CN102992521A - Desalination system and method - Google Patents
Desalination system and method Download PDFInfo
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- CN102992521A CN102992521A CN2011102652720A CN201110265272A CN102992521A CN 102992521 A CN102992521 A CN 102992521A CN 2011102652720 A CN2011102652720 A CN 2011102652720A CN 201110265272 A CN201110265272 A CN 201110265272A CN 102992521 A CN102992521 A CN 102992521A
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- 238000010612 desalination reaction Methods 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 24
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 153
- 239000000377 silicon dioxide Substances 0.000 claims abstract description 77
- 235000012239 silicon dioxide Nutrition 0.000 claims abstract description 74
- 239000003014 ion exchange membrane Substances 0.000 claims abstract description 55
- 239000003011 anion exchange membrane Substances 0.000 claims abstract description 40
- 239000012528 membrane Substances 0.000 claims abstract description 17
- 238000000926 separation method Methods 0.000 claims abstract description 12
- 239000012530 fluid Substances 0.000 claims description 141
- 150000002500 ions Chemical class 0.000 claims description 83
- 229960001866 silicon dioxide Drugs 0.000 claims description 73
- 210000004379 membrane Anatomy 0.000 claims description 20
- 125000002091 cationic group Chemical group 0.000 claims description 19
- 150000001768 cations Chemical class 0.000 claims description 14
- 238000010979 pH adjustment Methods 0.000 claims description 10
- 238000004891 communication Methods 0.000 claims description 9
- 238000005370 electroosmosis Methods 0.000 claims description 8
- 238000005342 ion exchange Methods 0.000 claims description 8
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 7
- 239000011780 sodium chloride Substances 0.000 claims description 4
- 238000005341 cation exchange Methods 0.000 abstract description 2
- 238000011033 desalting Methods 0.000 description 47
- 230000005012 migration Effects 0.000 description 16
- 238000013508 migration Methods 0.000 description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 14
- 238000001556 precipitation Methods 0.000 description 12
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 10
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 10
- 229910001424 calcium ion Inorganic materials 0.000 description 10
- 238000010586 diagram Methods 0.000 description 10
- 230000000670 limiting effect Effects 0.000 description 10
- 229910001425 magnesium ion Inorganic materials 0.000 description 10
- 230000008569 process Effects 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 239000000463 material Substances 0.000 description 6
- 241000370738 Chlorion Species 0.000 description 5
- 239000011575 calcium Substances 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 5
- 239000011777 magnesium Substances 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- 230000000717 retained effect Effects 0.000 description 5
- 150000003839 salts Chemical class 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 239000000654 additive Substances 0.000 description 4
- 230000000996 additive effect Effects 0.000 description 4
- 150000001450 anions Chemical class 0.000 description 4
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 4
- 238000000909 electrodialysis Methods 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000004020 conductor Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- STVZJERGLQHEKB-UHFFFAOYSA-N ethylene glycol dimethacrylate Substances CC(=C)C(=O)OCCOC(=O)C(C)=C STVZJERGLQHEKB-UHFFFAOYSA-N 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 229910001415 sodium ion Inorganic materials 0.000 description 3
- 239000010936 titanium Substances 0.000 description 3
- 229910052719 titanium Inorganic materials 0.000 description 3
- XHZPRMZZQOIPDS-UHFFFAOYSA-N 2-Methyl-2-[(1-oxo-2-propenyl)amino]-1-propanesulfonic acid Chemical compound OS(=O)(=O)CC(C)(C)NC(=O)C=C XHZPRMZZQOIPDS-UHFFFAOYSA-N 0.000 description 2
- DBCAQXHNJOFNGC-UHFFFAOYSA-N 4-bromo-1,1,1-trifluorobutane Chemical compound FC(F)(F)CCCBr DBCAQXHNJOFNGC-UHFFFAOYSA-N 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 229920000049 Carbon (fiber) Polymers 0.000 description 2
- 239000004917 carbon fiber Substances 0.000 description 2
- 239000003575 carbonaceous material Substances 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 230000005684 electric field Effects 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 238000009940 knitting Methods 0.000 description 2
- 230000036961 partial effect Effects 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 238000002203 pretreatment Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000001223 reverse osmosis Methods 0.000 description 2
- 241000894007 species Species 0.000 description 2
- -1 this Chemical compound 0.000 description 2
- IRLPACMLTUPBCL-KQYNXXCUSA-N 5'-adenylyl sulfate Chemical compound C1=NC=2C(N)=NC=NC=2N1[C@@H]1O[C@H](COP(O)(=O)OS(O)(=O)=O)[C@@H](O)[C@H]1O IRLPACMLTUPBCL-KQYNXXCUSA-N 0.000 description 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 239000004966 Carbon aerogel Substances 0.000 description 1
- YZCKVEUIGOORGS-UHFFFAOYSA-N Hydrogen atom Chemical compound [H] YZCKVEUIGOORGS-UHFFFAOYSA-N 0.000 description 1
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 description 1
- DPDMMXDBJGCCQC-UHFFFAOYSA-N [Na].[Cl] Chemical compound [Na].[Cl] DPDMMXDBJGCCQC-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000000443 aerosol Substances 0.000 description 1
- 239000000908 ammonium hydroxide Substances 0.000 description 1
- 238000005349 anion exchange Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000003990 capacitor Substances 0.000 description 1
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- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000011572 manganese Substances 0.000 description 1
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000002931 mesocarbon microbead Substances 0.000 description 1
- 239000007769 metal material Substances 0.000 description 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000003020 moisturizing effect Effects 0.000 description 1
- 239000008239 natural water Substances 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 230000010287 polarization Effects 0.000 description 1
- 239000010970 precious metal Substances 0.000 description 1
- 230000002829 reductive effect Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
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- 125000006850 spacer group Chemical group 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013076 target substance Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- GPPXJZIENCGNKB-UHFFFAOYSA-N vanadium Chemical compound [V]#[V] GPPXJZIENCGNKB-UHFFFAOYSA-N 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
