CN204151114U - A kind of cloth water structure of SPE electrolyzer - Google Patents
A kind of cloth water structure of SPE electrolyzer Download PDFInfo
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- CN204151114U CN204151114U CN201420519817.5U CN201420519817U CN204151114U CN 204151114 U CN204151114 U CN 204151114U CN 201420519817 U CN201420519817 U CN 201420519817U CN 204151114 U CN204151114 U CN 204151114U
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- water
- anode
- negative electrode
- cathode
- exchange membrane
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 284
- 239000004744 fabric Substances 0.000 title claims abstract description 22
- 239000002351 wastewater Substances 0.000 claims abstract description 54
- 238000000034 method Methods 0.000 claims abstract description 51
- 239000003014 ion exchange membrane Substances 0.000 claims abstract description 46
- 239000000463 material Substances 0.000 claims abstract description 44
- 239000012528 membrane Substances 0.000 claims abstract description 11
- 239000003011 anion exchange membrane Substances 0.000 claims abstract description 5
- 125000002091 cationic group Chemical group 0.000 claims abstract description 5
- 239000003054 catalyst Substances 0.000 claims description 17
- 238000007789 sealing Methods 0.000 claims description 17
- 230000003197 catalytic effect Effects 0.000 claims description 13
- 238000009826 distribution Methods 0.000 abstract description 28
- 239000008399 tap water Substances 0.000 abstract description 6
- 235000020679 tap water Nutrition 0.000 abstract description 6
- 230000000903 blocking effect Effects 0.000 abstract description 2
- 239000001257 hydrogen Substances 0.000 description 24
- 229910052739 hydrogen Inorganic materials 0.000 description 24
- 238000006056 electrooxidation reaction Methods 0.000 description 22
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 18
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 17
- 238000004939 coking Methods 0.000 description 14
- 230000000694 effects Effects 0.000 description 12
- 239000010936 titanium Substances 0.000 description 12
- 238000005265 energy consumption Methods 0.000 description 9
- 230000003647 oxidation Effects 0.000 description 9
- 238000007254 oxidation reaction Methods 0.000 description 9
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 8
- 239000002894 chemical waste Substances 0.000 description 8
- 229910052759 nickel Inorganic materials 0.000 description 8
- 150000002431 hydrogen Chemical class 0.000 description 7
- 229910052719 titanium Inorganic materials 0.000 description 7
- 230000015556 catabolic process Effects 0.000 description 6
- 230000007797 corrosion Effects 0.000 description 6
- 238000005260 corrosion Methods 0.000 description 6
- 238000006731 degradation reaction Methods 0.000 description 6
- 229920000557 Nafion® Polymers 0.000 description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 239000000741 silica gel Substances 0.000 description 5
- 229910002027 silica gel Inorganic materials 0.000 description 5
- 229910006404 SnO 2 Inorganic materials 0.000 description 4
- 238000010277 constant-current charging Methods 0.000 description 4
- 239000010955 niobium Substances 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- 230000001502 supplementing effect Effects 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000003513 alkali Substances 0.000 description 3
- 238000005868 electrolysis reaction Methods 0.000 description 3
- 239000003792 electrolyte Substances 0.000 description 3
- 238000004134 energy conservation Methods 0.000 description 3
- -1 hydroxyl radical free radical Chemical class 0.000 description 3
- 239000011259 mixed solution Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 2
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 2
- 229910003296 Ni-Mo Inorganic materials 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
- NPXOKRUENSOPAO-UHFFFAOYSA-N Raney nickel Chemical compound [Al].[Ni] NPXOKRUENSOPAO-UHFFFAOYSA-N 0.000 description 2
- 229910010413 TiO 2 Inorganic materials 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910052750 molybdenum Inorganic materials 0.000 description 2
- 239000011733 molybdenum Substances 0.000 description 2
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 description 2
- 229910052758 niobium Inorganic materials 0.000 description 2
- GUCVJGMIXFAOAE-UHFFFAOYSA-N niobium atom Chemical compound [Nb] GUCVJGMIXFAOAE-UHFFFAOYSA-N 0.000 description 2
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 description 2
- 238000007747 plating Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 2
- 229910052721 tungsten Inorganic materials 0.000 description 2
