CN201021439Y - An antiscaling electric ion removal and cleaning device and recycling negative ion and positive ion - Google Patents
An antiscaling electric ion removal and cleaning device and recycling negative ion and positive ion Download PDFInfo
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- CN201021439Y CN201021439Y CNU2007201054998U CN200720105499U CN201021439Y CN 201021439 Y CN201021439 Y CN 201021439Y CN U2007201054998 U CNU2007201054998 U CN U2007201054998U CN 200720105499 U CN200720105499 U CN 200720105499U CN 201021439 Y CN201021439 Y CN 201021439Y
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- 150000002500 ions Chemical class 0.000 title description 14
- 238000004140 cleaning Methods 0.000 title description 3
- 238000004064 recycling Methods 0.000 title 1
- 239000012528 membrane Substances 0.000 claims abstract description 16
- 239000003011 anion exchange membrane Substances 0.000 claims abstract description 12
- 239000003014 ion exchange membrane Substances 0.000 claims description 19
- 239000011347 resin Substances 0.000 claims description 19
- 229920005989 resin Polymers 0.000 claims description 19
- 238000009296 electrodeionization Methods 0.000 claims description 16
- 125000002091 cationic group Chemical group 0.000 claims description 12
- 238000011049 filling Methods 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
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 141
- 239000002253 acid Substances 0.000 abstract description 8
- 239000003957 anion exchange resin Substances 0.000 abstract description 5
- 239000003729 cation exchange resin Substances 0.000 abstract description 3
- 238000005341 cation exchange Methods 0.000 abstract description 2
- 150000001450 anions Chemical class 0.000 abstract 3
- 150000001768 cations Chemical class 0.000 abstract 2
- 238000010276 construction Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 10
- 241000668709 Dipterocarpus costatus Species 0.000 description 7
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Substances [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 6
- 238000007747 plating Methods 0.000 description 6
- 239000000243 solution Substances 0.000 description 5
- 238000007599 discharging Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 230000005684 electric field Effects 0.000 description 3
- 238000000909 electrodialysis Methods 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- VWDWKYIASSYTQR-UHFFFAOYSA-N Sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 238000010349 cathodic reaction Methods 0.000 description 2
- XFXPMWWXUTWYJX-UHFFFAOYSA-N cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 2
- 238000002242 deionisation method Methods 0.000 description 2
- 239000008151 electrolyte solution Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxyl anion Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 150000001457 metallic cations Chemical class 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 230000001105 regulatory Effects 0.000 description 2
- 239000002455 scale inhibitor Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate dianion Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- 239000004793 Polystyrene Substances 0.000 description 1
- 239000005092 Ruthenium Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid Chemical class OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 1
- 150000001253 acrylic acids Chemical class 0.000 description 1
- 238000005349 anion exchange Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 230000003750 conditioning Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000003411 electrode reaction Methods 0.000 description 1
- 238000009713 electroplating Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 125000004435 hydrogen atoms Chemical class [H]* 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L na2so4 Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- 229920002223 polystyrene Polymers 0.000 description 1
- 238000004382 potting Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- KJTLSVCANCCWHF-UHFFFAOYSA-N ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 229940001516 sodium nitrate Drugs 0.000 description 1
- 235000010344 sodium nitrate Nutrition 0.000 description 1
- 239000004317 sodium nitrate Substances 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- -1 sodium-chlor Chemical compound 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 125000003011 styrenyl group Chemical class [H]\C(*)=C(/[H])C1=C([H])C([H])=C([H])C([H])=C1[H] 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000012498 ultrapure water Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Abstract
The utility model discloses a scale-free electrically-deionizing water-purifying device which can reclaim anions and cations. The electrically deionizing device consists of five separate chambers which are, in order, respectively an anode chamber containing the anode, a first thin chamber filled with cation exchange resin, a thick chamber, a second thin chamber filled with anion exchange resin and a cathode chamber containing the cathode, wherein, two sides of the first thin chamber are respectively separated from the anode chamber and the thick chamber with two cation exchange membranes; two sides of the second thin chamber are respectively separated from the thick chamber and the cathode chamber with two anion exchange membranes. After a voltage is applied between the anode and the cathode, the anode-side water, the cathode-side water and the thick water are respectively recycled and partially renewed periodically; the raw water successively passes through the first thin chamber and the second thin chamber and then is turned into pure water. The construction of a membrane stack keeps an acid environment in the thick room and therefore inhibits scaling on the anion membrane surface; electrode water comes from split streams of pure water, avoiding scaling on the cathode surface; anions and cations in the raw water are concentrated in the thick water, and can be recycled.