- 229910052726 zirconium Inorganic materials 0.000 description 1
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
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
-
- 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
-
- 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
- C02F1/4604—Treatment of water, waste water, or sewage by electrochemical methods for desalination of seawater or brackish water
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/12—Addition of chemical agents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/18—Details relating to membrane separation process operations and control pH control
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2642—Aggregation, sedimentation, flocculation, precipitation or coagulation
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
- C02F1/46109—Electrodes
- C02F2001/46133—Electrodes characterised by the material
- C02F2001/46138—Electrodes comprising a substrate and a coating
- C02F2001/46142—Catalytic coating
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
-
- 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
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/46115—Electrolytic cell with membranes or diaphragms
-
- 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
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/4612—Controlling or monitoring
- C02F2201/46145—Fluid flow
-
- 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
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- Water Supply & Treatment (AREA)
- Engineering & Computer Science (AREA)
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- Chemical Kinetics & Catalysis (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Electrochemistry (AREA)
- Health & Medical Sciences (AREA)
- Urology & Nephrology (AREA)
- Analytical Chemistry (AREA)
- Molecular Biology (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The invention relates to a desalination system and a desalination method. The desalination system comprises a silicon dioxide removing device which comprises a first electrode, a second electrode, a plurality of ion-exchange membranes which can form pairs, and a plurality of separation net devices. The plurality of ion-exchange membranes are arranged between the first electrode and the second electrode, such that a plurality alternately arranged first and second channels are formed. The plurality of separation net devices are arranged between each adjacent two ion-exchange membranes, and between the first and second electrodes and adjacent ion-exchange membranes. A first element in each pair of ion-exchange membranes is an anion-exchange membrane. A second element forming a pair with the first element in each pair of ion-exchange membranes can be one of an anion-exchange membrane, a monovalent selective cation-exchange membrane, and a bipolar ion-exchange membrane. The first elements and the second elements in the plurality of ion-exchange membranes forming pairs are alternately arranged.
Description
Technical field
The present invention relates to a kind of desalination (Desalination) system and method for water recovery (Water Recovery), relate in particular to a kind of desalination system and method for utilizing ion-exchange membrane (Ion Exchange Membranes) to come the silicon-dioxide (Silica) in the removing fluids to reclaim to carry out water.
Background technology
In industrial circle, a large amount of waste water is produced such as the aqueous solution of saliferous.Usually, such waste water and be not suitable for directly in family or industry, using.In view of the finiteness of spendable water resources, from fluid, just seem particularly important as reclaiming qualified spendable water in waste water, brackish water, seawater or other saline solns.
Silicon-dioxide is a kind of common material that contains in the natural water.Because under usual conditions, its solubleness in water is lower, thereby many industrial process waters, all must ask the upper existence of the dioxide-containing silica that contains in the water such as boiler feed water, circulating cooling tower moisturizing etc., to avoid that the water device is caused the disadvantageous effects such as fouling.Therefore, need in many cases the silicon-dioxide in the water is carried out removing to a certain degree, to satisfy specific purposes requirement.
There has been multiple trial to come from the waste water that contains silicon-dioxide or other water sources, to remove silicon-dioxide.Such as, the fluid that contains silicon-dioxide is transfused to into desalting plant, carries out removing of silicon-dioxide such as reverse osmosis (Reverse Osmosis) film device that operates under higher pH value condition.Therebetween, because fluid has the silicon-dioxide ionization that higher pH value can promote that it contains, therefore, the pH value of this fluid is enhanced to impel removing of silicon-dioxide.Yet in existing the application, the mode that removes of this kind silicon-dioxide needs complicated and strict preprocessor and efficient lower, causes cost to increase, thereby loses in some cases economy.In addition, sometimes also can be owing to the unpredictalbe fluctuation of pretreatment system causes the indissoluble or the part soluble salt that contain in the fluid, such as fouling or the deposition in desalting plant such as calcium sulfate or calcium carbonate.This for silicon-dioxide remove and desalting plant itself all be disadvantageous.
So, a kind of new desalination system and method that silicon-dioxide removes of carrying out need to be provided.
Summary of the invention
One embodiment of the present of invention provide a kind of desalination system.This desalination system comprises can receive the silicon-dioxide apparatus for removing that the first input fluid removes silicon-dioxide in this fluid.This silicon-dioxide apparatus for removing comprises ion-exchange membrane and a plurality of separation screen device that the first and second electrodes, plural pieces can be paired.Plural pieces can paired ion-exchange membrane be arranged between described the first and second electrodes and forms a plurality of the first and second passages that are arranged alternately.A plurality of separation screen devices be arranged between the adjacent every a pair of ion-exchange membrane and the first and second electrodes and adjacent ion-exchange membrane between.Wherein, the first element in every a pair of ion-exchange membrane is anion-exchange membrane, one of can be in anion-exchange membrane, unit price selectivity cationic exchange membrane and the ambipolar ion-exchange membrane with paired the second element of its first element in every a pair of ion-exchange membrane, wherein the first element and the second element described plural pieces can be paired ion-exchange membrane in be arranged alternately.