- 239000010937 tungsten Substances 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- 230000004308 accommodation Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000007743 anodising Methods 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000001680 brushing effect Effects 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 239000008151 electrolyte solution Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 231100001261 hazardous Toxicity 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
- 239000010842 industrial wastewater Substances 0.000 description 1
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- 230000001473 noxious effect Effects 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
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- 150000002989 phenols Chemical class 0.000 description 1
- 239000000047 product Substances 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
- 229910052761 rare earth metal Inorganic materials 0.000 description 1
- 229910001404 rare earth metal oxide Inorganic materials 0.000 description 1
- 150000002910 rare earth metals Chemical class 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
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- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000003115 supporting electrolyte Substances 0.000 description 1
- 238000001149 thermolysis Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Landscapes
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
A cloth water structure for SPE electrolyzer, comprises water leg, ion-exchange membrane and at the anolyte compartment of ion-exchange membrane both sides and cathode compartment; Ion exchange membrane material is anion-exchange membrane or cationic exchange membrane; Anolyte compartment is provided with anode water-in and anode water outlet, and cathode compartment is provided with negative electrode water-in and negative electrode water outlet, and water leg is provided with water leg water-in and water leg water outlet; Pending waste water source is connected to anode water-in, and anode water outlet is connected to water leg water-in, and water leg water outlet is connected to negative electrode water-in, and negative electrode water outlet is connected to the process water after process.The utility model water distribution manner is simple, without the need to additional tap water as catholyte; PH is low in anode water outlet, greatly reduces negative electrode pH and reduces pH concentration difference between anode and cathode, electrolytic bath pressure is significantly reduced after entering negative electrode; Because negative electrode pH reduces, negative electrode fouling reduces with blocking probability; Final outflow water is close to neutrality.
Description
Technical field
The utility model relates to field of environment protection water treatment industry technical field, especially relates to a kind of cloth water structure of SPE electrolyzer.
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.
The utility model adopts the electrolyzer based on SPE proton exchange membrane Curve guide impeller effectively reduce interelectrode distance and reduce energy consumption, evade that Xiang Yuanshui adds supporting electrolyte and the cost that produces increases problem, and utilize proton exchange membrane to intercept the anode chamber and the cathode chamber, be effectively separated anode producing chlorine, oxygen and negative electrode institute hydrogen producing.But because proton exchange membrane cannot avoid positively charged ion from anode to the infiltration of negative electrode, therefore, negative electrode is at generation H
+while also originating in hydrogen, there is a large amount of OH
-ion and Na
+, Ca
2+generation alkali (reaction formula) is combined Deng positively charged ion.Although utilize liquid cathode design effectively can be reduced in the fouling of negative electrode generation BS (as Ca (OH)
2, NaOH etc.), but long-play still can bring proton exchange membrane at the fouling risk of cathode side, reduces proton exchange membrane conductivity and electrochemical cathode area.
In addition, due to the separation of proton exchange membrane, anode at electro-oxidation process because producing a large amount of H
+anode pH is reduced, and negative electrode is because of large volume production hydrogen consumption H
+, make H
+concentration reduces pH and raises, and brings concentration potential.For overcoming concentration potential and maintaining strength of current, must, by high for the voltage rise of SPE electrolytic bath, energy consumption be caused to increase thus.If additional acid-alkali accommodation anode and cathode pH certainly will increase running cost again, bring the pressure of subsequent disposal water desalination.Therefore, rational SPE electrolyzer operation scheme need be utilized to regulate between SPE yin, yang the two poles of the earth because ion-exchange membrane separates the pH concentration difference produced.
Utility model content
The purpose of this utility model is the cloth water structure designing a kind of novel SPE electrolyzer, solves the problem.
