CN204737787U - Electrochemistry - biological fluidized bed reactor - Google Patents
Electrochemistry - biological fluidized bed reactor Download PDFInfo
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- CN204737787U CN204737787U CN201520312293.7U CN201520312293U CN204737787U CN 204737787 U CN204737787 U CN 204737787U CN 201520312293 U CN201520312293 U CN 201520312293U CN 204737787 U CN204737787 U CN 204737787U
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Abstract
The utility model discloses an electrochemistry - biological fluidized bed reactor, including the anaerobism fluidized bed oxygen fluidized bed of becoming reconciled, the anaerobism fluidized bed is become reconciled the lower part of oxygen fluidized bed and is passed through the first electrode group link, and the anaerobism fluidized bed is become reconciled the upper portion of oxygen fluidized bed and is passed through the second electrode group link, the anaerobism fluidized bed is equipped with first water inlet and first delivery port, and good oxygen fluidized bed is equipped with second water inlet and second delivery port, is connected through sewer line between first delivery port and the second water inlet, the bottom of good oxygen fluidized bed is equipped with the aeration head. Its method for wastewater treatment is that the temperature that keeps the anaerobism fluidized bed to become reconciled in the oxygen fluidized bed is 18-38 DEG C, add the electrolyte in organic waste water after, send into the anaerobism fluidized bed in proper order and become reconciled the oxygen fluidized bed and handle. The utility model discloses introduce biodegradable in the electrochemical system of conventionality, reach the redox of electrochemistry and biodegradable coupling, accelerate the processing speed greatly, improve rich nitrogen organic waste water's treatment effect.
Description
Technical field
The utility model relates to technical field for the treatment of of organic waste, particularly a kind of electrochemistry-biological fluidized-bed reactor.
Background technology
Coking chemical waste water contains in the waste water of bio-refractory organic pollutant with other, its outstanding feature is that nitrogen content is high, hardly degraded organic substance is many, because its composition complexity, Stability Analysis of Structures, toxicity are comparatively strong and biodegradability is poor, conventional sewage water treatment method is difficult to cause effect, thus bring very large pollution to environment, become the technical barrier that environment-protective water process field is paid close attention to for many years and will be solved.
In traditional sewage water treatment method, biochemical process effectively can remove organism, stink in waste water, reduce chroma in waste water, and on engineer applied technical maturity, running cost is low, and convenient management is simple and easy, but the degradation speed of biochemical process to the poisonous and harmful Recalcitrant chemicals of complicated component is slow, decompose thorough, even due to poisoning and lose processing power.
And as a kind of conventional physical chemistry treatment process, electrochemical process is by electrochemical combustion or electrochemical conversion, there is redox reaction with the pollutent in waste water by obtaining or lose electronics quickly and efficiently, hardly degraded organic substance being transformed and is degraded into carbonic acid gas and water or better simply organism.Rapidly, processing power is strong and conversion unit is simple, processing ease in electrochemical techniques development, is easy to control.Compared with biochemical process, electrochemical method, can as high toxicity, the organic effective treating method of highly corrosive generally not by the impact of reactant bio-toxicity.But when adopting electrochemical process oxidation or reduction organism, there is multiple side reaction (as heat production, liberation of hydrogen, analyse oxygen, analyse chlorine etc.) in reaction process, current efficiency is lower, and therefore process energy consumption comparatively large, working cost is higher.
