CN203890100U - Combined electrolytic reactor - Google Patents
Combined electrolytic reactor Download PDFInfo
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- CN203890100U CN203890100U CN201420201683.2U CN201420201683U CN203890100U CN 203890100 U CN203890100 U CN 203890100U CN 201420201683 U CN201420201683 U CN 201420201683U CN 203890100 U CN203890100 U CN 203890100U
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Abstract
The utility model discloses a combined electrolytic reactor, which belongs to the technical field of wastewater treatment. The combined electrolytic reactor comprises a reactor and a reactor base, wherein a power supply chamber, a multidimensional electrode chamber, an iron-carbon micro-electrolysis chamber, a water distribution and aeration chamber and an equipment chamber are successively arranged in the reactor from top to bottom; the power supply chamber is positioned in a top cover of the reactor and provided with two power supply controllers; the multidimensional electrode chamber is positioned below the top cover of the reactor and contains four electrode plates, i.e., successively an electrode plate a, an electrode plate b, an electrode plate d and an electrode plate c from left and right; the electrode plate a and the electrode plate d are taken as main anodes; the electrode plate b and the electrode plate c are taken as main cathodes; carbon fillers are filled among the electrode plates; the iron-carbon micro-electrolysis chamber in which iron-carbon fillers are filled is positioned at the lower part of the multidimensional electrode chamber; the water distribution and aeration chamber is positioned at the lower part of the iron-carbon micro-electrolysis chamber and respectively used for carrying out water distribution and aeration by virtue of a water distribution pump and an aeration pump which are arranged in the equipment chamber. According to the combined electrolytic reactor, the treatment efficiency is effectively improved, and the generation of passivation and hardening is reduced.
Description
Technical field
The invention belongs to environmental engineering technical field of waste water processing, specifically a kind of combination electrolysis reactor.
Background technology
Move forward steadily and rapid development of economy along with China is industrialized, water pollution problems is increasingly serious.Serious water pollutes and not only increases the weight of water resources crisis, and affects people's productive life and healthy.
Trade effluent proportion in total amount of sewage discharge is large, and intractability is high.Trade effluent can be divided into by the chemical property of contained principal pollutant: inorganic wastewater, organic wastewater with difficult degradation thereby, composite waste, heavy metal wastewater thereby, containing waste water and the water coolant of radioactive substance.Wherein, the contained hardly degraded organic substance toxicity of organic wastewater with difficult degradation thereby is large, complicated, and chemical oxygen demand is high, and general microorganism does not almost have degradation effect to it.
Electro-catalytic oxidation technology carrys out the organic pollutant in degrading waste water by the active group that produces the strong oxidizing properties such as hydroxyl radical free radical, there is non-secondary pollution, cost is low, suitability is strong, efficiency high, has application advantage processing aspect high density, bio-refractory trade effluent.In the catalytic oxidation treatment technology of high density, bio-refractory trade effluent, micro-electrolysis method is the micromolecular compound based on the organism of difficult degradation being converted into effects such as redox, flocculation, absorption, co-precipitation to easy degraded, poisonous inorganics is converted into low toxicity or nontoxic inorganics precipitation or co-precipitation to be removed, but the treatment effect of micro-electrolysis is limited, the COD of high concentration hard-degraded organic waste water is gone out to clearance only to be had 20～30% even lower.Multidimension electrode is some granular or other fragmental working electrode material of filling between conventional two-dimensional electrode, make to load working electrode material surface charging, become a new utmost point (the 3rd utmost point), in working electrode surface generation electrochemical reaction, thereby make organic matter degradation.Comparing two-dimensional electrode, to have treatment facility Area Ratio large, the advantage that mass transfer in liquid phase efficiency is high, but in the time processing high concentration hard-degraded organic waste water, still there is the not good enough problem of processing efficiency in it.The processing efficiency of multidimension electrode and structure of reactor, electrode materials and electrode face finish material (for improving the surface catalysis performance of electrode) have close relationship, also lack at present the exploitation of reactor and the electrode that matches are with it prepared and combined, and the research of multidimension electrode and microelectrolysis processing unit combination aspect.
