CN114084941A - Permeation chromatography water purification equipment based on bipolar ion membrane and water purification method thereof - Google Patents
Permeation chromatography water purification equipment based on bipolar ion membrane and water purification method thereof Download PDFInfo
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- CN114084941A CN114084941A CN202111454271.0A CN202111454271A CN114084941A CN 114084941 A CN114084941 A CN 114084941A CN 202111454271 A CN202111454271 A CN 202111454271A CN 114084941 A CN114084941 A CN 114084941A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 160
- 239000012528 membrane Substances 0.000 title claims abstract description 48
- 238000000746 purification Methods 0.000 title claims abstract description 21
- 238000000034 method Methods 0.000 title claims abstract description 13
- 238000004587 chromatography analysis Methods 0.000 title description 2
- 238000002242 deionisation method Methods 0.000 claims abstract description 73
- 230000008929 regeneration Effects 0.000 claims abstract description 32
- 238000011069 regeneration method Methods 0.000 claims abstract description 32
- 238000003860 storage Methods 0.000 claims abstract description 24
- 239000008213 purified water Substances 0.000 claims abstract description 21
- 150000002500 ions Chemical class 0.000 claims description 30
- 150000001768 cations Chemical class 0.000 claims description 17
- 150000001450 anions Chemical class 0.000 claims description 16
- 238000005341 cation exchange Methods 0.000 claims description 16
- 239000003014 ion exchange membrane Substances 0.000 claims description 12
- 238000005349 anion exchange Methods 0.000 claims description 10
- 230000005684 electric field Effects 0.000 claims description 8
- 239000003011 anion exchange membrane Substances 0.000 claims description 7
- 239000003957 anion exchange resin Substances 0.000 claims description 7
- 238000010494 dissociation reaction Methods 0.000 claims description 7
- 239000011347 resin Substances 0.000 claims description 7
- 229920005989 resin Polymers 0.000 claims description 7
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 6
- 230000009471 action Effects 0.000 claims description 6
- 230000002146 bilateral effect Effects 0.000 claims description 6
- 239000003054 catalyst Substances 0.000 claims description 6
- 208000018459 dissociative disease Diseases 0.000 claims description 6
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical group [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 claims description 5
- 230000001172 regenerating effect Effects 0.000 claims description 5
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 claims description 4
- 239000003729 cation exchange resin Substances 0.000 claims description 4
- 229910052731 fluorine Inorganic materials 0.000 claims description 4
- 239000011737 fluorine Substances 0.000 claims description 4
- 239000003456 ion exchange resin Substances 0.000 claims description 4
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims description 4
- 230000008569 process Effects 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 238000006073 displacement reaction Methods 0.000 claims description 3
- 238000012544 monitoring process Methods 0.000 claims description 3
- 238000005373 pervaporation Methods 0.000 claims description 3
- 230000008595 infiltration Effects 0.000 claims description 2
- 238000001764 infiltration Methods 0.000 claims description 2
- 238000002347 injection Methods 0.000 claims description 2
- 239000007924 injection Substances 0.000 claims description 2
- 230000035699 permeability Effects 0.000 claims description 2
- 238000000502 dialysis Methods 0.000 abstract description 12
- 238000011282 treatment Methods 0.000 description 12
- 238000005516 engineering process Methods 0.000 description 9
- 238000001223 reverse osmosis Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 230000007704 transition Effects 0.000 description 4
- 238000005342 ion exchange Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 238000004659 sterilization and disinfection Methods 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 1
- 229910001423 beryllium ion Inorganic materials 0.000 description 1
- 208000020832 chronic kidney disease Diseases 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000006298 dechlorination reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000005593 dissociations Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 208000028208 end stage renal disease Diseases 0.000 description 1
- 201000000523 end stage renal failure Diseases 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 230000037427 ion transport Effects 0.000 description 1
- 238000010030 laminating Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000005325 percolation Methods 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
- 238000002834 transmittance Methods 0.000 description 1
- 238000011277 treatment modality Methods 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 238000000870 ultraviolet spectroscopy Methods 0.000 description 1
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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
- C02F1/4693—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
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
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- Life Sciences & Earth Sciences (AREA)
- Electrochemistry (AREA)
- Analytical Chemistry (AREA)
- Molecular Biology (AREA)
- Health & Medical Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention provides a dialysis water purification device based on a bipolar ion membrane and a water purification method thereof, raw water to be treated stored in a water storage device to be treated passes through a deionization regeneration type module at one time, purified water treated by the deionization regeneration type module is stored in a purified water storage device, and pure water injected into a concentration chamber is stored in a circulating water storage device; the water flowing out from the anode chamber of the pure water enters an anode circulating water tank, the water flowing out from the cathode chamber enters a cathode circulating water tank, and the pure water and the circulating water respectively circulate again and flow into a concentration chamber of the deionization module together.