Electro-biometric coupling technique not only combines the feature that biochemical process processing cost is low, electrochemical process process difficult degradation toxic pollutant is effective, and can the side reaction that current efficiency be caused in electrochemical reaction to reduce (as heat production, analysing oxygen, liberation of hydrogen, electromigration etc.) be effectively utilized in biological respinse, therefore in the aspect of whole coupling technique, make current efficiency and treatment effect significantly improve, reduce processing cost simultaneously.1992, people (the Mellor R B such as R.B Me11or, Ronnenberg J, Campbell W H, et al.Reduction of nitrate and nitrite in water by immobilized enzymes [J] .Nature, 1992,355 (20): 717-719.) on Nature magazine, reported first utilizes biofilm-electrode to carry out denitrifying research, denitrification enzyme and dyestuff (electron transit mediator) are fixed on cathode surface, the H that denitrification enzyme utilizes brine electrolysis to produce by them
2by NO
3 -be reduced to N
2, and achieve good denitrification effect.The people such as YSakakibara (Y Sakakibara, M Kuroda.Electric prompting and control ofdenitrification [J] .Biotech.Bioeng.1993,42:535-537.) negative electrode and anode are placed in respectively the denitrifying bacteria of the fixing biofilm of reactor research that two are connected to NO
3 -processing power, result shows, when electric current is 0mA, separates out without nitrogen; When electric current is increased to 40mA from 10mA, nitrogen output increases by 4 times.But because electrode surface microbial film specific surface area is less in biofilm-electrode process, microbial film such as easily to come off at the reason, and denitrification efficiency improves limited efficiency, makes the method for biofilm-electrode intensive treatment hardly degraded organic substance less in actual applications.
Therefore, at present in the urgent need to optimizing the design of electrochemical reactor, the mass transfer of the hydroxyl free basal orientation solution main body that anode surface produces is strengthened.
Utility model content
The purpose of this utility model is to overcome the deficiencies in the prior art, for rich nitrogen organic waste water, a kind of electrochemistry-biological fluidized-bed reactor is provided, this reactor structure based on fluidized-bed, biological degradation is introduced in the electrochemical system of routine, reach the redoxomorphism of electrochemistry and biological degradation coupling, speed up processing greatly, improves the treatment effect of rich nitrogen organic waste water.
The technical solution of the utility model is: a kind of electrochemistry-biological fluidized-bed reactor, comprise be connected anaerobic fluidized bed and aerobic fluidized bed, connected by the first electrode group between anaerobic fluidized bed bottom and aerobic fluidized bed bottom, connected by the second electrode group between anaerobic fluidized bed top and aerobic fluidized bed top; Anaerobic fluidized bed bottom is provided with the first water-in, anaerobic fluidized bed top is provided with the first water outlet, aerobic fluidized bed bottom is provided with the second water-in, and aerobic fluidized bed top is provided with the second water outlet, is connected between the first water outlet with the second water-in by sewer line; Aerobic fluidized bed bottom is provided with aeration head.
Described anaerobic fluidized bed with aerobic fluidized bed structure is identical, comprise inner core and urceolus respectively, inner core is the cylindrical structure opened up and down, and inner core is located in urceolus, and communicate with bottom urceolus bottom inner core, form annular space between the outer wall of inner core and the inwall of urceolus; The bottom of inner core is reaction zone; The top of urceolus is inverted cone-shaped structure, and form mud-water separation district, mud-water separation is provided with porous plate in district, and porous plate arranges carbon leaching material, and the outer tube inner wall be positioned at above carbon leaching material is provided with overflow weir.
Described anaerobic fluidized bed in, overflow weir place communicates with the first water outlet; In aerobic fluidized bed, overflow weir communicates with the second water outlet.
Described first electrode group comprises graphite cathode, graphite anode and direct supply, and graphite cathode is located in the inner core of anaerobic fluidized bed bottom, and graphite anode is located in the inner core of aerobic fluidized bed bottom, is connected between graphite cathode and graphite anode by direct supply;
Second electrode group comprises two Graphite Electrodess, respectively arranges a Graphite Electrodes, connected between two Graphite Electrodess by wire in anaerobic fluidized bed mud-water separation district and in aerobic fluidized bed mud-water separation district.
In described first electrode group, graphite cathode and graphite anode measure-alike, length is 200mm, and cross-sectional diameter is 20mm;
In second electrode group, two Graphite Electrodess measure-alike, length is 50mm, and cross-sectional diameter is 5mm.
Described anaerobic fluidized bed top is also provided with the first heating rod, and aerobic fluidized bed top is also provided with the second heating rod, and the first heating rod is connected with AC power respectively with the second heating rod.
