CN204111387U - A kind of employing anion-exchange membrane solid state electrolyte electrolytic cell assembly - Google Patents
A kind of employing anion-exchange membrane solid state electrolyte electrolytic cell assembly Download PDFInfo
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- CN204111387U CN204111387U CN201420519820.7U CN201420519820U CN204111387U CN 204111387 U CN204111387 U CN 204111387U CN 201420519820 U CN201420519820 U CN 201420519820U CN 204111387 U CN204111387 U CN 204111387U
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- exchange membrane
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- end plate
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- 239000003011 anion exchange membrane Substances 0.000 title claims abstract description 30
- 239000003792 electrolyte Substances 0.000 title claims abstract description 18
- 239000007787 solid Substances 0.000 title claims abstract description 17
- 239000000463 material Substances 0.000 claims abstract description 60
- 239000003014 ion exchange membrane Substances 0.000 claims abstract description 52
- 239000003054 catalyst Substances 0.000 claims abstract description 21
- 230000003197 catalytic effect Effects 0.000 claims abstract description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 44
- 238000007789 sealing Methods 0.000 claims description 24
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 22
- 239000010936 titanium Substances 0.000 claims description 20
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 18
- 229910052719 titanium Inorganic materials 0.000 claims description 18
- 239000001257 hydrogen Substances 0.000 claims description 15
- 229910052739 hydrogen Inorganic materials 0.000 claims description 15
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 14
- 238000005260 corrosion Methods 0.000 claims description 13
- 230000007797 corrosion Effects 0.000 claims description 13
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 12
- 239000000741 silica gel Substances 0.000 claims description 12
- 229910002027 silica gel Inorganic materials 0.000 claims description 12
- 229910006404 SnO 2 Inorganic materials 0.000 claims description 8
- 229910052759 nickel Inorganic materials 0.000 claims description 8
- 239000010955 niobium Substances 0.000 claims description 8
- 239000006260 foam Substances 0.000 claims description 7
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 4
- 229910003296 Ni-Mo Inorganic materials 0.000 claims description 4
- NPXOKRUENSOPAO-UHFFFAOYSA-N Raney nickel Chemical compound [Al].[Ni] NPXOKRUENSOPAO-UHFFFAOYSA-N 0.000 claims description 4
- 229910010413 TiO 2 Inorganic materials 0.000 claims description 4
- 239000004744 fabric Substances 0.000 claims description 4
- 229910052750 molybdenum Inorganic materials 0.000 claims description 4
- 239000011733 molybdenum Substances 0.000 claims description 4
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 claims description 4
- 229910052758 niobium Inorganic materials 0.000 claims description 4
- GUCVJGMIXFAOAE-UHFFFAOYSA-N niobium atom Chemical compound [Nb] GUCVJGMIXFAOAE-UHFFFAOYSA-N 0.000 claims description 4
- 238000007747 plating Methods 0.000 claims description 4
- 229910001404 rare earth metal oxide Inorganic materials 0.000 claims description 4
- 229910001220 stainless steel Inorganic materials 0.000 claims description 4
- 239000010935 stainless steel Substances 0.000 claims description 4
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 claims description 4
- 229910052721 tungsten Inorganic materials 0.000 claims description 4
- 239000010937 tungsten Substances 0.000 claims description 4
- 239000002699 waste material Substances 0.000 abstract description 7
- 230000015572 biosynthetic process Effects 0.000 abstract description 3
- 239000012528 membrane Substances 0.000 description 9
- 125000002091 cationic group Chemical group 0.000 description 8
- 230000003647 oxidation Effects 0.000 description 8
- 238000007254 oxidation reaction Methods 0.000 description 8
- 239000002351 wastewater Substances 0.000 description 7
- 238000006056 electrooxidation reaction Methods 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 239000002585 base Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 239000003513 alkali Substances 0.000 description 3
- 230000015556 catabolic process Effects 0.000 description 3
- 238000006731 degradation reaction Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000010815 organic waste Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- XYFCBTPGUUZFHI-UHFFFAOYSA-N Phosphine Chemical compound P XYFCBTPGUUZFHI-UHFFFAOYSA-N 0.000 description 2
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical compound C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 description 2
- SMWDFEZZVXVKRB-UHFFFAOYSA-N Quinoline Chemical compound N1=CC=CC2=CC=CC=C21 SMWDFEZZVXVKRB-UHFFFAOYSA-N 0.000 description 2
- 125000000129 anionic group Chemical group 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 229910002804 graphite Inorganic materials 0.000 description 2
- 239000010439 graphite Substances 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 230000005012 migration Effects 0.000 description 2
- 238000013508 migration Methods 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 description 2
- 239000002957 persistent organic pollutant Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000008399 tap water Substances 0.000 description 2