Description
Technical Field
The invention belongs to the technical field of pervaporation water purification treatment, and particularly relates to a pervaporation water purification device based on a bipolar ion membrane and a water purification method thereof.
Background
Each dialysis patient needs 30 liters of water per hour during dialysis treatment, and each treatment needs 150 liters of water per hour. Home dialysis must be feasible using on-site water production techniques. The preparation of dialysis water used in hospitals at present comprises the following steps: 1) dechlorination by activated carbon, 2) softening, 3) ultrafiltration, 4) primary reverse osmosis, 5) secondary reverse osmosis and 6) sterilization. Each step uses separate equipment, the steps together require a tens of square meters of equipment room, and the water yield of reverse osmosis decreases with decreasing temperature, so a 25 degree temperature must be maintained in the room. The use and maintenance costs of these devices are also high, such as 2) softening described above, requiring continuous addition of salt for regeneration of the ion exchange resin. 4) And 5) the reverse osmosis membrane needs to be replaced every 10 to 12 months. The market demand is huge, and the current situation can not satisfy the market demand far away. According to incomplete statistics, about 26 ten thousand patients who receive dialysis treatment in hospitals in our country, but up to 200 ten thousand patients who need dialysis treatment for end-stage renal disease. The number of people requiring treatment increases at a rate approaching two-digit percentage each year. Recent research in the medical field indicates that the survival rate of patients can be doubled by using a short-time dialysis treatment mode of 5-6 times per week compared with the traditional dialysis treatment mode of 2-3 times per week. This new treatment modality is currently growing in two-digit hundreds of years in both europe and japan in the united states. In addition, the device has positive effects on facilitating the treatment of patients, relieving the load of hospital beds, reducing the burden of patients and reducing the treatment cost.
At present, the technology adopted for preparing domestic dialysis water is a double-membrane reverse osmosis technology. The treatment technology of the medical dialysis water at foreign countries is also mainly a double-membrane reverse osmosis technology. Some new deionization technologies based on electrochemical technology are adopted to a certain extent in the year, but the adoption of the technologies is limited because the technologies also need to be matched with disinfection technologies to reach the standard of dialysis water.
Disclosure of Invention
In order to solve the above technical problem, the present invention provides a water purification apparatus for percolation based on a bipolar ion membrane, comprising: the system comprises a deionization regeneration type module, a to-be-treated water storage device, a purified water storage device, a circulating water storage device, an anode circulating water tank and a cathode circulating water tank;
the right and left sides of the deionization regeneration type module are respectively provided with an anode chamber and a cathode chamber, the end part of the anode chamber is provided with an anode, the end part of the cathode chamber is provided with a cathode, two concentration chambers and two deionization chambers are arranged between the anode chamber and the cathode chamber, the two deionization chambers are arranged at the central part of the deionization regeneration type module in a bilateral symmetry manner, and the two concentration chambers are arranged at the outer sides of the two deionization chambers in a bilateral symmetry manner;
the deionization chamber and the concentration chamber on the anode side are separated by an anion exchange membrane, the deionization chamber and the concentration chamber on the cathode side are separated by a cation exchange membrane, the two deionization chambers are separated by a bipolar ion membrane, and anion exchangers are filled in the deionization chamber and the concentration chamber on the anode side; the deionization chamber and the concentration chamber on the cathode side are filled with cation exchangers; the anode chamber and the adjacent concentrating chamber, and the cathode chamber and the adjacent concentrating chamber are separated by a fluorine ion exchange membrane with a water through hole;
pure water injected into the concentration chamber is stored in the circulating water storage;
and water flowing out of the anode chamber enters the anode circulating water tank, water flowing out of the cathode chamber enters the cathode circulating water tank, and the water and the circulating water respectively circulate again and flow into the concentration chamber of the deionization module together.
