salt difference.
  • the invention has the advantages that the electric field reinforced membrane permeating water treatment and material separation device and method of the invention overcome the traditional positive osmosis in concentration, dilution and desalting by using an electric field as a driving force instead of the traditional osmotic osmotic pressure driving.
  • the limitation and low energy consumption make the working efficiency of forward osmosis will be improved, and it is not limited to the concentration polarization phenomenon. Due to the surface potential of the membrane, the membrane has a certain blocking effect on the salt in the water, and its use is common.
  • a permeable membrane (such as an ultrafiltration membrane) can achieve a positive osmosis effect, which will greatly expand the application of the technology in water treatment and material separation, making it suitable for desalination, high value-added product concentration or toxic by-products. Dilution can also be used for product purification.
  • 1A is a diagram of a basic device according to an embodiment of the present invention, wherein: 1. a power source, 2. an anode chamber, a cathode chamber, and a membrane unit.
  • 1B is a diagram of a basic device according to an embodiment of the present invention, wherein: 1. a power source, 2. an anode chamber, a cathode chamber, and a membrane unit.
  • FIG. 2 is a schematic view showing the infiltration of seawater desalination of an electric field enhancement film according to Embodiment 1 of the present invention.
  • FIG. 3 is a schematic view showing concentration of an electric field reinforced membrane permeation product according to Embodiment 2 of the present invention.
  • Embodiment 4 is a view showing an electric field reinforced membrane permeation apparatus according to Embodiment 4 of the present invention.
  • the electric field reinforced membrane permeating water treatment and material separation device and method of the invention comprises an anode chamber connected to a positive pole of a power source, a cathode chamber connected to a negative pole of the power source, and a water permeable membrane unit, wherein the membrane unit is divided into a water supply unit and a water producing unit
  • the water supply membrane unit is composed of a cation exchange membrane, an anion exchange membrane and a water permeable membrane
  • the water production unit is composed of a water permeable membrane and a cation exchange membrane, wherein the water permeable membrane unit and the water permeable membrane unit have the same membrane.
  • the driving force of membrane permeation is an electric field.
  • the invention is a kind of subversion of the traditional forward osmosis technology, and the electric field is used as the driving force to replace the traditional osmotic pressure driven by the positive osmosis, and does not depend on the osmotic pressure of the drawing liquid.
  • the electric field is used as the driving force, and the working efficiency of the forward osmosis will be improved. And is not limited to the concentration polarization phenomenon.
  • the membrane due to the surface potential of the membrane, the membrane has a certain barrier effect on the salt in the water.
  • a normal permeable membrane such as ultrafiltration membrane
  • the limitations of traditional positive osmosis in concentration, dilution and desalination are overcome, the energy consumption is low, and the application prospect in energy and environment is broad.
  • the apparatus as shown in FIGS. 1A and B, includes a power source 1, an anode chamber 2, a cathode chamber 3, and a membrane unit 4; wherein a positive electrode of the power source is connected to the anode chamber, a cathode is connected to the cathode chamber, and a membrane unit is placed in the anode chamber and the cathode chamber.
  • the membrane unit is composed of an ion exchange membrane and a water permeable membrane.
  • the membrane unit is divided into a water supply unit and a water production unit; wherein the water supply membrane unit is composed of a cation exchange membrane, an anion exchange membrane and a water permeable membrane in sequence, and the water production unit is composed of a water permeable membrane and a cation exchange membrane in the water supply membrane unit.
  • the water supply membrane unit sequentially forms two chambers by a cation exchange membrane, an anion exchange membrane and a water permeable membrane; the D1 chamber is composed of a cation exchange membrane and an anion exchange membrane, and the D2 chamber is composed of an anion exchange membrane and a water permeable membrane.
  • the water producing unit is composed of a water permeable membrane in the water supply membrane unit and a water producing unit chamber R composed of a cation exchange membrane close to the negative electrode of the power source.
  • the water permeable membrane has a pore diameter of from 0.1 to 50,000 nm.
  • the sample to be treated is injected into the water producing unit, and the electrolyte is injected into the water supply unit, and an ion depletion layer (water supply unit) is formed on both sides of the permeable membrane under the action of the electric field.
  • an ion-rich layer water-producing unit
  • the membrane migrates to the water supply unit to effect separation.
  • the electrolyte of the water supply unit is a monovalent or multivalent salt solution having electrical conductivity.
  • the electric field reinforced membrane permeation does not require pumping liquid during the working process, and even the ion concentration of the water supply unit can be higher than that of the water producing unit, and the ion concentration of the water producing unit can be as low as near zero.