Described anaerobic fluidized bed in be also provided with recirculation assembly, recirculation assembly comprises recycle pump and recirculated water valve, anaerobic fluidized bed bottom is provided with circulating water intake, the entrance end of recycle pump is connected with anaerobic fluidized bed top by circulating water pipeline, the exit end of recycle pump is connected with circulating water intake by circulating water pipeline, and circulating water intake place arranges recirculated water valve.The setting of recirculation assembly, interiorly repeatedly can to process organic waste water anaerobic fluidized bed, improve the treatment effect of organic waste water.Recirculated water, through carbon leaching material filter obtain muddy water, the first water inlet organic waste water, three fully mixes in anaerobic fluidized bed bottom, more gradually rise carry out electrochemical reaction.
Described aerobic fluidized bed bottom is aeration mixing zone, and aeration head is located in aeration mixing zone, and aeration head is by the external blower fan of gas pipeline, and gas pipeline is provided with gas meter; Aerobic fluidized bed bottom is also provided with mud valve.In this structure, provide pressurized air by external blower fan, by aeration head send into aerobic fluidized bed in, gas meter is for measuring and regulating the operational throughput of air.
Described anaerobic fluidized bed in, the first water-in is by the external former tank of the first peristaltic pump, and the first water inlet is provided with the first water intaking valve, and the exit end of the first peristaltic pump is provided with the first rotor under meter; Former tank for storing original organic waste water, organic waste water send into anaerobic fluidized bed before, in former tank, add ionogen and mix, the first rotor under meter is for monitoring and regulating the flooding quantity of organic waste water.
In aerobic fluidized bed, second water inlet is provided with the second water intaking valve, and the second water outlet picks out tank, and the bottom of effluent trough is provided with outlet valve, the top of effluent trough is connected with the first anaerobic fluidized bed water-in by the second peristaltic pump, and the exit end of the second peristaltic pump is provided with the second spinner-type flowmeter.Effluent trough is mainly used in storing the waste water obtained after treatment, adds the second peristaltic pump and the second spinner-type flowmeter, when waste water is not up to standard after treatment, can be reintroduced back to anaerobic fluidized bed, carries out secondary treatment by the waste water in effluent trough.
By the method for wastewater treatment that above-mentioned electrochemistry-biological fluidized-bed reactor realizes, comprise the following steps:
(1) respectively at anaerobic fluidized bed and aerobic fluidized bed middle filling carbon leaching material, and keep anaerobic fluidized bed and aerobic fluidized bed in temperature be 18 ~ 38 DEG C;
(2) in organic waste water, add ionogen, and adjust ph is 7.0 ~ 7.5;
(3) organic waste water is sent into anaerobic fluidized bed in, there is electrochemistry and biodegradable concerted reaction in the process that organic waste water rises in anaerobic fluidized bed inner core simultaneously; When organic waste water rises to anaerobic fluidized bed mud-water separation district, carry out biological degradation and realize mud-water separation;
(4) organic waste water obtained from anaerobic fluidized bed separation is sent into aerobic fluidized bed, and electrochemistry and biodegradable concerted reaction occur the process that organic waste water rises in aerobic fluidized bed inner core simultaneously; When organic waste water rises to aerobic fluidized bed mud-water separation district, carry out biological degradation and realize mud-water separation, purifying waste water of resulting separation is directly discharged by the second water outlet.
In above-mentioned treating processes, carry out at the electrochemistry-biological treatment of organic waste water remains on 18 ~ 38 DEG C, the ionogen adopted is one or more of copper sulfate or ferrous sulfate, aerobic fluidized bed middle dissolved oxygen concentration (DO) more than 1.5mg/L, the flow velocity of the first water-in and the second water-in all controls as about 1.0L/min, and the galvanic current of the first electrode group is 5 ~ 20mA.