Publication number: 2900505, the applying date: 2006-04-27, patent name: multiple dimension electrode electric catalystic, multiple dimension electrode electric catalystic, comprise parallel negative plate, the positive plate that is relatively arranged in housing, the granule electrode of filling between yin, yang pole plate, water distributor, aeration tube and power supply, described positive plate connects to form by titanium plate is alternate with carbon-point.Structure to traditional electrolytic anode is improved, by titanium plate connect to form anode alternate with carbon-point, catalytic activity and the life-span of electrode are increased, can separate out oxygen when the electrolysis as the carbon-point of anode integral part, can strengthen the direct oxidation of organic molecule on electrode and by generating the indirect oxidation effect of strong oxidic particle, improve the electrolytic catalysis processing efficiency to organic waste water.The weak point of this device is: (1) only relies on common water distributor to carry out water distribution, can impact the homogeneity of water distribution, easily causes electrolysis to stop up and uses current efficiency to reduce; (2) floor space is relatively large, can increase initial cost expense; (3) reaction chamber lacks the processing water of delay, a little less than anti impulsion load; (4) comparatively sealing in structure, lacks the dependency structure of processing granule electrode material, and it is comparatively inflexible to move; (5) only rely on the improvement of electrolytic anode structure to promote the processing efficiency of organic waste water, its effect is limited; (6) granule electrode material effects is single; (7) aspect ratio is less, and solid-liquid is relatively poor by settlement separate effect.
Summary of the invention
1. the technical problem that will solve
Relatively low for the multidimension electrode processing efficiency existing in prior art, granule electrode material effects is single, and treatment facility floor space is large, and initial cost expense is high, easily stopping up, harden and the problem of passivation in iron-carbon micro-electrolysis chamber, the invention provides a kind of combination electrolysis reactor.Adopt technical scheme of the present invention, effectively improve processing efficiency, strengthen the efficient utilization to granule electrode material, effectively reduced iron-carbon micro-electrolysis chamber and stopped up, harden and the problem such as passivation, and flexible operation, simple to operate, compact construction, easy to maintenance, small accommodation area.
2. technical scheme
For achieving the above object, technical scheme provided by the invention is:
A kind of combination electrolysis reactor, it comprises reactor and reactor base, is followed successively by from top to bottom power supply room, multidimension electrode chamber, iron-carbon micro-electrolysis chamber, water distribution aeration chamber and canyon in described reactor;
Described power supply room is positioned at reactor head, disposes two power-supply controller of electric;
Described multidimension electrode chamber is positioned at described reactor head below, comprise four plate electrode plates, from left to right be followed successively by battery lead plate a, battery lead plate b, battery lead plate d and battery lead plate c, fix by anchor, described battery lead plate a and battery lead plate d are main anode, and battery lead plate b and battery lead plate c are main cathode, and battery lead plate is rectangle, between battery lead plate, be filled with carbon filler, water outlet is positioned at carbon filler top;
Described iron-carbon micro-electrolysis chamber is positioned at bottom, multidimension electrode chamber, is filled with iron carbon filler in it;
Described water distribution aeration chamber is positioned at the bottom of iron-carbon micro-electrolysis chamber, carry out water distribution and aeration by the cloth water pump in canyon and aeration pump respectively, discharge tube is positioned at the bottom of described water distribution aeration chamber, and bottom, iron-carbon micro-electrolysis chamber adopts 5% inclined-plane inclination material pipe end.
Preferably, described multidimension electrode chamber and the aspect ratio of iron-carbon micro-electrolysis chamber are all between 5:1～8:1, and the indoor iron carbon mass ratio of iron-carbon micro-electrolysis is between 2:1～2.5:1.
Preferably, described main anode is taking iron plate as base material, and through metallic coating processing, metallic coating is one of ruthenium iridium, iridium tantalum, titanium ruthenium iridium or iron ruthenium tin, and main cathode is taking stainless steel plate as base material.
Preferably, the material of described carbon filler is one of gac, hard coal or flyash.
Preferably, described water distribution aeration chamber comprises aeration head, aeration head support, and described aeration head ring-type is evenly arranged on described aeration head support, and aeration head is connected ventilation with described aeration pump by hose nipple, rubber hose.
Preferably, described water distribution aeration chamber comprises ring-type water distributor, and described water distributor is fixed by water distributor support, and water distributor pumps into current by cloth water pump, is flowed out by aperture uniform on water distributor.
A method of wastewater treatment for combination electrolysis reactor described in adopting, described reactor adopts continuous batch periodic running mode, i.e. and operation is made up of water inlet, reaction, water outlet and standing four basic working procedure in chronological order, cycle 1.7～3.6h; Reactor water inlet adopts upflowing, and sewage passes through iron-carbon micro-electrolysis chamber and multidimension electrode chamber from bottom to top successively by the water distributor that is positioned at bottom, and the water outlet from the above of water is after treatment discharged.