- 235000020679 tap water Nutrition 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 229920000557 Nafion® Polymers 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 238000007743 anodising Methods 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 230000033558 biomineral tissue development Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000010406 cathode material Substances 0.000 description 1
- 150000001767 cationic compounds Chemical class 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000007772 electrode material Substances 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 231100001261 hazardous Toxicity 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- -1 hydroxyl radical free radical Chemical class 0.000 description 1
- QWPPOHNGKGFGJK-UHFFFAOYSA-N hypochlorous acid Chemical compound ClO QWPPOHNGKGFGJK-UHFFFAOYSA-N 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 229910001411 inorganic cation Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000001473 noxious effect Effects 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 229910000073 phosphorus hydride Inorganic materials 0.000 description 1
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 1
- 230000010287 polarization Effects 0.000 description 1
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007784 solid electrolyte Substances 0.000 description 1
- 239000003115 supporting electrolyte Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Landscapes
- Water Treatment By Electricity Or Magnetism (AREA)
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
A kind of adopt anion-exchange membrane solid state electrolyte electrolytic cell assembly, comprise ion-exchange membrane and at the anolyte compartment of ion-exchange membrane both sides and cathode compartment; Anolyte compartment comprises anode end plate, porous anode propping material and anode catalyst layer; Cathode compartment comprises cathode end plate and porous cathode catalytic material; Ion exchange membrane material is anion-exchange membrane.The utility model avoids film and electrode interface fouling in electrolyzer and obtains problem; Slow down the scale formation of ion-exchange membrane greatly, avoid the problem of SPE electrolyzer fouling and clogging, improve stability and the life-span of waste disposal plant.The selection of the utility model to SPE electric tank cathode catalytic material also can be widened, and significantly can reduce the cost of waste disposal plant.
Description
Technical field
The utility model relates to field of environment protection water treatment industry technical field, especially relates to a kind of employing anion-exchange membrane solid state electrolyte electrolytic cell assembly.
Background technology
Many biochemical property of industrial waste waters are poor, comprise numerous inorganic and aromatic series hazardous and noxious substances such as a large amount of ammonia, cyanogen, phenols, pyridine, quinoline in addition, are difficult to biochemical degradation.Electrochemical advanced oxidation is the effective ways of this type of trade effluent of process, the free radical (as hydroxyl radical free radical direct oxidation) that electrochemical oxidation utilizes electrode surface to produce or the oxygenant (as hypochlorous acid indirect oxidation) generated, can the efficient oxidation degraded organic pollutants.In addition, negative electrode can under lower electromotive force, and in negative electrode generation electrical catalyze reduction water, proton produces hydrogen.But greater energy consumption is unanimously the bottleneck that puzzlement electrooxidation technology is applied to wastewater treatment, and due to the open by design of traditional electrolyte groove, negative electrode produces hydrogen and cannot effectively reclaim.Canadian Studies personnel adopt the electrolyzer based on SPE proton exchange membrane Curve guide impeller effectively reduce interelectrode distance and reduce energy consumption, evade the cost increase problem that Xiang Yuanshui adds supporting electrolyte, and utilize proton exchange membrane to intercept the anode chamber and the cathode chamber, be effectively separated anode producing chlorine and negative electrode institute hydrogen producing (WO2012/167375).But the solid electrolyte adopted in this utility model is cationic exchange membrane (as the Nafion film etc. that DuPont company produces), and negative electrode adopts the cathode catalysis layer containing Pt/C greatly to improve electrolyzer cost.Because proton exchange membrane cannot avoid positively charged ion from anode to the migration of negative electrode, therefore, in electrolytic process, except the proton produced in the oxidation of anode organic waste water is to except cathodic migration, the inorganic cation in waste water is (as Na
+, Ca
2+, Mg
2+deng) also can move to negative electrode, at cathode side and a large amount of OH produced because producing hydrogen
-ionic bond generates alkali.Therefore, this design of electrolysis cells unavoidably in the fouling of negative electrode generation BS (as Ca (OH)
2, Mg (OH)
2deng), long-play must bring the blocking of cathode gas diffusion layer and the increase of cathodic polarization, energy consumption is increased and reduces cathode life.Therefore, need badly the aspect such as mould material and film type, cathode construction, electrode materials of SPE " zero spacing " electrolyzer and operating method are improved.