Another embodiment of the present invention provides a kind of desalination system.This desalination system comprises the silicon-dioxide apparatus for removing.This silicon-dioxide apparatus for removing comprises anion-exchange membrane and a plurality of separation screen device that the first and second electrodes, plural pieces can be paired.Plural pieces can paired anion-exchange membrane be arranged between described the first and second electrodes and forms a plurality of the first and second passages that are arranged alternately.A plurality of separation screen devices be arranged between the adjacent every a pair of anion-exchange membrane and the first and second electrodes and adjacent anion-exchange membrane between.
Embodiments of the invention further provide a kind of method for remove silicon-dioxide from fluid.The method comprises that input the first input fluid is to removing by carrying out silicon-dioxide in the film formed first channel of ion-exchange paired in the silicon-dioxide apparatus for removing; Input the second input fluid to taking described silicon-dioxide apparatus for removing out of by the silicon-dioxide that removes from described the first input fluid with handle in the film formed second passage of ion-exchange paired described in the described silicon-dioxide apparatus for removing.Wherein, the first element in every a pair of ion-exchange membrane is anion-exchange membrane, one of can be in anion-exchange membrane, unit price selectivity cationic exchange membrane and the ambipolar ion-exchange membrane with paired the second element of its first element in every a pair of ion-exchange membrane, wherein the first element and the second element described plural pieces can be paired ion-exchange membrane in be arranged alternately.
Description of drawings
Be described for embodiments of the invention in conjunction with the drawings, the present invention may be better understood, in the accompanying drawings:
Fig. 1 is the synoptic diagram of an embodiment of desalination system of the present invention;
Fig. 2 is the synoptic diagram of a plurality of embodiment of desalting plant of the present invention to Fig. 4;
Fig. 5 is the synoptic diagram of another embodiment of desalination system of the present invention; And
Fig. 6 is the experimental diagrams of an embodiment of the silicon-dioxide removal rate of desalting plant of the present invention.
Embodiment
Figure 1 shows that the synoptic diagram of an embodiment of desalination system 10 of the present invention.In the present embodiment, desalination system 10 comprises desalting plant 11.This desalting plant 11 can be used to receive come from first-class body source (not shown) and contain many kinds of substance and the first input fluid 12 of other impurity so that it is carried out desalting treatment.In addition, in first fluid 12 is processed or after processing, this desalting plant 11 can receive the second input fluid 13 that comes from second body source (not shown), thereby a charge species that removes is removed out desalting plant 11 from the first input fluid 12.
Like this, because the desalting of desalting plant 11 is compared with the first input fluid 12, the first output fluid (product fluid) 14 that comes from this desalting plant 11 just contains the charged ion of low concentration.Compare with the second input fluid 13, the second output fluid (concentrated fluid) 15 that comes from this desalting plant 11 just contains the charged ion of higher concentration.In non-limiting example, the material and other impurity that comprise in the first input fluid 12 can comprise charged ion, such as magnesium ion (Mg
2+), calcium ion (Ca
2+), silicon-dioxide (Silica), sodium ion (Na
+), chlorion (Cl
-) and other ions.In a non-limiting example, the charged ion in the first input fluid 12 can comprise a part of target substance at least, and such as Ionized silicon-dioxide, like this, desalting plant 11 just can be used as the silicon-dioxide apparatus for removing and uses.In some instances, the first output fluid 14 also can be inputted in the desalting plant 11 or other desalting plants again, as carrying out further desalting treatment in pole-reversing electroosmosis (Electrodialysis Reversal) device.
Silicon-dioxide Chang Yinan ionization or partially ionized form are present in the first input fluid 12.Usually, the pH value that increases by the first input fluid 12 can improve the ionization of silicon-dioxide in this first input fluid 12 so that under electric field action silicon-dioxide is removed.Like this, as shown in Figure 1, thereby further comprising the pH adjustment unit 16 with desalting plant 11 fluid communication, desalination system 10 comes the pH value of the first input fluid 12 is regulated the degree of ionization that improves silicon-dioxide in this first fluid 12.
In some instances, the pH value that pH adjustment unit 16 can be used to adjust the first input fluid 12 is greater than 7, such as in from 8 to 11 scope.In other examples, the pH value of the first input fluid 12 can be adjusted in 9.5 to 11 the scope of being in.After to the silicon-dioxide ionization, at least a portion of the silicon-dioxide in the first input fluid 12 can HSiO
3 -And/or SiO
3 2-Or other ionic speciess exist.For convenience of explanation, in embodiments of the present invention, with HSiO
3 -For example describes.
In some instances, pH adjustment unit 16 can comprise that pH adjusts the source, its can input additive in the first input fluid 12 to adjust its pH value.In non-limiting example, pH adjustment unit 16 can be inputted alkaline additive in the first input fluid 12.Alkaline additive can include but not limited to sodium hydroxide, potassium hydroxide and ammonium hydroxide.In some applications, but being transfused in the first input fluid 12 of this alkaline additive automatic or manual.In certain application, pH adjustment unit 16 can not arrange yet, and the pH value of the first input fluid 12 can be adjusted in advance.