To achieve these goals, the technical solution adopted in the utility model is as follows:
A cloth water structure for SPE electrolyzer, comprises water leg, ion-exchange membrane and at the anolyte compartment of described ion-exchange membrane both sides and cathode compartment; Described ion exchange membrane material is anion-exchange membrane or cationic exchange membrane; Described anolyte compartment is provided with anode water-in and anode water outlet, and described cathode compartment is provided with negative electrode water-in and negative electrode water outlet, and described water leg is provided with water leg water-in and water leg water outlet;
Pending waste water source is connected to described anode water-in, and described anode water outlet is connected to described water leg water-in, and described water leg water outlet is connected to described negative electrode water-in, and described negative electrode water outlet is connected to the process water after process.
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 described anode water-in, and the water side of described anode flow field groove is provided with described 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 described negative electrode water-in, and the water side of described cathode flow field groove is provided with described 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.
Pending waste water source is connected to described anode water-in, and described anode water outlet is connected to described water leg water-in;
Described water leg water outlet is divided into two-way, and a road is connected to the process water after process, and another road is connected to described negative electrode water-in; Described negative electrode water outlet is also connected to described water leg water-in.
Pending waste water source is connected to described negative electrode water-in, and described negative electrode water outlet is connected to described water leg water-in, and described water leg water outlet is connected to described anode water-in, and described anode water outlet is connected to the process water after process.
Pending waste water source is divided into two-way, and a road is directly connected to described water leg water-in, and another road is connected to described negative electrode water-in, and described negative electrode water outlet is connected to described water leg water-in;
Described water leg water outlet is connected to described anode water-in, and described anode water outlet is connected to the process water after process.
A kind of water distribution method using the cloth water structure of SPE electrolyzer described in claim 1 or 2: pending waste water with flow velocity Q for 0.02-0.10ml/cm
2.min described anolyte compartment is entered, pending waste water is degraded and mineralising under the effect of anode generation electrooxidation, process water enters described water leg from described anode water outlet, the water outlet of described water leg flows into cathode compartment with flow velocity Q identical with described anode water-in again, produce after hydrogen through catholyte, discharge SPE electrolyzer.
A kind of water distribution method using the cloth water structure of SPE electrolyzer described in claim 3:
Pending waste water with flow velocity Q for 0.02-0.10ml/cm
2.min enter described anolyte compartment, pending waste water is degraded and mineralising under the effect of anode generation electrooxidation, and process water enters described water leg from described anode water outlet; The water outlet of described water leg enters negative electrode with the flow velocity of 10%-50%Q, and produce after hydrogen through catholyte, negative electrode water outlet is back to described water leg; The water outlet of last described water leg discharges SPE electrolyzer with flow velocity Q.
A kind of water distribution method using the cloth water structure of SPE electrolyzer described in claim 6:
Pending waste water first with flow velocity Q for 0.02-0.10ml/cm
2.min described cathode compartment is entered, pending waste water is discharged from described cathode compartment and is entered described water leg after negative electrode generation electrolytic reduction produces hydrogen, the water outlet of described water leg flows into described anolyte compartment with identical flow velocity Q again, organism is degraded and mineralising in the effect of anode generation electrooxidation, finally discharge SPE electrolyzer.
A kind of water distribution method using the cloth water structure of SPE electrolyzer described in claim 7:
First overall flow rate Q is 0.02-0.10ml/cm by pending waste water
2.min, be distributed into Q1 flow velocity and enter described water leg and 10%-50%Q1 flow velocity enters described cathode compartment, pending waste water is discharged from described cathode compartment and is imported described water leg again and mix with described pending waste water after negative electrode generation electrolytic reduction produces hydrogen; Described water leg mixed solution flows into described anolyte compartment with flow velocity Q again, organism is degraded and mineralising in the effect of anode generation electrooxidation, finally discharges SPE electrolyzer.
The utility model object is to provide a kind of based on solid state electrolyte " zero spacing " water distribution of electrolyzer and the Curve guide impeller of operation scheme, solve the pH concentration difference because ion-exchange membrane separation SPE yin, yang the two poles of the earth produce, and the groove voltage rise brought thus is high and energy consumption increases, the final device obtaining a kind of low energy consumption high-efficiency electrochemicial oxidation organic wastewater with difficult degradation thereby.