Further, the bipolar ionic membrane is formed by compounding a cation exchange layer, an anion exchange layer and an intermediate catalyst layer, and a plurality of grooves with the diameter of about 150 μm can be formed on the membrane surface of the bipolar ionic membrane; the bipolar ionic membrane generates water dissociation reaction under the action of a direct current electric field to generate H+And OH-Ions enter the deionization chambers on two sides.
Further, a water inlet A to be treated is arranged at the top of the deionization chamber on the anode side, and a treated water outlet B is arranged at the bottom of the deionization chamber; a treated water inlet C is arranged at the bottom of the deionization chamber on the cathode side, and a purified water outlet D is arranged at the top of the deionization chamber; the top parts of the two concentration chambers are respectively provided with a process water injection port E, and the side ends of the anode chamber and the cathode chamber are respectively provided with a discharge port F.
Furthermore, the anion exchange membrane and the cation exchange membrane are prepared by adopting ion exchange resin or a monolithic organic porous ion exchanger or alternatively laminating the anion exchange membrane and the cation exchange membrane, and the liquid transmittance is 1/100-1/1000.
Further, the circulating water storage adopts pure water with the conductivity of less than 1 muS/cm.
Furthermore, a plurality of small holes are uniformly distributed in the fluorine ion exchange membrane with the water through hole, circulating water flows into the water through hole, and ions concentrated near the fluorine ion exchange membrane with the water through hole can be discharged to the anode chamber side or the cathode chamber side.
Further, the membrane surface of the bipolar ionic membrane may be provided with a plurality of grooves having a diameter of about 150 μm.
The invention also provides a water purification method realized according to the osmosis water purification equipment, raw water to be treated stored in a water storage device to be treated passes through the deionization regeneration type module at one time, purified water treated by the deionization regeneration type module is stored in the purified water storage device, and pure water injected into the concentration chamber is stored in the circulating water storage device; the water flowing out from the anode chamber of the pure water enters an anode circulating water tank, the water flowing out from the cathode chamber enters a cathode circulating water tank, and the pure water and the circulating water respectively circulate again and flow into a concentration chamber of the deionization module together.
Furthermore, the current efficiency and the removal efficiency of the deionization regenerative module are determined by monitoring the purified water in the purified water storage at regular time,
current efficiency:
in the formula etaeFor current efficiency, Q is NO3 -F is the Faraday constant, N (NO)3 -) For NO transferred to the anode concentrating compartment3 -I is the current, t is the reactor run time;
removing efficiency: p ═ p (ρ)i-ρf)×100％/ρi；
In the formula, ρiAnd ρfIs respectively water inlet and outlet NO3 --mass concentration of N.
Further, the deionization regeneration type module is used for regenerating the resin of the anion/cation exchanger, and under the action of a direct current electric field, the middle catalyst layer of the bipolar ion membrane generates dissociation reaction to generate H+、OH-Ions, respectively, passing through cation exchangeThe exchange layer and the anion exchange layer migrate to the cathode and anode, H+Exchange reaction with cation in the resin of the spent cation exchanger, OH-And the anion exchange resin and the anion in the resin of the failed anion exchanger are subjected to displacement reaction, and simultaneously, the displaced cation and anion respectively migrate to the cathode chamber and the anode chamber, so that the regeneration of the anion exchange resin and the cation exchange resin is realized.
Drawings
Fig. 1 is a schematic structural diagram of a water percolating and purifying device based on bipolar ionic membrane according to the present invention;
fig. 2 is a schematic structural diagram of a deionization regeneration module in a water purification apparatus according to the present invention;
fig. 3 is a schematic structural diagram of a bipolar ion membrane in a water purification device according to the present invention;
Detailed Description
The technical scheme of the invention is specifically explained below with reference to the accompanying drawings. It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the disclosure. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments according to the present application. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
Fig. 1 is a schematic structural diagram of a water percolating and purifying device based on bipolar ionic membrane according to the present invention; this infiltration analyse water purification unit includes: a deionized regenerative module 100, a water to be treated storage 10, a purified water storage 20, a circulating water storage 50, an anode circulating water tank 30 and a cathode circulating water tank 40.