Utility model content
The purpose of this utility model is to design a kind of novel employing anion-exchange membrane solid state electrolyte electrolytic cell assembly, solves the problem.
To achieve these goals, the technical solution adopted in the utility model is as follows:
A kind of adopt anion-exchange membrane solid state electrolyte electrolytic cell assembly, comprise ion-exchange membrane and at the anolyte compartment of described ion-exchange membrane both sides and cathode compartment;
Described anolyte compartment comprises anode end plate, porous anode propping material and anode catalyst layer, described anode end plate is provided with anode flow field groove towards the side of described ion-exchange membrane, the feed-water end of described anode flow field groove is provided with anode water-in, and the water side of described anode flow field groove is provided with anode water outlet; Described anode catalyst layer and the sealing of described porous anode propping material are arranged between described anode end plate and described ion-exchange membrane; Described anode catalyst layer between described ion-exchange membrane and described porous anode propping material, and is close on described porous anode propping material; Described porous anode propping material is provided with anode collector, and described anode collector sealing is stretched out outside described anode end plate and described ion-exchange membrane;
Described cathode compartment comprises cathode end plate and porous cathode catalytic material, described cathode end plate is provided with cathode flow field groove towards the side of described ion-exchange membrane, the feed-water end of described cathode flow field groove is provided with negative electrode water-in, and the water side of described cathode flow field groove is provided with negative electrode water outlet; Described porous cathode catalytic material sealing is arranged between described cathode end plate and described ion-exchange membrane; Described porous cathode catalytic material is provided with cathode current collector, and described cathode current collector sealing is stretched out outside described cathode end plate and described ion-exchange membrane;
Described ion exchange membrane material is anion-exchange membrane.
Described porous sun propping material is corrosion resistant wire establishment net, and its order number is 50-400 order, and diameter wiry is 10-500 micron, and the thickness of wire cloth is 100-1000 micron;
Described anode catalyst layer is RuO
2-TiO
2, PbO
2, SnO
2-Sb
2o
3, Nb
2o
5-SnO
2, SnO
2-In
2o
3, IrO
2-Ta
2o
5, or rare-earth oxide/Sb
2o
5-SnO
2in one or more mixture.
Described corrosion resistant wire comprises tungsten filament, titanium silk, molybdenum filament or niobium silk.
Described corrosion resistant wire establishment net is titanium foam net, and the thickness of described titanium foam net is 300 microns-2000 microns;
Or described corrosion resistant wire establishment net is POROUS TITANIUM PLATE, and the thickness of described POROUS TITANIUM PLATE is 500 microns-3000 microns, and porosity is greater than 40%.
Described cathode end plate is that nickel or stainless steel nickel plating are made;
The design of described cathode flow field groove is consistent with described anode flow field groove, is laterally or longitudinally snakelike, pectination groove arrangement, groove width 1-3 millimeter, groove depth 0.5-2.0 millimeter, and two or three flow path groove walks abreast setting, and flow field conduit terminates to water outlet from water-in;
Described porous cathode catalytic material is the cathode for hydrogen evolution electrocatalysis material be applicable in alkaline water electrolytic cell.
Described cathode for hydrogen evolution electrocatalysis material comprises Ni, Raney Ni, Ni-S, Ni-Mo, or Ni-Mo-S.
Described cathode compartment is closely connected with described anolyte compartment, and only intercepted separately by described ion-exchange membrane, the thickness of described ion exchange membrane material is 50 microns-150 microns
Also comprise silica gel sealing ring, sealed by described silica gel sealing ring between described anode end plate and described ion-exchange membrane, also sealed by described silica gel sealing ring between described cathode end plate and described ion-exchange membrane.
The utility model object is to provide a kind of based on a kind of novel design based on anionic solid state electrolyte " zero spacing " electrolytic cell assembly and improvement, the fouling and clogging problem that the replacement of the middle SPE electrolyzer high cost cathode material of solution international monopoly PCT (WO2012/167375) and negative electrode produce alkali and cause, the final SPE electrolytic cell assembly obtaining a kind of novel low energy consumption high-efficiency electrochemicial oxidation organic wastewater with difficult degradation thereby.