Description
Technical field
The utility model relates to a kind of electrodeionization water-purifying device that does not have fouling and reclaim zwitterion.
Background technology
Electrodeionization (electrodeionization, being called for short EDI) packed-bed electrodialysis in early days is otherwise known as, be that electrodialysis and ion-exchange are organically combined, filling ion-exchange resin between the ion-exchange membrane of electrodialysis unit freshwater room is realized a kind of new separation technology that deionization is operated under the effect of applying direct current electric field.It can need not under the chemical acid alkali regenerated condition low concentration solution to be carried out advanced desalination.In recent years, the EDI development is very rapid, is used for pure water and high purity water preparation at many industrial circles such as medicine, electric power, electronics, food, and has also begun preliminary application in industries such as plating.
Yet since the seventies in 20th century, EDI is subjected to the puzzlement of auto levelizer fouling always.In the EDI operational process, the OH that the water decomposition reaction that cathodic reaction and the polarization of light chamber cause is produced
-Ion, the female die surface in negative electrode and dense chamber form partial strong basicity environment.In former water, electrode water or the water inlet of dense chamber, HCO is arranged
3 -And Ca
2+, Mg
2+When existing, easily form the carbonate and the precipitation of hydroxide of metal,, cause the membrane stack fouling attached to the female die surface of negative electrode and dense chamber Deng metal ion.Fouling has a strong impact on the steady running of electrodeionization process, makes membrane stack resistance increase, and equipment performance descends, and produces water water quality and reduces, and the useful matter in the former water can't reclaim smoothly, has also seriously limited popularization and the use of electrodeionization technology on water treatment industry.
The measure that prevents the fouling of EDI device at present has: the utmost point (patent US4956071, EP0379116 and US5026465); Add acid and reduce former water pH value (patent EP0916620 and US6017433); In dense power and water utmost point water, add Scale inhibitors (patent US6056878); Former water softens (patent EP1090885) by positive resin in advance; Dense water and fresh water counter-current operation reach at ion-exchange membrane of dense chamber increase dense chamber are divided into two chambers (patent US6149788 and CN1323279A); In dense chamber potting resin and two EDI device operated in series (patent US6187162 and US6296751).These measures can prevent fouling to a certain extent, but also have separately defective and weak point.Frequently pole-reversing makes device and flow process more complicated loaded down with trivial details, and the water conditioning of switching behind the electrode needs certain hour, and it is lower to produce water water quality.Former water acidifying needs a large amount of acid of extra adding, and product water is acid.Adopt Scale inhibitors to increase the use of chemical agent, reduce effluent characteristics.Softening and operated in series makes the device complexity to former water with positive resin in advance, and cost increases, and the acid-alkali regeneration of resin easily causes secondary pollution.Counter-current operation and special dense cell structure design requirements utmost point water and dense water can not recycle, and need constantly in utmost point chamber and the water inlet of dense chamber, to inject salts solution to keep its electroconductibility, cause the consumption of water and chemical very big, in addition, whole flow process intermediate ion distributes very inhomogeneous, increased the ununiformity of membrane stack internal resistance, for the operation of the long-term stability of EDI, its practicality remains practice test.
Summary of the invention
The purpose of this utility model is the deficiency that exists at prior art, and a kind of electrodeionization water-purifying device that does not have fouling and reclaim zwitterion is provided.
No fouling and the electrodeionization water-purifying device that reclaims zwitterion are made up of five compartments, and the order of compartment respectively is anolyte compartment, the first light chamber, dense chamber, the second light chamber, cathode compartment; Be provided with first cationic exchange membrane between the anolyte compartment and the first light chamber, be provided with second cationic exchange membrane between the first light chamber and the dense chamber, filling male ion-exchange resin in the first light chamber; Be provided with first anion-exchange membrane between the dense chamber and the second light chamber, be provided with second anion-exchange membrane between the second light chamber and the cathode compartment, fill anionite-exchange resin in the second light chamber; In the anolyte compartment, be provided with anode, in cathode compartment, be provided with negative electrode.