Figure 2 shows that the synoptic diagram of an embodiment of desalting plant 11 of the present invention.As shown in Figure 2, desalting plant 11 comprises ion- exchange membrane 19,20,21,22 and a plurality of separation screen device (Spacer) 23 that the first electrode 17, the second electrode 18, plural pieces can be paired.In the present embodiment, the first and second electrodes 17,18 respectively with power supply (not shown) thus positive and negative electrode link to each other can be respectively as positive pole and negative pole.In other embodiments, the polarity of the first and second electrodes 17,18 also can change.
In certain embodiments, the first and second electrodes 17,18 can be by the metallic substance of sheet, netted or other shape, such as titanium or be coated with the compositions such as titanium of the precious metals such as platinum.In further embodiments, the first and second electrodes 17, but 18 can comprise other heat conduction or athermanous electro-conductive material, and it can comprise the particle with reduced size and larger surface-area.In some instances, electro-conductive material can comprise one or more carbon materials.In non-limiting example, carbon material can comprise activated carbon particle (Activated Carbon Particles), porous carbon particle (Porous Carbon Particles), carbon fiber (Carbon Fibers), carbon aerosol (Carbon Aerogels), porous carbonaceous mesophase spherules (Porous Mesocarbon Microbeads) or its combination.At other example, electro-conductive material can comprise conducing composite material, such as manganese, and iron, the oxide compound of manganese and iron, the carbide of titanium, zirconium, vanadium, tungsten or its combination.
In the present embodiment, the first and second electrodes 17,18 can have tabular structure, thereby can be set parallel to each other to form the structure of stacking (Stack).In other examples, the first and second electrodes 17,18 also can have different shapes, such as sheet, bulk (Block) or column (Cylinder), and arrange according to different frameworks.For example, the first and second electrodes 17,18 can arrange with one heart, thereby have defined betwixt a space that spirrillum is continuous.
Paired ion-exchange membrane 19-22 can be used to that ion is carried out selectivity to be passed through, and it is arranged on the first and second electrodes 17, thereby 18 form a plurality of first channels that are arranged alternately 24 and second passage 25.In some instances, when operation, first channel 24 and second passage 25 can use as light chamber and dense chamber respectively.In the present embodiment, four ion-exchange membrane 19-22 have formed a first channel 24 and two second passages 25 that are arranged alternately.In other examples, at least three ion-exchange membranees can be arranged on 17,18 at the first and second electrodes and form one or more first channels and one or more second passage.
In the embodiment shown in Figure 2, the first element 20,22 of every a pair of ion-exchange membrane and corresponding the second element 19,21 are anion-exchange membrane.In some instances, each anion-exchange membrane can comprise unit price chosen anion exchange membrane or conventional anion-exchange membrane.Unit price chosen anion exchange membrane can only be used for monovalent anion to be passed through.Conventional anion-exchange membrane not only can but also can pass through monovalent anion by multivalent anions.
Like this, in when operation, when desalting plant 11 during at the normal polarity state, electric current applies thereon, and fluid is advanced in first channel 24 and the second passage 25 by input respectively such as the first and second input fluids 12,13.In certain application, the first and second input fluids 12,13 can be simultaneously or asynchronous input advance in the desalting plant 11.
Because the ion-exchange membrane 19-22 that arranges in the desalting plant 11 is anion-exchange membrane, in first channel (light chamber) 24, the Ionized silicon-dioxide of at least a portion in the first input fluid 12 is such as HSiO
3 -With other ions, such as OH
-And Cl
-Thereby move towards anode 17 by anion-exchange membrane 20 and to enter in the second passage (dense chamber) 25.Positively charged ion in the first input fluid 12 is such as Ca
2+And Mg
2+(not shown) then can not still be in the light chamber 24 by anion-exchange membrane 20.
In dense chamber 25, even electric field can apply certain tractive force to positively charged ion, the positively charged ion in the second input fluid 13 is such as Na
+Can not move by anion-exchange membrane 19, thereby be retained in the corresponding dense chamber 25.In desalting plant 11, light chamber 24 and dense chamber 25 are arranged alternately, and like this, the negatively charged ion in the second input fluid 13 in dense chamber 25 is such as hydroxide ion (OH
-) and chlorion (Cl
-), move by corresponding anion- exchange membrane 19,21, such as entering in the light chamber 24 of closing on corresponding dense chamber 25.
In non-limiting example, the second input fluid 13 can comprise soluble salt, and it contains activity or the higher negatively charged ion of degree of ionization with higher concentration, such as chlorion (Cl
-), like this, this fluid also can be described as the fluid that is rich in chlorion.In some instances, the active ion in the second input fluid 13 also can comprise sulfate ion (SO
4 2-) and hydroxide ion (OH
-).Thereby, work as object ion, such as silicon-dioxide ion (HSiO
3 -) enter corresponding dense chamber 25 from light chamber 24 after, in operating process, when the negatively charged ion in entering dense chamber 25 continues from dense chamber 25 to 24 migration of corresponding light chamber, compared to the object ion that moves in the dense chamber 25, when continuing migration, high density active anion in the second input fluid 13 can occupy at least most ion(ic)current, thus the migration of establishment object ion from dense chamber 25 to corresponding light chamber 24.