The utility model provides a kind of efficient, economic treatment process changing traditional organic wastewater with difficult degradation thereby, and the energy in efficient recovery waste water.The utility model utilizes " zero spacing " electrolyzer based on ion-exchange membrane, under the condition of impressed voltage 2.5-4V, anode efficient mineralization decomposes Persistent organic pollutants and ammonia nitrogen in organic waste water, the proton that organic substance decomposing can produce by negative electrode also originates in hydrogen under the effect of nickel-base catalyst, is reclaimed the energy.The utility model unique distinction utilizes anion-exchange membrane to replace cationic exchange membrane, and introduce circulating water flow at negative electrode, slow down the scale formation of ion-exchange membrane cathode side greatly, avoid negative electrode and produce because of positively charged ion the problem that alkali causes electrode blockage, improve the stability of waste disposal plant.
The beneficial effects of the utility model can be summarized as follows:
(1), after adopting anion-exchange membrane to instead of cationic exchange membrane in the utility model, there is reduction generation hydrogen at negative electrode and produce OH simultaneously in water
-, be delivered to anode side by anion-exchange membrane from cathode side, the proton that the oxidation operation in anode side waste water produces is combined and generates water, thus avoids film and electrode interface fouling in electrolyzer and obtain problem; Slow down the scale formation of ion-exchange membrane greatly, avoid the problem of SPE electrolyzer fouling and clogging, improve stability and the life-span of waste disposal plant.
(2) in addition, after adopting anion-exchange membrane to instead of cationic exchange membrane in the utility model, also can widen the selection of SPE electric tank cathode catalytic material, catalyst based and collector of Ni base, Fe etc. such as can be adopted to instead of the noble metal catalysts such as the Pt in cationic SPE electrolyzer, replace graphite bi-polar plate etc. with Ti base bipolar plates, significantly can reduce the cost of waste disposal plant.
Accompanying drawing explanation
Fig. 1 is the structural representation of the main apparent direction of the utility model SPE electrooxidation system
Fig. 2 is the stretch-out view of the utility model SPE electrooxidation system.
Wherein: 1. anode end plate 1,2. anode flow field groove 2; 3. silica gel sealing ring 3; 4. porous anode propping material 4; 5. anode catalyst layer 5; 6. anode collector 6; 7. ion-exchange membrane 7; 8. cathode current collector 8; 9. porous cathode catalytic material 9; 10. cathode flow field groove 10; 11. cathode end plate 11; 101. anode water-ins 101 (waste water); 102. anode water outlets 102 (process water); 201. negative electrode water-ins 201 (tap water); 202. negative electrode water outlets 202.
Embodiment
The technical problem solved to make the utility model, technical scheme and beneficial effect are clearly understood, below in conjunction with drawings and Examples, are further elaborated to the utility model.Should be appreciated that specific embodiment described herein only in order to explain the utility model, and be not used in restriction the utility model.
One as depicted in figs. 1 and 2 adopts anion-exchange membrane solid state electrolyte electrolytic cell assembly, comprises ion-exchange membrane 7 and at the anolyte compartment of described ion-exchange membrane 7 both sides and cathode compartment; Described anolyte compartment comprises anode end plate 1, porous anode propping material 4 and anode catalyst layer 5, described anode end plate 1 is provided with anode flow field groove 2 towards the side of described ion-exchange membrane 7, the feed-water end of described anode flow field groove 2 is provided with anode water-in 101, and the water side of described anode flow field groove 2 is provided with anode water outlet 102; Described anode catalyst layer 5 and the sealing of described porous anode propping material 4 are arranged between described anode end plate 1 and described ion-exchange membrane 7; Described anode catalyst layer 5 between described ion-exchange membrane 7 and described porous anode propping material 4, and is close on described porous anode propping material 4; Described porous anode propping material 4 is provided with anode collector 6, and described anode collector 6 sealing is stretched out outside described anode end plate 1 and described ion-exchange membrane 7; Described cathode compartment comprises cathode end plate 11 and porous cathode catalytic material 9, described cathode end plate 11 is provided with cathode flow field groove 10 towards the side of described ion-exchange membrane 7, the feed-water end of described cathode flow field groove 10 is provided with negative electrode water-in 201, and the water side of described cathode flow field groove 10 is provided with negative electrode water outlet 202; Described porous cathode catalytic material 9 sealing is arranged between described cathode end plate 11 and described ion-exchange membrane 7; Described porous cathode catalytic material 9 is provided with cathode current collector 8, and described cathode current collector 8 sealing is stretched out outside described cathode end plate 11 and described ion-exchange membrane 7; Described ion-exchange membrane 7 material is anion-exchange membrane.