This electrooxidation design of electrolysis cells as depicted in figs. 1 and 2.
(1) in the utility model, anolyte compartment is made up of anode end plate, anode flow field, silica gel sealing ring, anode collector, porous anode propping material, anode catalyst layer, 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 is RuO
2-TiO
2, PbO
2, SnO
2-Sb2O
3, Nb
2o
5-SnO
2, SnO
2-In
2o
3, IrO
2-Ta
2o
5, rare-earth oxide-SnO
2in one or more mixture.
(2), in the utility model, negative electrode is by cathode end plate, cathode flow field, silica gel sealing ring, porous cathode catalytic material, and cathode current collector five part forms; Cathode end plate is that the material such as nickel or stainless steel nickel plating is made, cathode flow field design is 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 is the cathode for hydrogen evolution electrocatalysis material be applicable in alkaline water electrolytic cell, as Ni, Raney Ni, and 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, ion exchange membrane material used is cationic exchange membrane (as Nafion film) or anion-exchange membrane, and 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) in the utility model there is following several water distribution manner in SPE electrolyzer, as shown in Figures 3 to 6:
A () as shown in Figure 3, waste water is with flow velocity Q (0.02-0.10ml/cm
2.min) SPE anode electrolytic cell (step 311) is entered, waste water is degraded and mineralising under the effect of anode generation electrooxidation, process water enters water leg (step 312) from anode export, water-collecting tank water is flowed into negative electrode (step 313) with flow velocity Q identical with anode again, produce after hydrogen through catholyte, discharge SPE electrolyzer (step 314).
B () as shown in Figure 4, waste water is with flow velocity Q (0.02-0.10ml/cm
2.min) enter SPE anode electrolytic cell (step 321), waste water is degraded and mineralising under the effect of anode generation electrooxidation, and process water enters water leg (step 322) from anode export; Water-collecting tank water enters negative electrode (step 323) with the flow velocity of 10%-50%Q, and produce after hydrogen through catholyte, negative electrode water outlet is back to water leg (step 324); Last water-collecting tank water discharges SPE electrolyzer (step 325) with flow velocity Q.
E () as shown in Figure 5, waste water is first with flow velocity Q (0.02-0.10ml/cm
2.min) SPE electric tank cathode (step 351) is entered, waste water is discharged from negative electrode and is entered water leg (step 352) after negative electrode generation electrolytic reduction produces hydrogen, water-collecting tank water flows into anode (step 353) with identical flow velocity Q again, organism is degraded and mineralising in the effect of anode generation electrooxidation, finally discharge SPE electrolyzer system (step 354).
F () as shown in Figure 6, waste water is first by overall flow rate Q (0.02-0.10ml/cm
2.min), be distributed into Q1 flow velocity and enter water leg (step 361) and 10%-50%Q1 flow velocity enters SPE electric tank cathode (step 362), waste water is discharged from negative electrode and is imported water leg again and mix (step 363) with raw wastewater after negative electrode generation electrolytic reduction produces hydrogen; Water leg mixed solution flows into anode (step 364) with flow velocity Q again, organism is degraded and mineralising in the effect of anode generation electrooxidation, finally discharges SPE electrolyzer system (step 365).
In the utility model, 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 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 or more mixture; In the utility model, described corrosion resistant wire comprises tungsten filament, titanium silk, molybdenum filament or niobium silk.
In the utility model, described corrosion resistant wire establishment net is titanium mesh grid net, and the thickness of described titanium 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 utility model, 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 the snakelike groove arrangement of longitudinal direction, groove width 2-5 millimeter, groove depth 1-3 millimeter, 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.
In the utility model, described cathode for hydrogen evolution electrocatalysis material comprises Ni, Raney Ni, Ni-S, Ni-Mo, or Ni-Mo-S.
In the utility model, 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.