Preferably, the method for wastewater treatment of described combination electrolysis reactor, the steps include:
A. before reactor operation, close the valve on discharge tube; Unload the cap lock that reactor top covers, open reactor head, and pack successively ready iron filings and carbon filler into reactor, then off-response device top cover, locks cap lock; Voltage is adjusted by power-supply controller of electric in opening power chamber, opens canyon and adjusts the flow of cloth water pump and the aeration rate of aeration pump;
B. fill phase, former water enters after the water-in of reactor bottom, is pumped into water distributor and is evenly gone out stream by aperture by cloth water pump, and flooding time is 0.2～0.3h, and flooding velocity is 30～60m
3/ h;
C. after water inlet end, enter step of reaction, open multidimension electrode and aeration pump, reduce the aeration rate of aeration pump and continue electrolysis 0.5～1.5h after 0.6～1.2h, aeration rate is 1～1.5m
3/ h;
D. after reaction finishes, enter the water outlet stage, close multidimension electrode, reduce aeration rate to 0.3～0.5m
3/ h also continues aeration 0.2～0.3h until go out stream end;
E. after water outlet finishes, enter the stage of leaving standstill, close aeration pump, after 0.2～0.3h, restart into water; Reactor operation 5～12h, opens reactor head and adds iron filings filler to supplement the iron filings of consumption.
3. beneficial effect
Adopt technical scheme provided by the invention, compared with existing known technology, there is following unusual effect:
(1) a kind of combination electrolysis reactor of the present invention, intakes as upflowing, because the quality of carbon filler is light compared with iron filings filler, therefore its under flow action, float on iron filings filler above, reduced because of the carbon filler impact that multidimension electrode is produced of running off; And carbon filler both, as the working electrode material of multidimension electrode, as the cathode material of iron-carbon micro-electrolysis reaction, had been strengthened the efficient utilization to carbon filler again;
(2) a kind of combination electrolysis reactor of the present invention, main anode is taking iron plate as base material, and process through metallic coating (metallic coating is one of ruthenium iridium, iridium tantalum, titanium ruthenium iridium or iron ruthenium tin), operating voltage is low, power consumption is little, current efficiency is high;
(3) a kind of combination electrolysis reactor of the present invention, the aspect ratio of reaction chamber (being multidimension electrode chamber and iron-carbon micro-electrolysis chamber) is between 5:1～8:1, and small accommodation area, reduced initial cost expense, and solid-liquid separation is more thorough;
(4) a kind of combination electrolysis reactor of the present invention, adopting the material of carbon filler is one of activated carbon, hard coal or flyash, all there is stronger adsorptive power, greatly improve the utilising efficiency of anodic oxygen voltinism product, reduce energy consumption, hard coal and flyash are with low cost again, can greatly reduce working cost;
(5) a kind of combination electrolysis reactor of the present invention, has increased the homogeneity of aeration by the uniform aeration head of ring-type, effectively reduced iron-carbon micro-electrolysis chamber and stopped up, harden and the problem such as passivation;
(6) a kind of combination electrolysis reactor of the present invention, combines iron-carbon micro-electrolysis and multidimension electrode structure of reactor compactness, simple to operate, easy to maintenance rationally and effectively;
(7) adopt combination electrolysis reactor of the present invention to carry out wastewater treatment, adopt continuous batch periodic running mode, have the processing water of delay in pond, anti impulsion load is strong; Each operation in technological process can be adjusted according to water quality, the water yield, flexible operation.
Brief description of the drawings
Fig. 1 is a kind of structural representation that combines electrolysis reactor of the present invention;
Fig. 2 is the A-A sectional view of Fig. 1;
Fig. 3 is the B-B sectional view of Fig. 1;
Fig. 4 is the C-C sectional view of Fig. 1.
In figure: 1, power supply room; 2, multidimension electrode chamber; 3, iron-carbon micro-electrolysis chamber; 4, water distribution aeration chamber; 5, canyon; 6, reactor head; 7, power-supply controller of electric; 8, cap lock; 9, anchor; 10, water outlet; 11, battery lead plate a; 12, battery lead plate b; 13, terminal stud; 14, battery lead plate c; 15, battery lead plate d; 16, electrode coating; 17, carbon filler; 18, iron carbon filler; 19, aeration head; 20, hose nipple; 21, aeration head support; 22, water distributor support; 23, water distributor; 24, aperture; 25, discharge tube; 26, rubber hose; 27, aeration pump; 28, water-in; 29, cloth water pump; 30, reactor; 31, reactor base.