In the embodiment be more preferably, described porous sun propping material is corrosion resistant wire establishment net, and its order number is 50-400 order, and diameter wiry is 10-500 micron, and the thickness of wire cloth is 100-1000 micron; Described anode catalyst layer 5 is RuO
2-TiO
2, PbO
2, SnO
2-Sb
2o
3, Nb
2o
5-SnO
2, SnO
2-In
2o
3, IrO
2-Ta
2o
5, or rare-earth oxide/Sb
2o
5-SnO
2in one or more mixture.
In the embodiment be more preferably, described corrosion resistant wire comprises tungsten filament, titanium silk, molybdenum filament or niobium silk.
In the embodiment be more preferably, described corrosion resistant wire establishment net is titanium foam net, and the thickness of described titanium foam net is 300 microns-2000 microns; Or described corrosion resistant wire establishment net is POROUS TITANIUM PLATE, and the thickness of described POROUS TITANIUM PLATE is 500 microns-3000 microns, and porosity is greater than 40%.
In the embodiment be more preferably, described cathode end plate 11 is made for nickel or stainless steel nickel plating; Described cathode flow field groove 10 designs consistent with described anode flow field groove 2, is that laterally or longitudinally snakelike, comb Installed groove is arranged, groove width 1-3 millimeter, groove depth 0.5-2.0 millimeter, and two or three flow path groove walks abreast and arranges flow field conduit and terminate to water outlet from water-in; Described porous cathode catalytic material 9 is for being applicable to the cathode for hydrogen evolution electrocatalysis material in alkaline water electrolytic cell.
In the embodiment be more preferably, described cathode for hydrogen evolution electrocatalysis material comprises Ni, Raney Ni, Ni-S, Ni-Mo, or Ni-Mo-S.
In the embodiment be more preferably, described cathode compartment is closely connected with described anolyte compartment, and only intercepted separately by described ion-exchange membrane 7, the thickness of described ion-exchange membrane 7 material is 50 microns-150 microns
In the embodiment be more preferably, described employing anion-exchange membrane solid state electrolyte electrolytic cell assembly also comprises silica gel sealing ring, sealed by described silica gel sealing ring 3 between described anode end plate 1 and described ion-exchange membrane 7, also sealed by described silica gel sealing ring 3 between described cathode end plate 11 and described ion-exchange membrane 7.
In certain specific embodiment:
(1) in the utility model, anolyte compartment is made up of anode end plate 1, anode flow field groove 10, silica gel sealing ring 3, anode collector 6, porous anode propping material 4, anode catalyst layer 5, wherein porous sun propping material is the corrosion resistant wire establishment such as tungsten filament, titanium silk, molybdenum filament, niobium silk net, its order number is 50-400 order, diameter wiry is 10-500 micron, and the thickness of wire cloth is 100 microns-1000 microns; As with titanium foam net as anode support material, its thickness is about 300 microns-2000 microns; As done support material by POROUS TITANIUM PLATE, its thickness is 500-3000 micron, and porosity is greater than 40%; Anode catalyst layer 5 is RuO
2-TiO
2, PbO
2, SnO
2-Sb
2o
3, Nb
2o
5-SnO
2, SnO
2-In
2o
3, IrO
2-Ta
2o
5, or rare-earth oxide/Sb
2o
5-SnO
2in one or more mixture.
(2), in the utility model, negative electrode is by cathode end plate 11, cathode flow field groove 10, silica gel sealing ring 3, porous cathode catalytic material 9, and cathode current collector 8 five part forms; Cathode end plate 11 is made for the material such as nickel or stainless steel nickel plating, cathode flow field 10 designs consistent with anode flow field, for horizontal or longitudinally snakelike, pectination groove arrangement, groove width 1-3 millimeter, groove depth 0.5-2.0 millimeter, two or three flow path groove is parallel to be arranged, and flow field conduit terminates to water outlet from water-in; Porous cathode catalytic material 9 for being applicable to the cathode for hydrogen evolution electrocatalysis material in alkaline water electrolytic cell, as Ni, Raney Ni, Ni-S, Ni-Mo, Ni-Mo-S etc.;
(3) cathode compartment of the utility model " zero spacing " electrolyzer is closely connected with anolyte compartment, only intercept separately by ion-exchange membrane 7, ion-exchange membrane 7 material used be anion-exchange membrane (as quaternary amine salt form anion-exchange membrane, season phosphine type anion-exchange membrane etc.), the thickness of film is 50-150 micron (μm); On " zero spacing " electrolyzer to apply operating voltage be 2-4 volt, electric tank working current density is 1-20 milliampere/square centimeter;
(4) SPE anode electrolytic cell, negative plate respectively have a water-in in the utility model, water-in is connected with top, flow field bottom pole plate; SPE anode electrolytic cell, negative electrode respectively have a water outlet, and water outlet is located at pole plate upper side, are connected with flow field end.