Described ion-exchange membrane is homogeneous ion-exchange membrane or heterogeneous ion-exchange membrane.
Compared with prior art, the utlity model has following advantage:
(1) can effectively prevent fouling, and apparatus system is simple comprehensively, easy to operate, practical;
(2) can produce pure water continuously and stably, the zwitterion in the former water obtains reclaiming simultaneously, has improved resource utilization;
(3) can use homogeneous ion-exchange membrane, also can use heterogeneous ion-exchange membrane, cost reduces;
(4) anion and cation exchange resin is separately filled, and light chamber resistance reduces, the current efficiency height, and energy consumption reduces;
(5) utmost point water and dense water all recycle, the utilization ratio height of water.
Description of drawings
Fig. 1 is no fouling and the electrodeionization water-purifying device structural representation that reclaims zwitterion;
Fig. 2 is an electrodeionization water-purifying process schematic flow sheet of the present utility model.
Among the figure: 1, the first light chamber 2, anolyte compartment, 3, the second light chamber 4, dense chamber, cathode compartment 5, anode 6, first cationic exchange membrane 7, second cationic exchange membrane 8, Zeo-karb 9, the first anion-exchange membranes 10, second anion-exchange membrane 11, anionite-exchange resin 12, negative electrode 13, electric deionizer 14, valve 15, dense water cycle jar 16, pump 17, pH meter 18, utmost point water pot 19, anode water circulation tank 20, negative electrode water cycle jar 21, waste liquid tank 22, agitator 23, under meter 24.
Embodiment
As shown in Figure 1, no fouling and the electrodeionization water-purifying device that reclaims zwitterion are made up of five compartments, and the order of compartment respectively is 1, the first light chamber 2, anolyte compartment, 3, the second light chamber 4, dense chamber, cathode compartment 5; Be provided with between first cationic exchange membrane light chambers 27, the first and the dense chamber 3 between the anolyte compartment 1 and the first light chamber 2 and be provided with second cationic exchange membrane 8, filling male ion-exchange resin 9 in the first light chamber 2; Be provided with between the dense chamber 3 and the second light chamber 4 to be provided with between first anion-exchange membrane light chambers 4 10, the second and the cathode compartment 5 and fill anionite-exchange resin 12 in the second anion-exchange membrane light chambers 4 11, the second; In anolyte compartment 1, be provided with anode 6, in cathode compartment 5, be provided with negative electrode 13.
Described ion-exchange membrane is homogeneous ion-exchange membrane or heterogeneous ion-exchange membrane.
No fouling is also reclaimed the electrodeionization process for purifying water of zwitterion: add voltage at the device two ends, successively the flow through first light chamber 2 and the second light chamber 4 of anolyte compartment water inlet, cathode compartment water inlet and the water inlet of dense chamber flow through respectively anolyte compartment 1, cathode compartment 5 and dense chamber 3 and recycle, former water produces pure water.Described anolyte compartment, cathode compartment water inlet are from the pure water shunting, and the water inlet of dense chamber is from former moisture flow.The anode water that recycles, negative electrode water and dense water need regular partial update, and the anode water that recycles, negative electrode water more new portion are shunted from pure water, and more new portion is from former moisture flow for the dense water that recycles, and the dense water of discharge is recycled.For increasing the electroconductibility of utmost point water, in the pure water shunting, add electrolyte solution, ionogen is sodium sulfate, SODIUMNITRATE or sodium-chlor.