When this electrochemistry-biological fluidized-bed reactor and method of wastewater treatment thereof use, concrete principle is as follows:
Treatment of Organic Wastewater mechanism is mainly electrochemical oxidation, biological degradation and synergy thereof.Electrode under suitable electrical potential conditions, negative electrode and anodic reaction as follows:
Negative electrode with the electrolytic hydrogen production of proton reduction and water, or by Cu
2+, Fe
2+become the Cu with reducing power
+, Cu and Fe, be specially:
2H
2O+2e＝H
2+2OH
-(e
0＝0.000V)
Cu
2++e＝Cu
+(e
0＝0.153V)
Cu
2++2e＝Cu (e
0＝0.337V)
Cu
++e＝Cu (e
0＝0.521V)
Fe
2++2e＝Fe (e
0＝-0.440V)
Electrode reaction on anode has:
C+2H
2O＝CO
2+4H
++4e (e
0＝0.207V)
2H
2O＝O
2+4H
++2e (e
0＝1.229V)
According to the electropotential of each reaction, at negative electrode to produce Cu, separately there is Cu
+and H
2, and anode should to produce CO
2be main, therefore by the redox reaction of electrolytic process, negative electrode provide hydrogen, Cu
+utilize as electron donor direct oxidation organism or supply denitrifying bacterium with Cu etc., anode provides CO
2as the nutrition source that biological respinse is nitrated.
The utility model, relative to prior art, has following beneficial effect:
(1) negative electrode is separated with anode, be installed on respectively anaerobic fluidized bed and aerobic fluidized bed in.NH
4 +removal depend on aerobe process, need with O
2nO is converted into Deng as electron acceptor(EA) generation oxidizing reaction
2 -or NO
3 -, and NO
2 -, NO
3 -in anaerobic fluidized bed, can realize Synergistic degradation or removal by denitrification with organic removal, in addition, organism can also oxidative degradation in aerobic fluidized bed bioprocess.The utility model have employed negative electrode and positive electrode be separated reactive system, negative electrode be mainly present in anaerobic fluidized bed in, and anode be mainly present in aerobic fluidized bed in.First, being separated of negative electrode and anode reduces produced redox mediator and reacts to each other and the energy wastage caused; Secondly, anaerobic fluidized bed middle NO is decreased
2 -and NO
3 -the movement of anode and aerobic fluidized bed middle NH
4 +to the movement of negative electrode, thus add reactant and the direct contact probability of respective electrode.
(2) with fluidized-bed structure mass transfer enhancement process, electrochemical reaction efficiency is improved.Under gac fluidized state, effect of mass transmitting is strengthened, and makes the transmission speed of electronics between medium in electrochemical process faster, is conducive to carrying out fast of redox reaction, thus efficiently removes pollutent.
(3) with Cu
2+and Fe
2+supplementing as electron transit mediator.In bioprocesses, enzyme serves vital effect as catalyzer, and wherein has the active centre of a lot of enzyme all to comprise metal ion, and modal is Cu and Fe, and therefore, it is necessary that appropriate Cu and Fe exists biological respinse.In addition, Cu
2+comparatively H
+be easier to accept electronics at negative electrode and produce the Cu with reducing power
+and Cu, and Fe
2+although the difficulty obtaining electronics on negative electrode is larger, the Fe of generation has and compares H
2higher reducing power.Therefore Cu
2+interpolation can accelerate electron transmission and improve the speed of pollutant removal, and Fe
2+the more stable pollutent of interpolation removeability matter.
(4) electrochemistry and biological respinse are worked in coordination with, in utilization compared with the rapidly and efficiently removal realizing nitrogen and organic pollutant when less energy-consumption.Electrochemical process can produce the oxidation and reducing substance with higher-energy, and the enzyme in bioprocesses is the most efficient catalyzer of current contaminant degradation, both coupling reactions are higher with pure biological respinse phase specific efficiency, and compared with electrochemical reaction, required energy consumption is less.
Accompanying drawing explanation
Fig. 1 is the principle schematic of this electrochemistry-biological fluidized-bed reactor.
Embodiment
Below in conjunction with embodiment, the utility model is described in further detail, but embodiment of the present utility model is not limited thereto.
Embodiment
A kind of electrochemistry-biological fluidized-bed reactor of the present embodiment, as shown in Figure 1, comprise anaerobic fluidized bed 1 and aerobic fluidized bed 2 that are connected, connected by the first electrode group between anaerobic fluidized bed bottom and aerobic fluidized bed bottom, connected by the second electrode group between anaerobic fluidized bed top and aerobic fluidized bed top; Anaerobic fluidized bed bottom is provided with the first water-in, anaerobic fluidized bed top is provided with the first water outlet, aerobic fluidized bed bottom is provided with the second water-in, and aerobic fluidized bed top is provided with the second water outlet, is connected between the first water outlet with the second water-in by sewer line; Aerobic fluidized bed bottom is provided with aeration head 3.