Such as, soluble salt comprises sodium-chlor (NaCl).In continuing transition process, at least one most of ion(ic)current can be occupied such as hydroxide ion by chlorion or other active ions, thereby causes at least one most of ionization silicon-dioxide can not carry ion(ic)current.In non-limiting example, in corresponding dense chamber 25, the concentration of active ion can be higher than even the concentration of the object ion that comes far above 24 migrations from light chamber.In other examples, when from dense chamber 25 to 24 migration of corresponding light chamber, in corresponding dense chamber 25, the large mobility of ions from the next object ion of light chamber 24 migrations in the inner of the mobility of ions of active ion (Ionic Mobility).In certain application, when from dense chamber 25 to 24 migration of corresponding light chamber, the quantity of the active ion in the second input fluid 13 can be greater than the object ion that advances from 24 migrations of light chamber the dense chamber 25, such as HSiO
3 -Quantity.
Like this, when operation, a part of active ion in the second input fluid 13 in the dense chamber 25 can move out and enter the light chamber 24 of closing on from corresponding anion-exchange membrane, in this process, because the active ion in the second input fluid 13 has occupied most of ion(ic)current, most of object ion is such as HSiO
3 -Can not be by corresponding anion- exchange membrane 19,21 and enter light chamber, thus it is stayed the dense chamber 25 entering the 25 follow-up continuations of insurance of dense chamber from corresponding light chamber 24.
In some instances, when negatively charged ion moves from dense chamber 25 to light chamber 24, in order to increase the accounting of the ion(ic)current that active ion carries in the second input fluid 13, as shown in Figure 1, desalination system 10 further comprises the ion adjustment unit 26 with the second input fluid 13 fluid communication.This ion adjustment unit 26 can impel in operation, and when negatively charged ion continued from dense chamber 25 to 24 migration of corresponding light chamber, the active ion in the second input fluid in the dense chamber 25 can occupy most of ion(ic)current.In non-limiting example, ion adjustment unit 26 increases the concentration of the second input fluid 13 active ions by the method for injecting sodium chloride solution in the second input fluid 13.In certain application, ion adjustment unit 26 can arrange or not arrange.
Like this, as shown in Figure 2, when the second input fluid 13 passed through dense chamber 25, the object ion that it comes from 24 migrations of light chamber was such as HSiO
3 -Take desalting plant 11 out of, thereby have respectively the object ion that comprises ionization silicon-dioxide low and higher concentration compared to the first and second input fluids the 12,13, first output fluid 14 and the second output fluid 15.
Usually, the pH value that improves the first input fluid 12 can cause the interior positively charged ion of fluid, such as calcium ion (Ca
2+) and magnesium ion (Mg
2+) in desalting plant, occur to precipitate or fouling.Yet, in the embodiment shown in fig. 1, because desalting plant 11 only arranges anion-exchange membrane, when the ionization silicon-dioxide in the first input fluid 12 is removed, positively charged ion in it, still be in the light chamber 24 such as calcium ion and magnesium ion, do not concentrate thereby can not enter in the dense chamber 25.Like this, just greatly reduce positively charged ion in the trend of the 25 interior generation foulings of dense chamber or precipitation.
In some instances, the polarity of the first and second electrodes 17,18 of desalting plant 11 can be reversed, and under opposite electrode state, the light chamber under the normal electrode state receives the second input fluid 13 as dense chamber originally; Originally the dense chamber under the normal electrode state receives the first input fluid 12 as light chamber and comes it is processed, such as removing the silicon-dioxide in it and avoiding or alleviate zwitterion in the possibility of desalting plant 11 interior generations precipitations.
Figure 3 shows that the synoptic diagram of another embodiment of desalting plant 30.Embodiment shown in Figure 3 is similar to embodiment shown in Figure 2, the two difference is in the embodiment shown in fig. 3, the ion-exchange membrane 20 of silicon-dioxide apparatus for removing 30,22, in 31 each the second element 31 is unit price selectivity cationic exchange membrane, thereby a plurality of unit price selectivity cationic exchange membranes (the second element) that are arranged alternately 31 and corresponding anion-exchange membrane (the first element) 20,22 have formed a plurality of the first and second passages 24,25 that are arranged alternately.When operation, the first and second passages 24,25 can be used as light chamber and use dense chamber.
Unit price selectivity cationic exchange membrane 31 only can pass through univalent cation, and polyvalent cation and negatively charged ion all can not pass through.In a non-limiting example, be used for using the material at unit price selectivity cationic exchange membrane 31 can comprise crosslinked multipolymer, it can be from acrylamido methyl propane sulfonic acid (Acrylamidomethylpropane sulfonic acid, AMPS) and Ethylene glycol dimethacrylate (Ethylene glycol dimethacrylate, EGDMA).
Like this, similar to embodiment shown in Figure 2, in when operation, when desalting plant 30 during in normal polarization state, electric current applies thereon, and the first and second input fluids 12,13 enter respectively first channel 24 and second passage 25.Because the effect that removes of desalting plant 30, in the first input fluid 12, the Ionized silicon-dioxide of at least a portion is such as HSiO
3 -Or other negatively charged ion, such as OH
-And Cl
-Can enter in the corresponding second passage 25 towards anode 17 migrations by anion-exchange membrane 20.
Polyvalent cation in the first input fluid 12 includes but not limited to calcium ion (Ca
2+) and magnesium ion (Mg
2+) owing to can not be retained in the light chamber 24 by unit price selectivity cationic exchange membrane 31.In some applications, the univalent cation in the first input fluid 12 is such as sodium ion (Na
+) can enter in the adjacent dense chamber 25 towards negative electrode 18 migrations by unit price selectivity cationic exchange membrane 31.