(5) organic waste water is with 0.02-0.10ml/cm
2.min flow velocity enters from the import of anionic SPE anode electrolytic cell, is degraded and mineralising under the effect of anode generation electrooxidation, and process water is discharged from anode export;
(6) negative electrode water inlet is tap water or anodizing water, and the hydrogen that negative electrode produces flows out from cathode outlet, and after gas obtains separation, liquid recycle flows into negative electrode.
Compared with prior art, the utility model tool has the following advantages:
(1), after adopting anion-exchange membrane to instead of cationic exchange membrane in the utility model, there is reduction generation hydrogen at negative electrode and produce OH simultaneously in water
-, be delivered to anode side by anion-exchange membrane from cathode side, the proton that the oxidation operation in anode side waste water produces is combined and generates water, thus avoids film and electrode interface fouling in electrolyzer and obtain problem; Avoid the problem of SPE electrolyzer fouling and clogging, improve stability and the life-span of waste disposal plant.
(2) in addition, after adopting anion-exchange membrane to instead of cationic exchange membrane in the utility model, also can widen the selection of SPE electric tank cathode catalytic material, catalyst based and collector of Ni base, Fe etc. such as can be adopted to instead of the noble metal catalysts such as the Pt in cationic SPE electrolyzer, replace graphite endplates etc. with Ti cardinal extremity plate, significantly can reduce the cost of waste disposal plant.
The utility model is described in detail in preferred embodiment above by concrete; but those skilled in the art should be understood that; the utility model is not limited to the above embodiment; all within spirit of the present utility model and principle; any amendment of doing, equivalent replacement etc., all should be included within protection domain of the present utility model.
Claims (8)
1. adopt an anion-exchange membrane solid state electrolyte electrolytic cell assembly, it is characterized in that: comprise ion-exchange membrane and at the anolyte compartment of described ion-exchange membrane both sides and cathode compartment;
Described anolyte compartment comprises anode end plate, porous anode propping material and anode catalyst layer, described anode end plate is provided with anode flow field groove towards the side of described ion-exchange membrane, the feed-water end of described anode flow field groove is provided with anode water-in, and the water side of described anode flow field groove is provided with anode water outlet; Described anode catalyst layer and the sealing of described porous anode propping material are arranged between described anode end plate and described ion-exchange membrane; Described anode catalyst layer between described ion-exchange membrane and described porous anode propping material, and is close on described porous anode propping material; Described porous anode propping material is provided with anode collector, and described anode collector sealing is stretched out outside described anode end plate and described ion-exchange membrane;
Described cathode compartment comprises cathode end plate and porous cathode catalytic material, described cathode end plate is provided with cathode flow field groove towards the side of described ion-exchange membrane, the feed-water end of described cathode flow field groove is provided with negative electrode water-in, and the water side of described cathode flow field groove is provided with negative electrode water outlet; Described porous cathode catalytic material sealing is arranged between described cathode end plate and described ion-exchange membrane; Described porous cathode catalytic material is provided with cathode current collector, and described cathode current collector sealing is stretched out outside described cathode end plate and described ion-exchange membrane; Described ion exchange membrane material is anion-exchange membrane.
2. employing anion-exchange membrane solid state electrolyte electrolytic cell assembly according to claim 1, it is characterized in that: described porous sun propping material is corrosion resistant wire establishment net, its order number is 50-400 order, diameter wiry is 10-500 micron, and the thickness of wire cloth is 100 microns-1000 microns;
Described anode catalyst layer is RuO
2-TiO
2, PbO
2, SnO
2-Sb
2o
3, Nb
2o
5-SnO
2, SnO
2-In
2o
3, IrO
2-Ta
2o
5, or rare-earth oxide/Sb
2o
5-SnO
2in one.