As shown in Figure 1, anaerobic fluidized bed with aerobic fluidized bed structure is identical, comprises inner core 4 and urceolus 5 respectively, inner core is the cylindrical structure opened up and down, inner core is located in urceolus, and communicates with bottom urceolus bottom inner core, forms annular space between the outer wall of inner core and the inwall of urceolus; The bottom of inner core is reaction zone; The top of urceolus is inverted cone-shaped structure, and form mud-water separation district, be provided with porous plate 6 in mud-water separation district, porous plate arranged carbon leaching material 7, the outer tube inner wall be positioned at above carbon leaching material is provided with overflow weir 8.In the present embodiment, adopt anaerobic fluidized bed and aerobic fluidized bed concrete structure parameter as follows: the side length b=100mm of reaction zone; Height H=the 600mm of reaction zone; Aspect ratio H/d=6.0; The volume V of reaction zone
1=7.5L (volume containing bottom cone); The volume V in mud-water separation district
2=4.0L; Diameter d=the 70mm of inner core.
In anaerobic fluidized bed, overflow weir place communicates with the first water outlet; In aerobic fluidized bed, overflow weir communicates with the second water outlet.
First electrode group comprises graphite cathode 9, graphite anode 10 and direct supply 11, and graphite cathode is located in the inner core of anaerobic fluidized bed bottom, and graphite anode is located in the inner core of aerobic fluidized bed bottom, is connected between graphite cathode and graphite anode by direct supply;
Second electrode group comprises two Graphite Electrodess 12, respectively arranges a Graphite Electrodes, connected between two Graphite Electrodess by wire in anaerobic fluidized bed mud-water separation district and in aerobic fluidized bed mud-water separation district.
In first electrode group, graphite cathode and graphite anode measure-alike, length is 200mm, and cross-sectional diameter is 20mm;
In second electrode group, two Graphite Electrodess measure-alike, length is 50mm, and cross-sectional diameter is 5mm.
Anaerobic fluidized bed top is also provided with the first heating rod 13, and aerobic fluidized bed top is also provided with the second heating rod 14, first heating rod and is connected with AC power 15 respectively with the second heating rod.
Also recirculation assembly is provided with in anaerobic fluidized bed, recirculation assembly comprises recycle pump 16 and recirculated water valve 17, anaerobic fluidized bed bottom is provided with circulating water intake, the entrance end of recycle pump is connected with anaerobic fluidized bed top by circulating water pipeline, the exit end of recycle pump is connected with circulating water intake by circulating water pipeline, and circulating water intake place arranges recirculated water valve.The setting of recirculation assembly, interiorly repeatedly can to process organic waste water anaerobic fluidized bed, improve the treatment effect of organic waste water.Recirculated water, through carbon leaching material filter obtain muddy water, the first water inlet organic waste water, three fully mixes in anaerobic fluidized bed bottom, more gradually rise carry out electrochemical reaction.
Aerobic fluidized bed bottom (i.e. reaction zone place) is aeration mixing zone, and aeration head is located in aeration mixing zone, and aeration head is by the external blower fan 18 of gas pipeline, and gas pipeline is provided with gas meter 19; Aerobic fluidized bed bottom is also provided with mud valve 20.In this structure, provide pressurized air by external blower fan, by aeration head send into aerobic fluidized bed in, gas meter is for measuring and regulating the operational throughput of air.
In anaerobic fluidized bed, the exit end that the first water-in is provided with the first water intaking valve 23, first peristaltic pump by the first external former tank 22, first water inlet of peristaltic pump 21 is provided with the first rotor under meter 24; Former tank for storing original organic waste water, organic waste water send into anaerobic fluidized bed before, in former tank, add ionogen and mix, the first rotor under meter is for monitoring and regulating the flooding quantity of organic waste water.