In dense chamber 25, because the existence of unit price selectivity cationic exchange membrane 31, the negatively charged ion in it comprises the HSiO that comes from 24 migrations of light chamber
3 --Just can't be further by unit price selectivity cationic exchange membrane 31 entering in the light chamber 24 of closing on, thereby still be retained in the corresponding dense chamber 25.Because the existence of anion- exchange membrane 20,22, the positively charged ion in the dense chamber 25 is such as sodium ion (Na
+) still be in too in the dense chamber 25.
Like this, when the second input fluid 13 during by dense chamber 25, advance univalent cation and negatively charged ion in the dense chamber 25 from 24 migrations of light chamber, comprise object ion such as HSiO
3 -Just concentrated in dense chamber 25 and quilt is taken out of desalting plant 30, thereby exports the charged ion that fluid 15 has respectively low and higher concentration compared to the first and second input fluids the 12,13, first output fluid 14 and second, comprises ionization silicon-dioxide.
Thereby because desalting plant 30 is provided with unit price selectivity cationic exchange membrane 31, at least a portion ionization silicon-dioxide can be removed from the first input fluid 12.Therebetween, partial cation in the first input fluid 12 is such as calcium ion (Ca
2+) and magnesium ion (Mg
2+) then still be in the light chamber 24 and can not enter and concentrate in the dense chamber 25, thereby greatly alleviate it in the risk of dense chamber 25 interior generation precipitations or fouling.
Figure 4 shows that the synoptic diagram of an embodiment of desalting plant 32.As shown in Figure 4, this embodiment is similar to the embodiment shown in Fig. 3, the two difference is in the embodiment shown in fig. 4, each second element of the ion-exchange membrane of desalting plant 32 is ambipolar ion-exchange membrane (Bipolar Ion Exchange Membrane), rather than the unit price selectivity cationic exchange membrane 31 shown in Fig. 3.Like this, a plurality of ambipolar ion-exchange membrane that is arranged alternately (the second element) 33 and anion-exchange membrane (the first element) 20,22 are arranged on 17,18 at the first and second electrodes to form a plurality of the first and second passages 24,25 that are arranged alternately.
In non-limiting example, ambipolar ion-exchange membrane generally include cationic exchange layer, anionresin layer and be arranged on cationic exchange membrane and anion-exchange membrane between knitting layer (Junction Layer).In the ambipolar ion-exchange membrane operating process, thereby diffusing into knitting layer by the cation and anion exchange layer, water resolves into hydrogen ion (H+) and hydroxide ion (OH-).Hydrogen ion passes through the cationic exchange layer towards movable cathode; Hydroxide ion moves towards anode by the anionresin layer.Other negatively charged ion and positively charged ion are then got rid of outside ambipolar ion-exchange membrane by positively charged ion and anionresin layer respectively.
Like this, similar to embodiment shown in Figure 3, in operation, in light chamber 24, the negatively charged ion in the first input fluid 12 is such as HSiO
3 -Can enter in the adjacent dense chamber 25, the positively charged ion in it then can not still be retained in the corresponding light chamber 24 by ambipolar ion-exchange membrane 33 such as calcium ion and magnesium ion.In dense chamber 25, because the excretion of ambipolar ion-exchange membrane 33, from the next negatively charged ion of light chamber 24 migrations, such as HSiO
3 -Still be retained in the dense chamber 25 and can not further move in adjacent light chamber 24.
Thereby, when the second input fluid 13 passes through dense chamber 25, from the next negatively charged ion of light chamber 24 migrations, such as HSiO
3 -Then taken out of and avoided simultaneously positively charged ion in the desalting plant 32, the concentrating in corresponding dense chamber such as calcium ion and magnesium ion greatly reduces the risk that precipitation or fouling occur.
In certain application, for fear of or the setting that alleviates owing to pH adjustment unit 16 cause positively charged ion, the possibility of precipitation or fouling occurs in desalting plant 11,30 or 32 such as calcium ion and magnesium ion, desalination system 10 can be provided with pretreatment unit.This pretreatment unit can be used to be transfused to before the silicon-dioxide apparatus for removing at the first input fluid 12 processes fluid to remove at least the part polyvalent cation, thereby produce the first input fluid 12 with suitable total dissolved solidss (Total Dissolved Solids, TDS) level and cation concn.
Figure 5 shows that the synoptic diagram of another embodiment of desalination system 10 of the present invention.As shown in Figure 5, this embodiment is similar to embodiment shown in Figure 1, the two difference is in the embodiment shown in fig. 5, pretreatment unit 34 is arranged on the upstream of desalting plant 11 and comes pre-treatment input fluid 35 to remove the ion that at least a portion degree of ionization is higher in it with its fluid communication, such as calcium ion and magnesium ion, thereby produce the first input fluid 12 with suitable total dissolved solidss (Total Dissolved Solids, TDS) level and cation concn.
In the present embodiment, pretreatment unit 34 comprises pole-reversing electroosmosis (Electrodialysis Reverse, EDR) device.In other embodiments, pretreatment unit 34 can comprise electrodialysis (Electrodialysis, ED) device, super capacitor desalination (Supercapacitor Desalination, SCD) device or softening (Softening) device of cationic exchange come convection cell 35 to carry out pre-treatment.