Embodiment
Below in conjunction with Figure of description and specific embodiment, the present invention is described in detail.
Embodiment 1
As Fig. 1, the combination electrolysis reactor of the present embodiment is tubular structure, and reactor 30 is fixed on reactor base 31, the overall high 5.1m of reactor 30, and it comprises power supply room 1, multidimension electrode chamber 2, iron-carbon micro-electrolysis chamber 3, water distribution aeration chamber 4, canyon 5.
Power supply room 1 is positioned at reactor head 6, configures two power-supply controller of electric 7; The high 0.4m of reactor head 6, impressed voltage is 220V.Multidimension electrode chamber 2 is positioned at reactor head 6 bottoms, diameter is 0.4m, and height is 2.0m, comprises four plate electrode plates, (each battery lead plate upper end is provided with terminal stud 13 to be from left to right followed successively by battery lead plate a11, battery lead plate b12, battery lead plate d15 and battery lead plate c14, electrode plate surface is 60 × 60cm, and polar plate spacing is 14cm, fixing by anchor 9, anchor 9 height are 5cm, the part that battery lead plate exceeds anchor 9 is 5cm, stretches into the part of multidimension electrode chamber 2, and virtual height is 0.5m; Battery lead plate a11 and battery lead plate d15 are main anode, and battery lead plate a11 and battery lead plate c14 are main cathode, the carbon filler 17 that between battery lead plate, packing height is 1.2m, and water outlet 10 is positioned at carbon filler 17 tops; Iron-carbon micro-electrolysis chamber 3 is positioned at 2 bottoms, multidimension electrode chamber, and diameter is 0.5m, is highly 2.6m, the iron carbon filler 18 that in it, packing height is 2.4m; The part vertical height that connects the reactor wall of iron-carbon micro-electrolysis chamber 3 and multidimension electrode chamber 2 is 0.1m, with the angle of horizontal direction be 60 ° of (see figure 1).
Water distribution aeration chamber 4 is positioned at the bottom of iron-carbon micro-electrolysis chamber 3, carries out water distribution and aeration respectively by the cloth water pump 29 in canyon 5 and aeration pump 27; Discharge tube 25 is positioned at the bottom of iron-carbon micro-electrolysis chamber 3, and diameter is 100mm, and 3 bottoms, iron-carbon micro-electrolysis chamber adopt 5% inclined-plane (being the per-cent of vertical range/horizontal throw) inclination material pipe end.
As Fig. 1, water distribution aeration chamber 4 comprises aeration head 19, aeration head support 21, and aeration head 19 ring-types are evenly arranged on described aeration head support 21, and aeration head 19 is connected ventilation with described aeration pump 27 by hose nipple 20, rubber hose 26.Iron carbon mass ratio in iron-carbon micro-electrolysis chamber 3 is 2.5:1.
As Fig. 4, water distribution aeration chamber 4 also comprises ring-type water distributor 23, and water distributor 23 is fixing by water distributor support 22, and water distributor 23 pumps into current by cloth water pump 29, is flowed out by aperture uniform on water distributor 24.
Reactor adopts continuous batch periodic running mode, i.e. operation is made up of water inlet, reaction, water outlet and standing four basic working procedure in chronological order, and the cycle is 1.7～3.6h; Electrolyte stream is to vertical with the sense of current; Water inlet is upflowing, and sewage passes through iron-carbon micro-electrolysis chamber 3 and multidimension electrode chamber 2 from bottom to top successively by the water distributor 23 that is positioned at bottom, and water is after treatment discharged from water outlet 10;
As Fig. 1,2, main anode, taking iron plate as base material, through metallic coating processing, scribbles electrode coating 16 on base material, and this coating is iridium tantalum, and main cathode is taking stainless steel plate as base material; The material of carbon filler is flyash.
As Fig. 1,2,3, aeration head 19 ring-types are evenly arranged; Water distributor is ring-type, pumps into by cloth water pump 29, goes out to flow uniform water inlet by aperture 24.