In aerobic fluidized bed, second water inlet is provided with the second water intaking valve 25, second water outlet picks out tank 26, the bottom of effluent trough is provided with outlet valve 27, the top of effluent trough is connected with the first anaerobic fluidized bed water-in by the second peristaltic pump 28, and the exit end of the second peristaltic pump is provided with the second spinner-type flowmeter 29.Effluent trough is mainly used in storing the waste water obtained after treatment, adds the second peristaltic pump and the second spinner-type flowmeter, when waste water is not up to standard after treatment, can be reintroduced back to anaerobic fluidized bed, carries out secondary treatment by the waste water in effluent trough.
By the method for wastewater treatment that above-mentioned electrochemistry-biological fluidized-bed reactor realizes, comprise the following steps:
(1) respectively at anaerobic fluidized bed and aerobic fluidized bed middle filling carbon leaching material, and keep anaerobic fluidized bed and aerobic fluidized bed in temperature be 18 ~ 38 DEG C;
(2) in organic waste water, add ionogen, and adjust ph is 7.0 ~ 7.5;
(3) organic waste water is sent into anaerobic fluidized bed in, there is electrochemistry and biodegradable concerted reaction in the process that organic waste water rises in anaerobic fluidized bed inner core simultaneously; When organic waste water rises to anaerobic fluidized bed mud-water separation district, carry out biological degradation and realize mud-water separation;
(4) organic waste water obtained from anaerobic fluidized bed separation is sent into aerobic fluidized bed, and electrochemistry and biodegradable concerted reaction occur the process that organic waste water rises in aerobic fluidized bed inner core simultaneously; When organic waste water rises to aerobic fluidized bed mud-water separation district, carry out biological degradation and realize mud-water separation, purifying waste water of resulting separation is directly discharged by the second water outlet.
In the present embodiment, organic waste water adopts homemade simulation coking chemical waste water, adopts following component to prepare: (NH
4)
2sO
450g, NaHCO
3100g, NaCl 20g, K
2hPO
4h
2o 4.35g, Na
2hPO
4h
2o6.68g, KH
2pO
49.74g, FeCl
30.435mg, CaCl
20.728mg, MgSO
41mg, MnSO
40.798mg, ZnSO
4h
2o 0.826mg, methyl alcohol 12g, phenol 4.75g, quinoline 1g, pyrene 0.1g, be dissolved in 50L tap water, and natural pH is 7.3 ~ 7.5.
In simulation coking chemical waste water, the index of every pollutent is: COD 652.76mg/L, NH
4 +-N 200mg/L, phenol 95mg/L, quinoline 20mg/L, pyrene 2mg/L.
When using above-mentioned electrochemistry-biological fluidized-bed reactor to process, with the flow velocity of 1.04L/min, the hydraulic detention time (HRT) controlling reaction zone in each fluidized-bed is 7.2h continuum micromeehanics, and in reactor, total HRT of (containing disengaging zone) is 23.1h.With the aerobic fluidized bed middle DO of blower fan aeration control at more than 1.5mg/L, aerobic fluidized bed water outlet is back to anaerobic fluidized bed with 1.5:1 ratio.Aerobic fluidized bed and anaerobic fluidized bed middle sludge concentration all controls as 4.0gMLSS/L, and strength of current is respectively 0mA, 5mA, 10mA, 20mA.
Test shows, electrochemically strengthening effect significantly can strengthen the denitrification of bioprocess, at 22 DEG C, does not add Cu
2+and Fe
2+when as electron transit mediator, the electric current of 10mA can make denitrification efficiency bring up to more than 49% from 24%; Add Cu
2+during as electron transit mediator, denitrification efficiency brings up to more than 90% further.Hardly degraded organic substance remove mainly occur in anaerobic fluidized bed in, the organic carbon source as anti-nitration reaction is utilized by denitrifying bacteria.Electrochemica biological fluidised bed system is utilized to achieve the efficient Synergistic degradation of hardly degraded organic substance and nitrogen, the electric current of 10mA and add Cu
2+as electron transit mediator, total HRT controls at 23.1h, can realize Denitrification rate and reach 90%, and total nitrogen is removed and reached more than 60%, organic removal rate more than 90%.After this system process, the ammonia nitrogen concentration of water outlet is less than 1mg/L, and COD is less than 80mg/L, and various hardly degraded organic substance concentration is all lower than detectability.