Metallic cation C in the former water
+With negatively charged ion A
-Successively by Zeo-karb 9 and anionite-exchange resin 12 absorption and remove, former water obtains purifying.Anodic reaction: 2H takes place in anolyte compartment 1
2O-4e → O
2+ 4H
+, the H of generation
+Under effect of electric field, pass first cationic exchange membrane 7 and enter the first light chamber 2, a part of H
+The Zeo-karb that wherein lost efficacy is regenerated another part H
+The positively charged ion C that gets off with desorb
+Then pass second cationic exchange membrane 8 and enter dense chamber 3.Simultaneously, cathodic reaction: 4H takes place in cathode compartment 5
2O+4e → 2H
2+ 4OH
-, the OH of generation
-Pass second anion-exchange membrane 11 and enter the second light chamber 4, a part of OH
-The anionite-exchange resin that wherein lost efficacy is regenerated another part OH
-The negatively charged ion A that gets off with desorb
-Pass first anion-exchange membrane 10 and also enter dense chamber 3.In the middle of all ions, H
+Electromigration speed be maximum, secondly be OH
-, therefore, in the identical time, migrate to the H of dense chamber 3
+Amount always greater than OH
-Amount, it is acid that the solution in the dense chamber 3 are all the time, metallic cation C
+Can't form its precipitation of hydroxide, suppress the fouling on first anion-exchange membrane, 10 surfaces.Utmost point water is shunted from pure water, and the fouling on negative electrode 13 surfaces also is avoided.
Water-purifying process flow process of the present utility model as shown in Figure 2.Each passes through valve 15, pump 17 and under meter 24 regulating and controlling into and out of current and flow.Between the cathode and anode of electric deionizer 14, add voltage, dense water circulates between dense chamber 3 and dense water cycle jar 16, dense acidity of water is by pH meter 18 on-line determinations, anode water circulates between anolyte compartment 1 and anode water circulation tank 20, negative electrode water circulates between cathode compartment 5 and negative electrode water cycle jar 21, successively the flow through first light chamber 2 and the second light chamber 4 of former water produces pure water, make utmost point water at the by-passing portions adding electrolyte solution of pure water and store in utmost point water pot 19, and utmost point water is introduced anode water circulation tank 20 and negative electrode water cycle jar 21 respectively.Yin, yang ion in the former water is removed the H that electrode reaction produced by being held back by resin
+And OH
-Migrate to the first light chamber 2 and the second light chamber 4 respectively, the Zeo-karb and the anionite-exchange resin that wherein lost efficacy are regenerated the positively charged ion in the former water that desorb is got off and negatively charged ion and section H
+And OH
-Migrate to dense chamber 3 together.Along with the operation of device, the dense water concentration that circulates increases, and circulating anode water pH value reduces, and circulation negative electrode water pH value raises.Dense water concentration is crossed conference and is caused ionic concentration gradient increase between dense water and the fresh water, and dense chamber 3 is to the concentration diffusion aggravation of light chamber 2 and 4, and deionization weakens, and fresh water water quality reduces.Anode water pH value is low excessively, the too high meeting of negative electrode water pH value causes a large amount of H
+And OH
-Also migrate to dense chamber 3, cause current efficiency to descend by effect of electric field.Therefore, at set intervals, need to discharge a part of dense water, anode water and negative electrode water, concentrated water drainage goes out part and is replenished by former water equal-volume, and cathode and anode water discharge section is replenished by the utmost point water equal-volume in the utmost point water pot 19.The recyclable utilization of dense water of discharging, the acid anode water of discharge and alkaline negative electrode water are mixed in waste liquid tank 22, discharging after agitator 23 stirs.