The method of wastewater treatment of aforesaid combination electrolysis reactor, the steps include:
A. before reactor 30 operations, close the valve on discharge tube 25, while preventing charging, filler is missed from discharge tube 25; Unload cap lock 8, open reactor head 6 and pack successively ready iron filings and carbon filler into reactor, then off-response device top cover 6, locks cap lock 8; Voltage is adjusted by power-supply controller of electric 7 in opening power chamber 1, opens canyon 5 and adjusts the flow of cloth water pump 29 and the aeration rate of aeration pump 27, is more than into the preparation work before water.
B. fill phase, former water, after water-in 28, is pumped into water distributor 23 and is evenly gone out stream by aperture 24 by cloth water pump 29, and flooding time is 0.2h, and flooding velocity is 55.42m
3/ h, by water inlet, former water is full of whole reactor 30;
C. after water inlet end, enter step of reaction, after unlatching multidimension electrode and aeration pump 27,0.6～1.2h, reduce the aeration rate of aeration pump and continue electrolysis 0.5～1.5h, aeration rate is 1m
3/ h; By even gas distribution, increase the homogeneity of the disturbance to iron carbon filler, effectively reduce iron-carbon micro-electrolysis chamber and stopped up, harden and the problem such as passivation;
D. after reaction finishes, enter the water outlet stage, close multidimension electrode, reduce aeration rate to 0.3m
3/ h also continues aeration 0.2～0.3h until go out stream end.Reduce aeration rate, can utilize hardening of the iron carbon filler that stops on the settlement separate basis of solid-liquid;
E. after water outlet finishes, enter quiescent phase, close aeration pump 27,0.2～0.3h and restart into water;
After reactor operation for some time, open reactor head 6 and add iron carbon filler 18 to supplement the iron filings of consumption.
Embodiment 2
The one combination electrolysis reactor of the present embodiment based on above-described embodiment 1 is that example is carried out wastewater treatment, certain waste water from dyestuff, and active green KE-4BD waste water starting point concentration is 360-400mg/L, CODc
r: 275-308mg/L, pH:4.5-5.0, colourity: 1200-1500 is doubly.
Reactor main anode is taking iron plate as base material, and through metallic coating processing, metallic coating is ruthenium iridium, and main cathode is taking stainless steel plate as base material; The material of carbon filler is activated carbon.
Wastewater treatment process, step is as follows:
(1) fill phase, reactor flooding velocity is 35m
3/ h, flooding time is 0.2h;
(2) step of reaction, multidimension electrode operating voltage is 220V, current density is 30mA/cm
3, the opening time is 0.8h, and the working hour of aeration pump 27 is 2.0h, and the aeration rate of front 0.8h is 40L/min, and the aeration rate of rear 1.2h is 20L/min; In the water outlet stage, aeration rate is 5L/min, and the working hour is 0.2h;
(3) quiescent phase, aeration pump 27 is closed, and after 0.2h, restarts into water.
Continuously operation iron-free carbon bed stops up, harden, the problem appearance such as passivation.Intake continuously after 3 batches, reactor operation 5h, opens reactor head 6 and adds 0.5m
3iron carbon filler 18 is to supplement the iron filings of consumption, and then off-response device top cover 6, locks cap lock 8 and also start next round water inlet.
Starting point concentration is 360-400mg/L water outlet CODc after electrolysis
r: 34-50mg/L, doubly, COD clearance is about 88% to colourity: 30-60, and chroma removal rate is about 98%.Reach stable effluent quality to stable effluent quality and reach textile dyeing and finishing emission of industrial pollutants standard (CB4287-2012).
Embodiment 3
The one combination electrolysis reactor of the present embodiment based on above-described embodiment 1 is that example is carried out wastewater treatment, certain dyeing waste water, and water quality is CODc
r: 520-580mg/L, pH:10.5-11.0, colourity: 400-500 is doubly.
Reactor main anode is taking iron plate as base material, and through metallic coating processing, metallic coating is iron ruthenium tin, and main cathode is taking stainless steel plate as base material; The material of carbon filler is hard coal.
Wastewater treatment process, step is as follows:
(1) fill phase, reactor flooding velocity is 30m
3/ h, flooding time is 0.25h;
(2) step of reaction, multidimension electrode operating voltage is 220V, current density is 40mA/cm
3, the opening time is 1.0h, and the working hour of aeration pump 27 is 2.0h, and the aeration rate of front 1.0h is 40L/min, and the aeration rate of rear 1.0h is 20L/min; In the water outlet stage, aeration rate is 6L/min, and the working hour is 0.3h;
(3) quiescent phase, aeration pump is closed, and after duration 0.25h, restarts into water.