In the utility model, also comprise silicon 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 beneficial effects of the utility model can be summarized as follows:
A () as shown in Figure 3, this kind of water distribution manner (a) is the simplest, without the need to additional tap water as catholyte; PH is low in anode water outlet, greatly reduces negative electrode pH and reduces pH concentration difference between anode and cathode, electrolytic bath pressure is significantly reduced after entering negative electrode; Because negative electrode pH reduces, negative electrode fouling reduces with blocking probability; Final outflow water is close to neutrality.
B () as shown in Figure 4, the characteristic of this kind of water distribution manner is similar to method a, anodizing water section passes back into negative electrode, without the need to additional tap water as catholyte; Anode water outlet mixes with negative electrode water outlet, and adjusting water outlet pH is close to neutral; Partially disposed water is back to negative electrode, avoids negative electrode pH too high, reduces negative electrode fouling, corrosion and reduction product probability, is reduced and energy-conservation with time slot pressure.
E () as shown in Figure 5, this kind of water distribution manner is similar to method a, but direction is contrary, and water distribution manner is the simplest equally, without the need to additional tap water as electrolytic solution; Using waste water as electrolyte stream through negative electrode, negative electrode pH can be avoided too high, reduce negative electrode fouling probability, reduction groove pressure is also energy-conservation; Waste water is after catholyte, and pH is raised, then enter anode can be conducive to electrooxidation produce hydroxyl radical free radical.
F () as shown in Figure 6, in this kind of water distribution manner, negative electrode utilizes waste water and supplements as catholyte without the need to additional tap water, and negative electrode pH can be avoided too high, reduce negative electrode fouling probability, and reduction electrolytic bath pressure is also energy-conservation; Enter anode after negative electrode water outlet mixes with waste water, make anode water inlet meta-alkali, be conducive to the generation of hydroxyl radical free radical and the generation of electrooxidation.
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: anode end plate 1, anode flow field groove 2; Silica gel sealing ring 3; Porous anode propping material 4; Anode catalyst layer 5; Anode collector 6; Ion-exchange membrane 7; Cathode current collector 8; Porous cathode catalytic material 9; Cathode flow field groove 10; Cathode end plate 11; Anode water-in 101 (waste water); Anode water outlet 102 (process water); Negative electrode water-in 201 (tap water); Negative electrode water outlet 202.
Fig. 3 is a kind of water distribution manner of SPE electrolyzer.
The another kind of water distribution manner of Fig. 4 most SPE electrolyzer.
Another water distribution manner of Fig. 5 most SPE electrolyzer.
Another water distribution manner of Fig. 6 most SPE electrolyzer.
Wherein, water leg 31; Anolyte compartment 32; Cathode compartment 33; Waste water source 34.
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.
The cloth water structure of a kind of SPE electrolyzer as shown in Figures 1 to 6, comprises water leg, ion-exchange membrane and at the anolyte compartment of described ion-exchange membrane both sides and cathode compartment; Described ion exchange membrane material is anion-exchange membrane or cationic exchange membrane; Described anolyte compartment is provided with anode water-in and anode water outlet, and described cathode compartment is provided with negative electrode water-in and negative electrode water outlet, and described water leg is provided with water leg water-in and water leg water outlet; Pending waste water source is connected to described anode water-in, and described anode water outlet is connected to described water leg water-in, and described water leg water outlet is connected to described negative electrode water-in, and described negative electrode water outlet is connected to the process water after process.
In the embodiment be more preferably, 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 described anode water-in, and the water side of described anode flow field groove is provided with described 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 described negative electrode water-in, and the water side of described cathode flow field groove is provided with described 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.
In the embodiment be more preferably, pending waste water source is connected to described anode water-in, and described anode water outlet is connected to described water leg water-in; Described water leg water outlet is divided into two-way, and a road is connected to the process water after process, and another road is connected to described negative electrode water-in; Described negative electrode water outlet is also connected to described water leg water-in.
In the embodiment be more preferably, pending waste water source is connected to described negative electrode water-in, described negative electrode water outlet is connected to described water leg water-in, and described water leg water outlet is connected to described anode water-in, and described anode water outlet is connected to the process water after process.