The raw water to be treated stored in the water storage 10 to be treated passes through the deionization regeneration type module 100 at a time, and the purified water treated by the deionization regeneration type module is stored in the purified water storage 20. The current efficiency and removal efficiency of the deionization regeneration module 100 are determined by periodically monitoring the purified water in the purified water storage 20.
In the deionization regeneration process, the current efficiency and the removal efficiency are important criteria for evaluating the advantages and the disadvantages of a deionization regeneration type module, and the 2 parameters are adopted to evaluate the treatment effect.
Current efficiency:
in the formula etaeFor current efficiency, Q is NO3 -F is the Faraday constant (96485C/mol), N (NO)3 -) For NO transferred to the anode concentrating compartment3 -I is the current and t is the reactor run time.
Removing efficiency: p ═ p (ρ)i-ρf)×100％/ρi；
In the formula, ρiAnd ρfIs respectively water inlet and outlet NO3 -Mass concentration of-N, NO3 —The content of N was measured by UV spectrophotometry using HJ/T346-2007.
Fig. 2 is a schematic structural diagram of a deionization regeneration type module in the osmosis water purification device of the present invention. The deionization regeneration type module 100 is a 6-cell organic glass reactor, the left side and the right side of the deionization regeneration type module 100 are respectively provided with an anode chamber 101 and a cathode chamber 102, the end part of the anode chamber 101 is provided with an anode, the end part of the cathode chamber 101 is provided with a cathode, two concentration chambers 108 and 109 and two deionization chambers 106 and 107 are arranged between the anode chamber 101 and the cathode chamber 102, the two deionization chambers 106 and 107 are arranged at the central part of the deionization regeneration type module 100 in a bilateral symmetry manner, and the two concentration chambers 108 and 109 are arranged at the outer sides of the two deionization chambers 106 and 107 in a bilateral symmetry manner.
The deionization chamber 106 and the concentration chamber 108 are partitioned by an anion exchange membrane 111 on the anode side, the deionization chamber 107 and the concentration chamber 109 are partitioned by a cation exchange membrane 112 on the cathode side, the deionization chambers 106 and 107 are partitioned by a bipolar ion membrane 113, and anion exchangers are filled in the deionization chamber 106 on the anode side and the concentration chamber 108 on the anode side; the cathode-side deionization chamber 107 and the cathode-side concentration chamber 109 are filled with cation exchangers.
The anode chamber 101 and the concentrating chamber 108, and the cathode chamber 102 and the concentrating chamber 109 are separated by a fluorine ion exchange membrane 114 having a water passage.
A water inlet A to be treated is arranged at the top of the deionization chamber 106, and a treated water outlet B is arranged at the bottom; a treated water inlet C is provided at the bottom of the deionization chamber 107, and a purified water outlet D is provided at the top.
Circulating water inlets E are provided at the top of the concentrating chambers 108 and 109, and outlets F are provided at the side ends of the anode chamber 101 and the cathode chamber 102.
A plurality of small holes are uniformly distributed in the fluorine-based ion exchange membrane with water passage holes, and ions concentrated in the vicinity of the fluorine-based ion exchange membrane with water passage holes can be discharged to the anode chamber 101 or the cathode chamber 102 side by the circulating water flowing into the water passage holes.
The anion exchange membrane 111 and the cation exchange membrane 112 are ion exchange membranes having a liquid permeability of about 1/100 to 1/1000.
The electrode is preferably in a shape in which the electric field distribution is uniform and the discharge of the liquid is not hindered, and a rod-like, mesh-like, or ring-like electrode can be used. The material is not particularly limited, and platinum having corrosion resistance is preferable. The power supply may be incorporated into the deionization regeneration module, or an external power supply may be used, preferably a dc power supply, but may also be an ac power supply.
The circulating water storage 50 stores pure water injected into the concentration chamber of the deionization regeneration module 100, and pure water having an electric conductivity of 1 μ S/cm or less is generally used for discharging the moved ions to the electrode chamber. The water flowing out of the anode chamber enters the anode circulation water tank, and the water flowing out of the cathode chamber enters the cathode circulation water tank, and is circulated again and flows into the concentration chamber of the deionization module 100 together with the circulating water.