  • the above device is used to perform seawater desalination, and the same solution is introduced into the water supply unit to dilute a sample, specifically:
  • the solution of the water supply unit can be concentrated to one-fifth of the original volume.
  • Sodium sulfate and sodium chloride waste liquid are respectively introduced into the water supply units D1 and D2 of the device; industrial wastewater (such as chlor-alkali wastewater) that needs to be desalted and returned to water is introduced into the water producing unit; Under the action of the electric field, an ion depletion layer (water supply unit) and an ion enrichment layer (water production unit) are respectively formed on both sides of the water permeable membrane. Therefore, under the action of electroosmotic pressure, the water source continuously permeates through the water supply unit. The membrane migrates to the water producing unit, and at the same time, due to the action of the electric field, the ions of the water producing unit are continuously removed, and the purpose of water supply concentration and water reuse is realized.

Abstract

一种用于水处理、物料分离的装置，该装置为电源（1）、阳极室（2）、阴极室（3）及膜单元（4）；其中，电源（1）的正极与阳极室（2）连接、负极与阴极室（3）连接，两极室之间为膜单元（4）；膜单元（4）由离子交换膜与透水膜组成。还公开了一种采用用于水处理、物料分离的装置分离物料的方法以及一种用于水处理、物料分离的装置的应用。

Description

一种用于水处理、物料分离的装置及其分离方法 技术领域
本发明属于膜分离及应用技术领域，具体是一种电场强化的膜渗透水处理和物料分离技术用于水处理、物料分离的装置和方法。
背景技术
水和能源的短缺促使人类必须考虑发展更多突破传统自然资源限制的技术。膜分离技术由于其高效和独有的分离特性而被广泛应用在海水淡化、废水处理等水处理领域以及用于能源、农业、制药和食品加工等行业。但是压力膜，如反渗透(reverse osmosis,RO)虽然高效，但是其运行需要消耗大量外源能量，使其大规模应用变得经济上不可行。正渗透作为新兴的绿色膜分离技术，不需要外加压力作为分离驱动力，而是靠选择性膜两侧溶液自身的渗透压差推动正渗透分离过程，是目前世界膜分离领域研究的热点之一。
正渗透技术在脱盐、浓缩和水净化等领域有广泛的应用前景。正渗透的驱动力是两种溶液的渗透压差，因此，在应用正渗透技术进行工作时通常需要很高浓度的汲取液，而且理论上当膜两边的渗透压达到平衡后，正渗透既无法继续工作。正渗透的汲取液由于含盐量较高，因此其循环利用需要消耗大量的能量。另外，正渗透膜为了阻截盐的反扩散，通常膜孔径为小于1纳米的致密膜，而膜内浓差极化是正渗透过程中渗透压降低和导致通量下降的不可忽视的重要因素。
因此，现急需一种正渗透过程的驱动力不依赖于汲取液的渗透压的物料分离装置和方法。
发明内容
鉴于以上背景技术，本发明提供了一种电场强化膜渗透水处理和物料分离的装置和方法，通过由透水膜组成的供水单元和产水单元，实现类正渗透分离的目的。
为了实现上述目的，本发明提供如下技术方案：