Like this, when operation, fluid 35 is transfused in pole-reversing electroosmosis device 34 processes to remove at least a portion negatively charged ion and the positively charged ion that it contains, such as calcium ion and magnesium ion, can be used to input the first input fluid 12 with proper solubility total solids (Total Dissolved Solids, TDS) level and cation concn of processing in the desalting plant 11 thereby produce.Therebetween, fluid 36 also is transfused in pole-reversing electroosmosis device 34 to be taken out of in this pole-reversing electroosmosis device 34 with an ion that removes from fluid 35, thereby produces output fluid 37.Compared to fluid 36, this output fluid 37 includes the charged ion of higher concentration.
In certain application, as shown in Figure 5, desalination system 10 can further comprise the precipitation unit 38 with pole-reversing electroosmosis device 34 fluid communication.In some instances, precipitation unit 38 can be used to provide fluid 36 so that its circulation enters in the pole-reversing electroosmosis device 34.Along with the continuous circulation of fluid 36, the salt in it or the concentration of other impurity may constantly increase, and the salt that partial solubility is lower is such as calcium sulfate etc. even reach capacity or over-saturation in fluid 36.Like this, saturated or over-saturation reaches certain degree when this, just generation in precipitation unit 38 of precipitation.In some instances, along with the carrying out of operation, the solid (not shown) that precipitation produces and a part of fluid 36 can be discharged by pipeline 39 autoprecipitation unit 38.Fluid 40 also can input fluid replacement 36.In non-limiting example, fluid 40 can be from identical fluid source with fluid 35.
Figure 6 shows that the experimental diagrams of an embodiment of the silicon-dioxide removal rate of desalting plant 11 of the present invention.For convenience of explanation, take the desalting plant 11 shown in Fig. 2 as example.The water inlet total dissolved solidss are about 350ppm in the experiment, wherein contain the about 40ppm of silicon-dioxide, and its pH value is adjusted to about 11 before entering the silicon-dioxide apparatus for removing.As shown in Figure 6, in the continuous service process of 5 day time, the removal rate of the silicon-dioxide of desalting plant 11 is about 50%, and more stable, this has shown that the precipitation of desalting plant 11 interior generations or scale formation were also avoided or alleviated when silicon-dioxide in the first input fluid 12 can be effectively removed.
Fig. 1 only is schematically to embodiment shown in Figure 5, and Fig. 1 identical label in Fig. 5 can represent similar element.In embodiments of the present invention, Fig. 1 can be used to silicon-dioxide in the removing fluids to embodiment shown in Figure 5.In other examples, it also can be used to remove other suitable ion, such as remove dianion from fluid.The first element of each centering in desalting plant 11,30 or the 32 intermediate ion exchange membranes is anion-exchange membrane; The second element of each centering in the ion-exchange membrane is anion-exchange membrane, unit price selectivity cationic exchange membrane or ambipolar ion-exchange membrane.Wherein the silicon-dioxide of the first input fluid intermediate ion is transferred to by the first element and is realized in the second input fluid removing, and the common trait of the second element is to stop the polyvalent cation in the first input fluid to be transferred to simultaneously in the second input fluid to reduce owing to polyvalent cation concentrated fouling risk that causes in the second input fluid.Like this, the ion in the first input fluid 12 just can be by effective and stable removing such as silicon-dioxide.In addition, pretreatment unit also can be provided to avoid desalting plant that precipitation or fouling occur in the process that the first input fluid 12 is processed within it.
Although describe the present invention in conjunction with the specific embodiments, those skilled in the art will appreciate that and to make many modifications and modification to the present invention.Therefore, recognize that the intention of claims is to cover all such modifications and the modification in true spirit of the present invention and the scope.
Claims (18)
1. desalination system comprises:
Can receive the silicon-dioxide apparatus for removing that the first input fluid removes silicon-dioxide in this fluid, comprise:
The first and second electrodes;
Plural pieces can be paired ion-exchange membrane, it is arranged between described the first and second electrodes and forms a plurality of the first and second passages that are arranged alternately;
A plurality of separation screen devices, it is arranged between adjacent per two ion-exchange membranees and the first and second electrodes and separately between the adjacent ion-exchange membrane; And
Wherein, the first element in every a pair of ion-exchange membrane is anion-exchange membrane, one of can be in anion-exchange membrane, unit price selectivity cationic exchange membrane and the ambipolar ion-exchange membrane with paired the second element of its first element in every a pair of ion-exchange membrane, wherein the first element and the second element described plural pieces can be paired ion-exchange membrane in be arranged alternately.
2. desalination system as claimed in claim 1, wherein said silicon-dioxide apparatus for removing can further receive the second input fluid to take the ion that removes from described the first input fluid out of.
3. desalination system as claimed in claim 2, the every a slice in the ion-exchange membrane that wherein said plural pieces can be paired is anion-exchange membrane.
4. desalination system as claimed in claim 2, it further includes the ion adjustment unit with described silicon-dioxide apparatus for removing fluid communication, and this ion adjustment unit can be used to adjust the concentration of negatively charged ion in described the second input fluid.
5. desalination system as claimed in claim 4, it further includes the pretreatment unit with described silicon-dioxide apparatus for removing fluid communication, and this pretreatment unit can be used to polyvalent cation at least part of removing fluids to produce described the first input fluid.
6. desalination system as claimed in claim 5, wherein said pretreatment unit comprises the pole-reversing electroosmosis device.
7. desalination system as claimed in claim 1, it further includes the pH adjustment unit with described silicon-dioxide apparatus for removing fluid communication, and this pH adjustment unit can be used to adjust the pH value of described the first input fluid.