In the embodiment be more preferably, pending waste water source is divided into two-way, and a road is directly connected to described water leg water-in, and another road is connected to described negative electrode water-in, and described negative electrode water outlet is connected to described water leg water-in; Described water leg water outlet is connected to described anode water-in, and described anode water outlet is connected to the process water after process.
A kind of method for supplementing water using the cloth water structure of the SPE electrolyzer shown in Fig. 3: pending waste water with flow velocity Q for 0.02-0.10ml/cm
2.min described anolyte compartment is entered, pending waste water is degraded and mineralising under the effect of anode generation electrooxidation, process water enters described water leg from described anode water outlet, the water outlet of described water leg flows into cathode compartment with flow velocity Q identical with described anode water-in again, produce after hydrogen through catholyte, discharge SPE electrolyzer.
A kind of method for supplementing water using the cloth water structure of the SPE electrolyzer shown in Fig. 4:
Pending waste water with flow velocity Q for 0.02-0.10ml/cm
2.min enter described anolyte compartment, pending waste water is degraded and mineralising under the effect of anode generation electrooxidation, and process water enters described water leg from described anode water outlet; The water outlet of described water leg enters negative electrode with the flow velocity of 10%-50%Q, and produce after hydrogen through catholyte, negative electrode water outlet is back to described water leg; The water outlet of last described water leg discharges SPE electrolyzer with flow velocity Q.
A kind of method for supplementing water using the cloth water structure of the SPE electrolyzer shown in Fig. 5:
Pending waste water first with flow velocity Q for 0.02-0.10ml/cm
2.min described cathode compartment is entered, pending waste water is discharged from described cathode compartment and is entered described water leg after negative electrode generation electrolytic reduction produces hydrogen, the water outlet of described water leg flows into described anolyte compartment with identical flow velocity Q again, organism is degraded and mineralising in the effect of anode generation electrooxidation, finally discharge SPE electrolyzer.
The method for supplementing water of the cloth water structure of the SPE electrolyzer of a kind of use shown in Fig. 6:
First overall flow rate Q is 0.02-0.10ml/cm by pending waste water
2.min, be distributed into Q1 flow velocity and enter described water leg and 10%-50%Q1 flow velocity enters described cathode compartment, pending waste water is discharged from described cathode compartment and is imported described water leg again and mix with described pending waste water after negative electrode generation electrolytic reduction produces hydrogen; Described water leg mixed solution flows into described anolyte compartment with flow velocity Q again, organism is degraded and mineralising in the effect of anode generation electrooxidation, finally discharges SPE electrolyzer.
Embodiment 1
SPE electrolyzer adopts the mesh grid of Ti silk, by brushing SnCl
4and SbCl
3(by 9:1, total concn 1.1mol/L) butanol solution, dries 5min for 125 DEG C, 500 DEG C of thermolysis sintering 5min, reciprocating operation 10 times, preparation Ti/SnO
2-Sb
2o
5solid solution anode catalyst layer 5; Adopt nickel screen as negative electrode, yin, yang the two poles of the earth are separated with ion-exchange membrane 7 (as Nafion), and electrode useful area is all as 150cm
2.SPE electrolyzer electrooxidation Treatment of Wastewater in Coking operation scheme is as follows: SPE electrolyzer carries out water distribution (as Fig. 3) according to water distribution manner a, namely coking chemical waste water enters SPE anode electrolytic cell (step 311) with certain flow rate, after anode electrolytic cell electrolytic oxidation, process water imports water leg (step 312); Water-collecting tank water enters SPE electric tank cathode (step 313) with flow velocity identical with anode, produces after hydrogen through catholyte, and process water discharges SPE electrolyzer system (step 314).Pass into direct current between SPE electrolyzer cathode and anode, adopt constant current charging mode to run.