一种用于水处理、物料分离装置，装置为电源1、阳极室2、阴极室3及膜单元4；其中，电源的正极与阳极室连接、负极与阴极室连接，两极室之间为膜单元；所述膜单元由离子交换膜与透水膜组成组成。
所述膜单元分为供水单元和产水单元；其中，供水膜单元依次由阳离子交换膜、阴离子交换膜和透水膜组成，产水单元由供水膜单元中的透水膜和阳离子交换膜组成。
所述供水膜单元依次由阳离子交换膜、阴离子交换膜和透水膜形成两个腔室；D1室为阳离子交换膜和阴离子交换膜组成，D2室为阴离子交换膜和透水膜组成。
所述供水单元D1和D2室可通入相同或不同的供水。所述产水单元为由供水膜单元中的透水膜和靠近电源负极的阳离子交换膜组成的产水单元腔室R。
所述透水膜孔径介于0.1-50000nm。
所述阴、阳离子交换膜可以是各种材质的离子交换膜。
一种采用用于水处理、物料分离装置分离物料的方法，将待处理样品注入至产水单元，并将电解液注入至供水单元，在电场的作用下在透水膜两侧分别形成离子耗尽层(供水单元)和离子富集层(产水单元)，使其在电子渗透压的作用下，供水单元中的水透过透水膜向产水单元迁移，同时在电场的作用，产水单元的离子透过透水膜向供水单元迁移，实现分离。
所述供水单元的电解液为具有电导率的单价或多价盐溶液。所述电场强化膜渗透，在工作过程中不需要汲取液，甚至供水单元的离子浓度可以高于产水单元，产水单元离子浓度可以低至近零。
其中，通过管路将供水通入供水膜单元，低盐浓度产水通过管路与产水膜单元相连。供水单元中形成的两个腔体可分别或通过一条管路将相同或不同的供水供入其中，进而形成两个腔室的分别单独使用或联通为整体使用。
上述装置和方法可以应用在水处理和物料分离领域，如产物浓缩、稀释、样品提纯等过程，并且还可用于利用盐差发电。
本发明所具有的优点：本发明电场强化膜渗透水处理和物料分离装置和方法，其通过电场作为驱动力，代替传统正渗透的渗透压驱动，克服了传统正渗透在浓缩、稀释和脱盐方面的局限性，能耗低，使得正渗透的工作效率将会提高，且不受限于浓差极化现象，由于膜的表面电位作用，膜对于水中的盐具有一定的阻截效果，其利用普通透水膜(如超滤膜)可达到正渗透的作用，这将会极大扩展该技术在水处理和物料分离的应用领域，使其可以用于海水淡化、高附加值产物浓缩或有毒副产物稀释，也可以用于产物提纯。
附图说明
图1A为本发明实施例提供的基本装置图，其中，1.电源、2.阳极室、3.阴极室、4.膜单元。
图1B为本发明实施例提供的基本装置图，其中，1.电源、2.阳极室、3.阴极室、4.膜单元。
图2为本发明实施例1提供的电场强化膜渗透海水淡化示意图。
图3为本发明实施例2提供的电场强化膜渗透产物浓缩示意图。
图4为本发明实施例4提供的电场强化膜渗透装置图。
具体实施方式
下面结合附图和实例对本发明作进一步说明，为了更清楚地说明本发明实施例，下面结合附图中的介绍对实施例或现有技术进行描述，非常明显地，附图中记载的仅仅是本发明的一些实施例。
本发明电场强化膜渗透水处理和物料分离装置和方法，方法包括与电源的正极连接的阳极室、与电源的负极连接的阴极室及透水膜单元，所述膜单元分为供水单元和产水单元；所述供水膜单元由阳离子交换膜、阴离子交换膜和透水膜组成，所述产水单元由透水膜和阳离子交换膜组成，其中供水膜单元和产水膜单元的透水膜是同一片膜，膜渗透的驱动力为电场。本发明是对传统正渗透技术的一种颠覆，以电场作为驱动力代替传统正渗透的渗透压驱动，不依赖于汲取液的渗透压，通过电场作为驱动力，正渗透的工作效率将会提高，且不受限于浓差极化现象。另外，由于膜的表面电位作用，膜对于水中的盐具有一定的阻截效果。因此，如果利用普通透水膜(如超滤膜)可达到正渗透的作用，克服了传统正渗透在浓缩、稀释和脱盐方面的局限性，能耗低，在能源和环境领域应用前景广阔。
实施例1
装置，参见图1A和B，包括电源1、阳极室2、阴极室3及膜单元4；其中，电源的正极与阳极室连接、负极与阴极室连接，膜单元置于阳极室和阴极室之间；所述膜单元由离子交换膜与透水膜组成组成。
所述膜单元分为供水单元和产水单元；其中，供水膜单元依次由阳离子交换膜、阴离子交换膜和透水膜组成，产水单元由供水膜单元中的透水膜和阳离子交换膜组成。
所述供水膜单元依次由阳离子交换膜、阴离子交换膜和透水膜形成两个腔室；D1室为阳离子交换膜和阴离子交换膜组成，D2室为阴离子交换膜和透水膜组成。所述产水单元由供水膜单元中的透水膜和靠近电源负极的阳离子交换膜组成的产水单元腔室R。
所述透水膜孔径介于0.1-50000nm。
电场强化膜渗透方法过程，参见图1，将待处理样品注入至产水单元，并将电解液注入至供水单元，在电场的作用下在透水膜两侧分别形成离子耗尽层(供水单元)和离子富集层(产水单元)，使其在电子渗透压的作用下，供水单元中的水透过透水膜向产水单元迁移，同时在电场的作用，产水单元的离子透过透水膜向供水单元迁移，实现分离。