Described no fouling is also reclaimed the electrodeionization process for purifying water of zwitterion, and callable positively charged ion comprises Ca
2+, Mg
2+, Ba
2+, Fe
3+, Al
3+, Cd
2+, Pb
2+, Cr
3+, Cu
2+, Zn
2+, Ni
2+, Co
2+, Sn
2+, Cu (NH
3)
4 2+, NH
4 +, negatively charged ion comprises NO
3 -, NO
2 -, PO
4 3-, CN
-, F
-, Cr
2O
7 2-, Ag (CN)
2 -, Au (CN)
2 -, Cd (CN)
4 2-, Zn (CN)
4 2-, Cu (CN)
3 -
Embodiment 1
Adopt five compartment electric deionizers shown in Figure 1 to produce pure water, technical process as shown in Figure 2.Anode is a titanium plating ruthenium mesh electrode, and negative electrode is the netted electrode of stainless steel.Anion and cation exchange resin is respectively D201 macroporous strong basic styrene series negative resin and D001 macropore strong acid polystyrene sun resin, and positive resin is a Hydrogen, and negative resin is a hydroxyl type.The yin, yang ion-exchange membrane is respectively homemade DF120 homogeneous-phase anion exchange film and DF120 homogeneous phase cation exchange film.The useful area of film and electrode is 150cm
2, intermembranous apart from 0.8cm, electrode vessel thickness 1.6cm, the first light chamber and the second light chamber are filled the cationic, anionic exchange resin of about 120ml respectively.Former water is the tap water behind mechanical filter.At first, a small amount of former water carries out purifying by the first light chamber and the second light chamber of electric deionizer successively, the second light chamber water outlet is mixed with the Na of 25mg/L
2SO
4Solution is as utmost point water.Open transfusion system, former water, dense water, anode and cathode water are flowed through pipeline separately, add 20V voltage, former water is carried out electrodeionization handle at the device electrode two ends.Every 5-10 hour, dense water, anode and cathode water are carried out partial update, the mixed evenly back discharging of the dense water regulating YIN and YANG utmost point water of discharge.The product water conductivity 0.10-0.20 μ S/cm that under above-mentioned processing condition, makes, water production rate 80-120L/h.
Embodiment 2
Yin, yang ion-exchange membrane among the embodiment 2 is homemade out-phase yin, yang ion-exchange membrane; The useful area of film and electrode is expanded as 900cm
2The first light chamber and the second light chamber are filled the cationic, anionic exchange resin of about 720ml respectively; Former water is the plating piece rinse water that Electroplate Factory's nickel plating production line is discharged, and wherein contains Ni
2+About 50mg/L, SO
4 2-About 82mg/L, pH value about 6; Add 60V voltage at the device electrode two ends; All the other device parts and water purification flow path are all identical with embodiment 1.Under the aforesaid operations condition, electric deionizer continous-stable operation 240 hours, former water treatment amount 1.5m
3/ h, Ni in the fresh water
2+Concentration is lower than 0.05mg/L, Ni in the dense water
2+Amount can reach 4200mg/L, current efficiency 35%～39%, and the dense water pH value 2～3 that circulates is not found precipitation behind the stripping device.The dense water of gained can directly return coating bath and use, and fresh water can be used for cleaning plating piece.
Embodiment 3
The device of embodiment 3, water purification flow path and operation steps are identical with embodiment 1, and difference from Example 1 is: embodiment 3 adopts homemade out-phase yin, yang ion-exchange membrane; Former water is for containing NO
3 -70mg/L, PO
4 3-The water of 30mg/L; Utmost point water is the NaNO of 25mg/L
3Solution; Dense water reclaims as fertilizer; The cathode and anode water that upgrades is discharged the back and is utilized again with former water is mixed.The control device flooding velocity is 200L/h, NO in the gained water outlet
3 -Concentration is lower than 0.3mg/L, PO
4 3-Concentration is lower than 0.06mg/L.
Embodiment 4
The device of embodiment 4, water purification flow path and operation steps are also identical with embodiment 1, its difference from Example 1 is: the Zeo-karb of embodiment 4 is that 116 acidulous acrylic acids are positive resin, and anionite-exchange resin is 213 strong basicity acrylic acid series negative resins; Ion-exchange membrane is homemade out-phase yin, yang ion-exchange membrane; Former water is the cyanide wastewater of Electroplate Factory's cyanide electroplating (prime coat) technology discharging, wherein Cu (CN)
3 -The about 15mg/L of content, CN
-The about 25mg/L of content, pH value about 10; Dense water reclaims and returns the aqueduct use again.The device flooding velocity is controlled to be 100L/h, CN in the water outlet
-Concentration is lower than 0.2mg/L, Cu (CN)
3 -Concentration is lower than 0.4mg/L, can be used for cleaning plating piece.