The structure of the bipolar ion membrane 113 is different from that of a common ion exchange membrane, as shown in fig. 3, the bipolar ion membrane is formed by combining a cation exchange layer, an anion exchange layer and an intermediate catalyst layer, and is similar to a sandwich structure, and the bipolar ion membrane undergoes a water dissociation reaction under the action of a direct current electric field to generate H+And OH-Ions. There are two ion transport modes in bipolar ion membranes depending on the direction of the applied voltage. Under the drive of a forward direct current electric field, anions on the right side of the anion exchange layer of the bipolar ionic membrane migrate into the anion exchange layer, cations on the left side of the cation exchange layer migrate into the cation exchange layer, and the ion concentration of a transition region between the anion exchange layer and the cation exchange layer is increased. When the reverse voltage is small, positive ions and negative ions in the solution respectively penetrate through the cation exchange layer and the anion exchange layer and move from the transition region to the cathode and the anode, the ion concentration in the transition region is reduced, the resistance of the membrane is reduced, when the reverse voltage is increased to a certain value, the ion amount fed in from the outside of the membrane through diffusion and permeation is not enough to counteract the ion amount lost by electromigration, so that the ions in the transition region are exhausted to form a high potential gradient, the bipolar ion membrane is subjected to water dissociation, and the generated H is generated+、OH-Into the two-sided membrane deionization chambers, i.e., deionization chambers 106 and 107 in fig. 2.
In a preferred embodiment, the membrane surface of the bipolar ionic membrane may be provided with a plurality of grooves having a diameter of about 150 μm, which increase the packing density of the ion exchange membrane by about two times, thereby achieving a faster ion exchange rate.
The cation exchanger and the anion exchanger are those having an ion exchange function, and may be ion exchange resins, monolithic organic porous ion exchangers, or the like, and two or more kinds of these ion exchangers may be alternately stacked as appropriate and used in a mixed phase as long as they have an ion exchange capacity of cations or anions. The deionization regeneration type module can be used for regenerating resin, and the middle catalyst layer of the bipolar ion membrane generates dissociation reaction under the action of a direct current electric field to generate H+、OH-Ions, which migrate through the cation exchange layer and the anion exchange layer to the anode and the cathode, respectively, H+Exchange reaction with cation in spent cation exchange resin, OH-And the anion exchange resin and the anion in the ineffective anion exchange resin are subjected to displacement reaction, and simultaneously, the displaced cation and anion respectively migrate to the cathode chamber and the anode chamber, so that the regeneration of the anion exchange resin and the cation exchange resin is realized.
The number of apparatuses and the scale of the process described herein are intended to simplify the description of the present invention. Applications, modifications and variations of the present invention will be apparent to those skilled in the art.
While embodiments of the invention have been disclosed above, it is not intended to be limited to the uses set forth in the specification and examples. It can be applied to all kinds of fields suitable for the present invention. Additional modifications will readily occur to those skilled in the art. It is therefore intended that the invention not be limited to the exact details and details shown and described herein, but should be construed according to the broad principles defined by the appended claims and their equivalents.
Claims (10)
1. A water purification unit is analysed to infiltration based on bipolar ionic membrane usefulness, its characterized in that includes: the system comprises a deionization regeneration type module, a to-be-treated water storage device, a purified water storage device, a circulating water storage device, an anode circulating water tank and a cathode circulating water tank;
the right and left sides of the deionization regeneration type module are respectively provided with an anode chamber and a cathode chamber, the end part of the anode chamber is provided with an anode, the end part of the cathode chamber is provided with a cathode, two concentration chambers and two deionization chambers are arranged between the anode chamber and the cathode chamber, the two deionization chambers are arranged at the central part of the deionization regeneration type module in a bilateral symmetry manner, and the two concentration chambers are arranged at the outer sides of the two deionization chambers in a bilateral symmetry manner;
the deionization chamber and the concentration chamber on the anode side are separated by an anion exchange membrane, the deionization chamber and the concentration chamber on the cathode side are separated by a cation exchange membrane, the two deionization chambers are separated by a bipolar ion membrane, and anion exchangers are filled in the deionization chamber and the concentration chamber on the anode side; the deionization chamber and the concentration chamber on the cathode side are filled with cation exchangers; the anode chamber and the adjacent concentrating chamber, and the cathode chamber and the adjacent concentrating chamber are separated by a fluorine ion exchange membrane with a water through hole;
pure water injected into the concentration chamber is stored in the circulating water storage;
and water flowing out of the anode chamber enters the anode circulating water tank, water flowing out of the cathode chamber enters the cathode circulating water tank, and the water and the circulating water respectively circulate again and flow into the concentration chamber of the deionization module together.