3. employing anion-exchange membrane solid state electrolyte electrolytic cell assembly according to claim 2, is characterized in that: described corrosion resistant wire comprises tungsten filament, titanium silk, molybdenum filament or niobium silk.
4. employing anion-exchange membrane solid state electrolyte electrolytic cell assembly according to claim 2, is characterized in that: described corrosion resistant wire establishment net is titanium foam net, and the thickness of described titanium foam net is 300 microns-2000 microns;
Or described corrosion resistant wire establishment net is POROUS TITANIUM PLATE, and the thickness of described POROUS TITANIUM PLATE is 500 microns-3000 microns, and porosity is greater than 40%.
5. employing anion-exchange membrane solid state electrolyte electrolytic cell assembly according to claim 1, is characterized in that: described cathode end plate is that nickel or stainless steel nickel plating are made;
The design of described cathode flow field groove is consistent with described anode flow field groove, is laterally or longitudinally snakelike, pectination groove arrangement, groove width 1-3 millimeter, groove depth 0.5-2.0 millimeter, and two or three flow path groove walks abreast setting, and flow field conduit terminates to water outlet from water-in;
Described porous cathode catalytic material is the cathode for hydrogen evolution electrocatalysis material be applicable in alkaline water electrolytic cell.
6. employing anion-exchange membrane solid state electrolyte electrolytic cell assembly according to claim 5, is characterized in that: described cathode for hydrogen evolution electrocatalysis material comprises Ni, Raney Ni, Ni-S, Ni-Mo, or Ni-Mo-S.
7. employing anion-exchange membrane solid state electrolyte electrolytic cell assembly according to claim 1, it is characterized in that: described cathode compartment is closely connected with described anolyte compartment, only intercepted separately by described ion-exchange membrane, the thickness of described ion exchange membrane material is 50 microns-150 microns.
8. employing anion-exchange membrane solid state electrolyte electrolytic cell assembly according to claim 1, it is characterized in that: also comprise silica gel sealing ring, sealed by described silica gel sealing ring between described anode end plate and described ion-exchange membrane, also sealed by described silica gel sealing ring between described cathode end plate and described ion-exchange membrane.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104192957A (en) * | 2014-09-11 | 2014-12-10 | 北京今大禹环保技术有限公司 | Solid electrolyte electrolytic cell device using anion-exchange membrane |
| CN105461023A (en) * | 2015-11-06 | 2016-04-06 | 北京航空航天大学 | Electrolytic tank apparatus using oxygen reduction cathode |
| CN111334816A (en) * | 2020-04-20 | 2020-06-26 | 浙江高成绿能科技有限公司 | Method for preparing hypochlorous acid water by electrolysis |
| CN113024031A (en) * | 2021-03-12 | 2021-06-25 | 江西绿建环保科技有限公司 | Integrated membrane coupling-electric flocculation sewage treatment device |
| US11339483B1 (en) | 2021-04-05 | 2022-05-24 | Alchemr, Inc. | Water electrolyzers employing anion exchange membranes |
-
2014
- 2014-09-11 CN CN201420519820.7U patent/CN204111387U/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104192957A (en) * | 2014-09-11 | 2014-12-10 | 北京今大禹环保技术有限公司 | Solid electrolyte electrolytic cell device using anion-exchange membrane |
| CN105461023A (en) * | 2015-11-06 | 2016-04-06 | 北京航空航天大学 | Electrolytic tank apparatus using oxygen reduction cathode |
| WO2017076282A1 (en) * | 2015-11-06 | 2017-05-11 | 北京航空航天大学 | Electrolytic tank apparatus using oxygen reduction cathode |
| CN105461023B (en) * | 2015-11-06 | 2018-08-10 | 北京航空航天大学 | A kind of electrolytic cell assembly using oxygen reduction cathode |
| CN111334816A (en) * | 2020-04-20 | 2020-06-26 | 浙江高成绿能科技有限公司 | Method for preparing hypochlorous acid water by electrolysis |
| CN113024031A (en) * | 2021-03-12 | 2021-06-25 | 江西绿建环保科技有限公司 | Integrated membrane coupling-electric flocculation sewage treatment device |
| US11339483B1 (en) | 2021-04-05 | 2022-05-24 | Alchemr, Inc. | Water electrolyzers employing anion exchange membranes |
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