8. desalination system comprises:
The silicon-dioxide apparatus for removing comprises:
The first and second electrodes;
Plural pieces can be paired anion-exchange membrane, it is arranged between described the first and second electrodes and forms a plurality of the first and second passages that are arranged alternately; And
A plurality of separation screen devices, it is arranged between adjacent per two anion-exchange membranes and the first and second electrodes and separately between the adjacent anion-exchange membrane.
9. desalination system as claimed in claim 8, wherein said silicon-dioxide apparatus for removing receives respectively the first input fluid to remove the silicon-dioxide in this fluid and to receive the second input fluid to take the silicon-dioxide that removes out of from described the first input fluid by described the first and second passages.
10. desalination system as claimed in claim 9, it further includes the pH adjustment unit with described silicon-dioxide apparatus for removing fluid communication, and this pH adjustment unit can be used to adjust the pH value of described the first input fluid.
11. desalination system as claimed in claim 8, it further includes the ion adjustment unit with described silicon-dioxide apparatus for removing fluid communication, and this ion adjustment unit can be used to adjust the concentration of negatively charged ion in described the second input fluid.
12. a method that is used for removing from fluid silicon-dioxide comprises:
Input the first input fluid to removing by carrying out silicon-dioxide in the film formed first channel of ion-exchange paired in the silicon-dioxide apparatus for removing;
Input the second input fluid to taking described silicon-dioxide apparatus for removing out of by the silicon-dioxide that removes from described the first input fluid with handle in the film formed second passage of ion-exchange paired described in the described silicon-dioxide apparatus for removing; And
Wherein, the first element in every a pair of ion-exchange membrane is anion-exchange membrane, one of can be in anion-exchange membrane, unit price selectivity cationic exchange membrane and the ambipolar ion-exchange membrane with paired the second element of its first element in every a pair of ion-exchange membrane, wherein the first element and the second element described plural pieces can be paired ion-exchange membrane in be arranged alternately.
13. method as claimed in claim 12, wherein said silicon-dioxide apparatus for removing comprises:
The first and second electrodes;
The described paired ion-exchange membrane of plural pieces, it is arranged between described the first and second electrodes and forms a plurality of described the first and second passages that are arranged alternately; And
A plurality of separation screen devices, it is arranged between described adjacent per two ion-exchange membranees and the first and second electrodes and separately between the adjacent ion-exchange membrane.
14. the every a slice in the ion-exchange membrane that method as claimed in claim 12, wherein said plural pieces can be paired is anion-exchange membrane.
15. method as claimed in claim 14, it further is included in described the second input fluid and enters the front concentration that increases the negatively charged ion in described the second input fluid of described silicon-dioxide apparatus for removing.
16. the concentration of the negatively charged ion in the method as claimed in claim 15, described the second input fluid of wherein said increase realizes by the mode of the solution of interpolation sodium chloride-containing.
17. method as claimed in claim 12, it further is included in described the first input fluid and enters the front pH value of adjusting described the first input fluid of described silicon-dioxide apparatus for removing.
18. method as claimed in claim 17, wherein said the first input fluid pH value are adjusted in 9.5 to 11 the scope of being in.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011102652720A CN102992521A (en) | 2011-09-08 | 2011-09-08 | Desalination system and method |
| PCT/US2012/050512 WO2013036354A1 (en) | 2011-09-08 | 2012-08-13 | Desalination system and method |
| TW101131932A TW201315533A (en) | 2011-09-08 | 2012-08-31 | Desalination system and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011102652720A CN102992521A (en) | 2011-09-08 | 2011-09-08 | Desalination system and method |
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|---|---|
| CN102992521A true CN102992521A (en) | 2013-03-27 |
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|---|---|
| CN (1) | CN102992521A (en) |
| TW (1) | TW201315533A (en) |
| WO (1) | WO2013036354A1 (en) |
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| CN107381729A (en) * | 2017-08-29 | 2017-11-24 | 大唐（北京）水务工程技术有限公司 | A kind of processing method of electrodialysis reactor and desulfurization wastewater |
| CN112833018A (en) * | 2021-02-23 | 2021-05-25 | 广东理文造纸有限公司 | A system and method for cleaning vacuum pump deposits for papermaking |
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| SG11201510440XA (en) * | 2013-06-19 | 2016-01-28 | Massachusetts Inst Technology | Water desalination/purification and bio-agent preconcentration |
| WO2020264012A1 (en) * | 2019-06-25 | 2020-12-30 | Magna Imperio Systems Corp. | Electrodialysis process and bipolar membrane electrodialysis devices for silica removal |
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| WO2008153274A1 (en) * | 2007-06-11 | 2008-12-18 | Yoo, Yung-Geun | Preparation method of mineral water and mineral salt from deep ocean water |
| WO2011009950A1 (en) * | 2009-07-23 | 2011-01-27 | Societe Anonyme Des Eaux Minerales D'evian, "S.A.E.M.E" | A process for producing water enriched with natural orthosilicic acid |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107381729A (en) * | 2017-08-29 | 2017-11-24 | 大唐（北京）水务工程技术有限公司 | A kind of processing method of electrodialysis reactor and desulfurization wastewater |
| CN112833018A (en) * | 2021-02-23 | 2021-05-25 | 广东理文造纸有限公司 | A system and method for cleaning vacuum pump deposits for papermaking |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2013036354A1 (en) | 2013-03-14 |
| TW201315533A (en) | 2013-04-16 |
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