2. The apparatus according to claim 1, wherein the bipolar ionic membrane is composed of a cation exchange layer, an anion exchange layer and an intermediate catalyst layer, and the membrane surface of the bipolar ionic membrane is provided with a plurality of grooves with the diameter of about 150 μm; the bipolar ionic membrane generates water dissociation reaction under the action of a direct current electric field to generate H+And OH-Ions enter the deionization chambers on two sides.
3. The apparatus according to claim 1, wherein a treated water inlet a is provided at the top and a treated water outlet B is provided at the bottom of the deionization chamber on the anode side; a treated water inlet C is arranged at the bottom of the deionization chamber on the cathode side, and a purified water outlet D is arranged at the top of the deionization chamber; the top parts of the two concentration chambers are respectively provided with a process water injection port E, and the side ends of the anode chamber and the cathode chamber are respectively provided with a discharge port F.
4. The apparatus of claim 1, wherein the anion exchange membrane and the cation exchange membrane are prepared by alternately stacking ion exchange resins or monolithic organic porous ion exchangers or both, and have a liquid permeability of 1/100-1/1000.
5. The apparatus according to claim 1, wherein the circulating water reservoir is pure water having an electrical conductivity of 1 μ S/cm or less.
6. The apparatus according to claim 1, wherein the fluorine-based ion exchange membrane having a water passage hole has a plurality of small holes uniformly distributed therein, and circulating water flows into the water passage hole, so that ions concentrated in the vicinity of the fluorine-based ion exchange membrane having a water passage hole can be discharged to the anode chamber or the cathode chamber side.
7. The apparatus according to claim 1, wherein the bipolar ionic membrane has a plurality of grooves with a diameter of about 150 μm on the membrane surface.
8. The water purification method implemented by the pervaporation water purification apparatus according to any of claims 1 to 7, wherein the raw water to be treated stored in the water reservoir to be treated is once passed through the deionization regeneration type module, the purified water treated by the deionization regeneration type module is stored in the purified water reservoir, and the purified water injected into the concentration chamber is stored in the circulating water reservoir; the water flowing out from the anode chamber of the pure water enters an anode circulating water tank, the water flowing out from the cathode chamber enters a cathode circulating water tank, and the pure water and the circulating water respectively circulate again and flow into a concentration chamber of the deionization module together.
9. The water purification method of claim 8, wherein the current efficiency and removal efficiency of the deionization regeneration module are determined by periodically monitoring the purified water in the purified water storage,
current efficiency:
in the formula etaeFor current efficiency, Q is NO3 -F is the Faraday constant, N (NO)3 -) For NO transferred to the anode concentrating compartment3 -I is the current, t is the reactor run time;
removingEfficiency p ═ p (p)i-ρf)×100％/ρi；
In the formula, ρiAnd ρfIs respectively water inlet and outlet NO3 --mass concentration of N.
10. The water purification method of claim 8, wherein the deionization regeneration module is used for regenerating the resin of the anion/cation exchanger, and the intermediate catalyst layer of the bipolar ion membrane undergoes dissociation reaction under the action of the direct current electric field to generate H+、OH-Ions, which migrate through the cation exchange layer and the anion exchange layer to the anode and the cathode, respectively, H+Exchange reaction with cation in the resin of the spent cation exchanger, OH-And the anion exchange resin and the anion in the resin of the failed anion exchanger are subjected to displacement reaction, and simultaneously, the displaced cation and anion respectively migrate to the cathode chamber and the anode chamber, so that the regeneration of the anion exchange resin and the cation exchange resin is realized.
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2128556Y (en) * | 1992-01-21 | 1993-03-24 | 国家海洋局杭州海水淡化和水处理技术开发中心 | Convex and concave ion-exchanging film |
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