When the initial COD concentration of coking chemical waste water is 280mg/L, SPE electrolyzer is with under different in flow rate, different current density, and in reaction process, SPE electrolytic bath pressure, effluent COD concentration, COD degradation rate and electric energy energy consumption are as shown in table 1:
SPE electrolyzer Treatment of Wastewater in Coking under table 1 water distribution manner a
Embodiment 2
SPE electrolyzer adopts the mesh grid of Ti silk, and anode catalyst layer preparation method is as embodiment 1; Adopt nickel screen as negative electrode, yin, yang the two poles of the earth are separated with ion-exchange membrane 7 (as Nafion), and electrode useful area is all as 150cm
2.SPE electrolyzer electrooxidation Treatment of Wastewater in Coking operation scheme is as follows: SPE electrolyzer carries out water distribution (as Fig. 4) according to water distribution manner b, namely coking chemical waste water enters SPE anode electrolytic cell (step 321) with flow velocity Q1, after anode electrolytic cell electrolytic oxidation, process water enters water leg (step 322); In water-collecting tank water, a part enters electric tank cathode (step 323) with the flow velocity Q2 of 10-50%Q1, produces after hydrogen, then pass back into water leg (step 324) through catholyte; Final process water with Q1 from water leg outflow system.Pass into direct current between SPE electrolyzer cathode and anode, adopt constant current charging mode to run.
When the initial COD concentration of coking chemical waste water is 280mg/L, SPE electrolyzer is to run under different in flow rate, different current density condition, and in reaction process, SPE electrolytic bath pressure, effluent COD concentration, COD degradation rate and electric energy energy consumption are as shown in table 2:
SPE electrolyzer Treatment of Wastewater in Coking under table 2 water distribution manner b
Embodiment 3
SPE electrolyzer adopts the mesh grid of Ti silk, and anode catalyst layer preparation method is as embodiment 1; Adopt nickel screen as negative electrode, yin, yang the two poles of the earth are separated with ion-exchange membrane 7 (as Nafion), and electrode useful area is all as 150cm
2.SPE electrolyzer carries out water distribution (as Fig. 5) according to water distribution manner e, carrying out practically mode is as follows: coking chemical waste water enters SPE electric tank cathode (step 351) with flow velocity Q, after electric tank cathode electrolysis liberation of hydrogen, waste water enters water leg (step 352); Water-collecting tank water enters anode electrolytic cell (step 353) with flow velocity Q again, after anodic oxidation process, and final outflow SPE anode (step 354).Pass into direct current between SPE electrolyzer cathode and anode, adopt constant current charging mode to run.
When the initial COD concentration of coking chemical waste water is 280mg/L, SPE electrolyzer is to run under different in flow rate, different current density condition, and in reaction process, SPE electrolytic bath pressure, effluent COD concentration, COD degradation rate and electric energy energy consumption are as shown in table 3:
SPE electrolyzer Treatment of Wastewater in Coking under table 3 water distribution manner e
Embodiment 4
SPE electrolyzer adopts the mesh grid of Ti silk, and anode catalyst layer preparation method is as embodiment 1; Adopt nickel screen as negative electrode, yin, yang the two poles of the earth are separated with ion-exchange membrane 7 (as Nafion), and electrode useful area is all as 150cm
2.SPE electrolyzer carries out water distribution (as Fig. 6) according to water distribution manner f, carrying out practically mode is as follows: coking chemical waste water flows to water leg (step 361) and SPE electric tank cathode (step 362) with flow velocity Q1, Q2 (Q1/Q2=1-5) respectively, Q2 effluent part after electric tank cathode electrolysis liberation of hydrogen, then flows into water leg (step 363); In water leg, water enters anode electrolytic cell (step 364) with flow velocity Q (Q=Q1+Q2) again, after anodic oxidation process, and final outflow SPE anode (step 365).Pass into direct current between SPE electrolyzer cathode and anode, adopt constant current charging mode to run.