Claims (2)
1. electrodeionization water-purifying device that does not have fouling and reclaim zwitterion, it is characterized in that: it is made up of five compartments, and the order of compartment respectively is anolyte compartment (1), the first light chamber (2), dense chamber (3), the second light chamber (4), cathode compartment (5); Be provided with first cationic exchange membrane (7) between the anolyte compartment (1) and the first light chamber (2), be provided with second cationic exchange membrane (8) between the first light chamber (2) and dense chamber (3), filling male ion-exchange resin (9) in the first light chamber (2); Be provided with first anion-exchange membrane (10) between the dense chamber (3) and the second light chamber (4), be provided with second anion-exchange membrane (11) between the second light chamber (4) and the cathode compartment (5), fill anionite-exchange resin (12) in the second light chamber (4); In anolyte compartment (1), be provided with anode (6), in cathode compartment (5), be provided with negative electrode (13).
2. a kind of electrodeionization water-purifying device that does not have fouling and reclaim zwitterion according to claim 1 is characterized in that: described ion-exchange membrane is homogeneous ion-exchange membrane or heterogeneous ion-exchange membrane.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201054998U CN201021439Y (en) | 2007-01-11 | 2007-01-11 | An antiscaling electric ion removal and cleaning device and recycling negative ion and positive ion |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201054998U CN201021439Y (en) | 2007-01-11 | 2007-01-11 | An antiscaling electric ion removal and cleaning device and recycling negative ion and positive ion |
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| Publication Number | Publication Date |
|---|---|
| CN201021439Y true CN201021439Y (en) | 2008-02-13 |
Family
ID=39088853
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|---|---|---|---|
| CNU2007201054998U Expired - Fee Related CN201021439Y (en) | 2007-01-11 | 2007-01-11 | An antiscaling electric ion removal and cleaning device and recycling negative ion and positive ion |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100482594C (en) * | 2007-01-11 | 2009-04-29 | 吴祖成 | Electrodeionization water-purifying device and method for recovering cation and anion without scaling |
| CN101993387A (en) * | 2010-11-03 | 2011-03-30 | 天津大学 | Purifying method for electronic-grade N,N-dimethylformamide |
| CN102502927A (en) * | 2011-12-22 | 2012-06-20 | 浙江大学 | Device and method for desalinizing alkaline water and seawater as well as concentrating and recovering mineral salts |
| CN103103555A (en) * | 2012-12-29 | 2013-05-15 | 上海新阳半导体材料股份有限公司 | Purifying preparation method of high-purity methanesulfonic acid |
| CN106362594A (en) * | 2016-08-30 | 2017-02-01 | 中国科学院青海盐湖研究所 | Monovalent ion selectivity electrodialysis device and preparation method of lithium chloride concentrated liquor |
| CN111770785A (en) * | 2018-03-02 | 2020-10-13 | 利安德巴塞尔乙酰有限责任公司 | Method and apparatus for resin wafer enhanced electrodeionization for selective acid separation |
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2007
- 2007-01-11 CN CNU2007201054998U patent/CN201021439Y/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100482594C (en) * | 2007-01-11 | 2009-04-29 | 吴祖成 | Electrodeionization water-purifying device and method for recovering cation and anion without scaling |
| CN101993387A (en) * | 2010-11-03 | 2011-03-30 | 天津大学 | Purifying method for electronic-grade N,N-dimethylformamide |
| CN102502927A (en) * | 2011-12-22 | 2012-06-20 | 浙江大学 | Device and method for desalinizing alkaline water and seawater as well as concentrating and recovering mineral salts |
| CN102502927B (en) * | 2011-12-22 | 2013-06-12 | 浙江大学 | Device and method for desalinizing alkaline water and seawater as well as concentrating and recovering mineral salts |
| CN103103555A (en) * | 2012-12-29 | 2013-05-15 | 上海新阳半导体材料股份有限公司 | Purifying preparation method of high-purity methanesulfonic acid |
| CN103103555B (en) * | 2012-12-29 | 2015-08-19 | 上海新阳半导体材料股份有限公司 | A kind of method for preparing purified of high-purity methanesulfonic acid |
| CN106362594A (en) * | 2016-08-30 | 2017-02-01 | 中国科学院青海盐湖研究所 | Monovalent ion selectivity electrodialysis device and preparation method of lithium chloride concentrated liquor |
| CN111770785A (en) * | 2018-03-02 | 2020-10-13 | 利安德巴塞尔乙酰有限责任公司 | Method and apparatus for resin wafer enhanced electrodeionization for selective acid separation |
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