Continuously operation iron-free carbon bed stops up, harden, the problem appearance such as passivation.Intake continuously after 3 batches, reactor operation 12h, opens reactor head 6 and adds 0.6m
3iron carbon filler 18 is to supplement the iron filings of consumption, and then off-response device top cover 6, locks cap lock 8 and also start next round water inlet.
Water outlet CODc after electrolysis
r: 40-66mg/L, doubly, COD clearance is about 92% to colourity: 10-30, and chroma removal rate is about 96%.Reach stable effluent quality to stable effluent quality and reach textile dyeing and finishing emission of industrial pollutants standard (CB4287-2012).
Claims (5)
1. a combination electrolysis reactor, it comprises reactor (30) and reactor base (31), it is characterized in that, in described reactor (30), be followed successively by from top to bottom power supply room (1), multidimension electrode chamber (2), iron-carbon micro-electrolysis chamber (3), water distribution aeration chamber (4) and canyon (5);
Described power supply room (1) is positioned at reactor head (6), disposes two power-supply controller of electric (7);
Described multidimension electrode chamber (2) is positioned at described reactor head (6) below, comprise four plate electrode plates, from left to right be followed successively by battery lead plate a (11), battery lead plate b (12), battery lead plate d (15) and battery lead plate c (14), fixing by anchor (9), described battery lead plate a (11) and battery lead plate d (15) are main anode, battery lead plate b (12) and battery lead plate c (14) are main cathode, battery lead plate is rectangle, between battery lead plate, be filled with carbon filler (17), water outlet (10) is positioned at carbon filler (17) top,
Described iron-carbon micro-electrolysis chamber (3) is positioned at bottom, multidimension electrode chamber (2), is filled with iron carbon filler (18) in it;
Described water distribution aeration chamber (4) is positioned at the bottom of iron-carbon micro-electrolysis chamber (3), carry out water distribution and aeration by cloth water pump (29) and aeration pump (27) in canyon (5) respectively, discharge tube (25) is positioned at the bottom of described water distribution aeration chamber (4), and iron-carbon micro-electrolysis chamber (3) bottom adopts 5% inclined-plane inclination material pipe end.
2. a kind of combination electrolysis reactor according to claim 1, is characterized in that, described main anode is taking iron plate as base material, and through metallic coating processing, metallic coating is one of ruthenium iridium, iridium tantalum, titanium ruthenium iridium or iron ruthenium tin, and main cathode is taking stainless steel plate as base material.
3. a kind of combination electrolysis reactor according to claim 1, is characterized in that, the material of described carbon filler (17) is one of gac, hard coal or flyash.
4. a kind of combination electrolysis reactor according to claim 3, it is characterized in that, described water distribution aeration chamber (4) comprises aeration head (19), aeration head support (21), it is upper that described aeration head (19) ring-type is evenly arranged in described aeration head support (21), and aeration head (19) is connected ventilation with described aeration pump (27) by hose nipple (20), rubber hose (26).
5. a kind of combination electrolysis reactor according to claim 4, it is characterized in that, described water distribution aeration chamber (4) comprises ring-type water distributor (23), described water distributor (23) is fixing by water distributor support (22), water distributor (23) pumps into current by cloth water pump (29), is flowed out by aperture uniform on water distributor (24).
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103910414A (en) * | 2014-04-23 | 2014-07-09 | 中国核工业华兴建设有限公司 | Combined electrolysis reactor and waste water treatment method thereof |
| CN113642190A (en) * | 2021-08-25 | 2021-11-12 | 湖北大学 | Current design method of filling type three-dimensional electrode |
-
2014
- 2014-04-23 CN CN201420201683.2U patent/CN203890100U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103910414A (en) * | 2014-04-23 | 2014-07-09 | 中国核工业华兴建设有限公司 | Combined electrolysis reactor and waste water treatment method thereof |
| CN103910414B (en) * | 2014-04-23 | 2015-12-09 | 中国核工业华兴建设有限公司 | A kind of combination electrolysis reactor and method of wastewater treatment thereof |
| CN113642190A (en) * | 2021-08-25 | 2021-11-12 | 湖北大学 | Current design method of filling type three-dimensional electrode |
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