When the initial COD concentration of coking chemical waste water is 280mg/L, SPE electrolyzer is to run under different in flow rate, different current density condition, and in reaction process, SPE electrolytic bath pressure, effluent COD concentration, COD degradation rate and electric energy energy consumption are as shown in table 4:
SPE electrolyzer Treatment of Wastewater in Coking under table 4 water distribution manner f
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 (5)
1. a cloth water structure for SPE electrolyzer, is characterized in that: comprise water leg, ion-exchange membrane and at the anolyte compartment of described ion-exchange membrane both sides and cathode compartment; Described ion exchange membrane material is anion-exchange membrane or cationic exchange membrane; Described anolyte compartment is provided with anode water-in and anode water outlet, and described cathode compartment is provided with negative electrode water-in and negative electrode water outlet, and described water leg is provided with water leg water-in and water leg water outlet;
Pending waste water source is connected to described anode water-in, and described anode water outlet is connected to described water leg water-in, and described water leg water outlet is connected to described negative electrode water-in, and described negative electrode water outlet is connected to the process water after process.
2. the cloth water structure of SPE electrolyzer according to claim 1, it is characterized in that: 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 described anode water-in, and the water side of described anode flow field groove is provided with described 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 described negative electrode water-in, and the water side of described cathode flow field groove is provided with described 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.
3. the cloth water structure of SPE electrolyzer according to claim 1 and 2, is characterized in that: pending waste water source is connected to described anode water-in, and described anode water outlet is connected to described water leg water-in;
Described water leg water outlet is divided into two-way, and a road is connected to the process water after process, and another road is connected to described negative electrode water-in; Described negative electrode water outlet is also connected to described water leg water-in.
4. the cloth water structure of SPE electrolyzer according to claim 1 and 2, it is characterized in that: pending waste water source is connected to described negative electrode water-in, described negative electrode water outlet is connected to described water leg water-in, described water leg water outlet is connected to described anode water-in, and described anode water outlet is connected to the process water after process.
5. the cloth water structure of SPE electrolyzer according to claim 1 and 2, it is characterized in that: pending waste water source is divided into two-way, one tunnel is directly connected to described water leg water-in, and another road is connected to described negative electrode water-in, and described negative electrode water outlet is connected to described water leg water-in;
Described water leg water outlet is connected to described anode water-in, and described anode water outlet is connected to the process water after process.
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| CN201420519817.5U CN204151114U (en) | 2014-09-11 | 2014-09-11 | A kind of cloth water structure of SPE electrolyzer |
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|---|---|---|---|
| CN201420519817.5U CN204151114U (en) | 2014-09-11 | 2014-09-11 | A kind of cloth water structure of SPE electrolyzer |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104211141A (en) * | 2014-09-11 | 2014-12-17 | 北京今大禹环保技术有限公司 | Water distribution structure and water distribution method of SPE (Solid Phase Extraction) electrolytic tank |
| CN105461023A (en) * | 2015-11-06 | 2016-04-06 | 北京航空航天大学 | Electrolytic tank apparatus using oxygen reduction cathode |
| CN110983367A (en) * | 2019-12-31 | 2020-04-10 | 山东东岳高分子材料有限公司 | Chlor-alkali membrane electrolytic cell containing porous conductive plate |
| CN111807573A (en) * | 2020-07-16 | 2020-10-23 | 湖南中湘春天环保科技有限公司 | Treatment device and method for thallium-containing wastewater |
-
2014
- 2014-09-11 CN CN201420519817.5U patent/CN204151114U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104211141A (en) * | 2014-09-11 | 2014-12-17 | 北京今大禹环保技术有限公司 | Water distribution structure and water distribution method of SPE (Solid Phase Extraction) electrolytic tank |
| CN105461023A (en) * | 2015-11-06 | 2016-04-06 | 北京航空航天大学 | Electrolytic tank apparatus using oxygen reduction cathode |
| CN110983367A (en) * | 2019-12-31 | 2020-04-10 | 山东东岳高分子材料有限公司 | Chlor-alkali membrane electrolytic cell containing porous conductive plate |
| CN110983367B (en) * | 2019-12-31 | 2021-05-28 | 山东东岳高分子材料有限公司 | Chlor-alkali membrane electrolytic cell containing porous conductive plate |
| CN111807573A (en) * | 2020-07-16 | 2020-10-23 | 湖南中湘春天环保科技有限公司 | Treatment device and method for thallium-containing wastewater |
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Granted publication date: 20150211 |