所述供水单元的电解液为具有电导率的单价或多价盐溶液。电场强化膜渗透在工作过程中不需要汲取液，甚至供水单元的离子浓度可以高于产水单元，产水单元离子浓度可以低至近零。
其适用于产物浓缩、稀释、样品提纯等过程。
实施例2
利用上述装置，进行海水淡化，供水单元内通入同样的溶液，对一种样品进行淡化，具体为：
向所述装置的供水单元内通入3wt％浓度的NaCl溶液；在所述产水单元通入海水；接通电源，在电场的作用下在透水膜两侧分别形成离子耗尽层(供水单元)和离子富集层(产水单元)，因此，在电致渗透压的作用下，水源源不断从供水单元透过透水膜向产水单元迁移，溶液的渗透压就会使水往产水方向走，同时由于电场的作用，产水单元的离子不断被迁移至供水单元，同时实现了产水和脱盐的双重目的(参见图2)。由图2可见，产水单元的电导率可以降到近零，同时供水单元的电导率约是海水的两倍，即该装置可以同时实现产水和脱盐的目的。
实施例3
利用上述装置，进行硫酸钠浓缩，供水单元内通入同样的溶液，对一种样品进行浓缩，具体为：
向所述装置的供水单元内通入硫酸钠溶液；在所述产水单元通入硫酸钠溶液；接通电源，在电场的作用下在透水膜两侧分别形成离子耗尽层(供水单元)和离子富集层(产水单元)，因此，在电致渗透压的作用下，水源源不断从供水单元透过透水膜向产水单元迁移，同时由于电场的作用，产水单元的离子不断被移走，同时实现了硫酸钠浓缩的目的(参见图3)。
由图3可见，供水单元的溶液可以浓缩至原体积的五分之一。
实施例4
利用上述装置(图4)，进行硫酸钠和氯化钠废液浓缩，同时实现水回用，供水单元D1和D2室分别通入硫酸钠和氯化钠废液，对两种样品进行浓缩，具体为：
向所述装置的供水单元D1和D2室内分别通入硫酸钠和氯化钠废液；在所述产水单元通入需要脱盐且回用水的工业废水(如氯碱废水)；接通电源，在电场的作用下在透水膜两侧分别形成离子耗尽层(供水单元)和离子富集层(产水单元)，因此，在电致渗透压的作用下，水源源不断从供水单元透过透水膜向产水单元迁移，同时由于电场的作用，产水单元的离子不断被移走，同时实现了供水浓缩和水回用的目的。
上面以举例方式对本发明进行了详细描述，并不是全部的实施例。基于本发明中的实施例，本领域普通技术人员在没有做出创造性劳动的前提下所获得的所有其他实施例，都属于本发明保护的范围。

Claims (10)

  1. 一种用于水处理、物料分离的装置，其特征在于：装置为电源(1)、阳极室(2)、阴极室(3)及膜单元(4)；其中，电源的正极与阳极室连接、负极与阴极室连接，两极室之间为膜单元；所述膜单元由离子交换膜与透水膜组成组成。
  2. 按权利要求1所述的用于水处理、物料分离的装置，其特征在于：所述膜单元分为供水单元和产水单元；其中，供水膜单元依次由阳离子交换膜、阴离子交换膜和透水膜组成，产水单元由供水膜单元中的透水膜和阳离子交换膜组成。
  3. 按权利要求2所述的用于水处理、物料分离的装置，其特征在于：所述供水膜单元依次由阳离子交换膜、阴离子交换膜和透水膜形成两个腔室；D1室为阳离子交换膜和阴离子交换膜组成，D2室为阴离子交换膜和透水膜组成。
  4. 按权利要求3所述的用于水处理、物料分离的装置，其特征在于：所述供水单元D1和D2室可通入相同或不同的供水。
  5. 按权利要求2所述的用于水处理、物料分离的装置，其特征在于：所述产水膜单元为供水膜单元中的透水膜和靠近电源负极的阳离子交换膜组成的产水单元腔室R。
  6. 按权利要求2-5任意一项所述的用于水处理、物料分离的装置，其特征在于：所述透水膜孔径介于0.1-50000nm。
  7. 按权利要求2-5任意一项所述的用于水处理、物料分离的装置，其特征在于：所述阴、阳离子交换膜可以是各种材质的离子交换膜。
  8. 一种采用权利要求1用于水处理、物料分离装置分离物料的方法，其特征在于：将待处理样品注入至产水单元，并将电解液注入至供水单元，在电场的作用下在透水膜两侧分别形成离子耗尽层(供水单元)和离子富集层(产水单元)，使其在电致渗透压的作用下，供水单元中的水透过透水膜向产水单元迁移，同时在电场的作用，产水单元的离子透过透水膜向供水单元迁移，实现分离。
  9. 按权利要求7所述的用于水处理、物料分离装置分离物料的方法，其特征在于：所述供水单元的电解液为具有电导率的单价或多价的一种或两种的盐溶液。
  10. 一种权利要求1所述的用于水处理、物料分离装置的应用，其特征在于：所述装置应用在水处理、物料的分离过程或用于盐差发电。
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