As mentioned above, just can realize the utility model preferably, above-described embodiment is only preferred embodiment of the present utility model, is not used for limiting practical range of the present utility model; Namely all equalizations done according to the utility model content change and modify, all by the utility model claim scope required for protection is contained.
Claims (9)
1. electrochemistry-biological fluidized-bed reactor, it is characterized in that, comprise be connected anaerobic fluidized bed and aerobic fluidized bed, connected by the first electrode group between anaerobic fluidized bed bottom and aerobic fluidized bed bottom, connected by the second electrode group between anaerobic fluidized bed top and aerobic fluidized bed top; Anaerobic fluidized bed bottom is provided with the first water-in, anaerobic fluidized bed top is provided with the first water outlet, aerobic fluidized bed bottom is provided with the second water-in, and aerobic fluidized bed top is provided with the second water outlet, is connected between the first water outlet with the second water-in by sewer line; Aerobic fluidized bed bottom is provided with aeration head.
2. a kind of electrochemistry-biological fluidized-bed reactor according to claim 1, it is characterized in that, described anaerobic fluidized bed with aerobic fluidized bed structure is identical, comprise inner core and urceolus respectively, inner core is the cylindrical structure opened up and down, inner core is located in urceolus, and communicates with bottom urceolus bottom inner core, forms annular space between the outer wall of inner core and the inwall of urceolus; The bottom of inner core is reaction zone; The top of urceolus is inverted cone-shaped structure, and form mud-water separation district, mud-water separation is provided with porous plate in district, and porous plate arranges carbon leaching material, and the outer tube inner wall be positioned at above carbon leaching material is provided with overflow weir.
3. a kind of electrochemistry-biological fluidized-bed reactor according to claim 2, is characterized in that, described anaerobic fluidized bed in, overflow weir place communicates with the first water outlet; In aerobic fluidized bed, overflow weir communicates with the second water outlet.
4. a kind of electrochemistry-biological fluidized-bed reactor according to claim 2, it is characterized in that, described first electrode group comprises graphite cathode, graphite anode and direct supply, graphite cathode is located in the inner core of anaerobic fluidized bed bottom, graphite anode is located in the inner core of aerobic fluidized bed bottom, is connected between graphite cathode and graphite anode by direct supply;
Second electrode group comprises two Graphite Electrodess, respectively arranges a Graphite Electrodes, connected between two Graphite Electrodess by wire in anaerobic fluidized bed mud-water separation district and in aerobic fluidized bed mud-water separation district.
5. a kind of electrochemistry-biological fluidized-bed reactor according to claim 4, is characterized in that, in described first electrode group, and graphite cathode and graphite anode measure-alike, length is 200mm, and cross-sectional diameter is 20mm;
In second electrode group, two Graphite Electrodess measure-alike, length is 50mm, and cross-sectional diameter is 5mm.
6. a kind of electrochemistry-biological fluidized-bed reactor according to claim 1, it is characterized in that, described anaerobic fluidized bed top is also provided with the first heating rod, and aerobic fluidized bed top is also provided with the second heating rod, and the first heating rod is connected with AC power respectively with the second heating rod.
7. a kind of electrochemistry-biological fluidized-bed reactor according to claim 1, it is characterized in that, described anaerobic fluidized bed in be also provided with recirculation assembly, recirculation assembly comprises recycle pump and recirculated water valve, anaerobic fluidized bed bottom is provided with circulating water intake, the entrance end of recycle pump is connected with anaerobic fluidized bed top by circulating water pipeline, and the exit end of recycle pump is connected with circulating water intake by circulating water pipeline, and circulating water intake place arranges recirculated water valve.
8. a kind of electrochemistry-biological fluidized-bed reactor according to claim 1, it is characterized in that, described aerobic fluidized bed bottom is aeration mixing zone, and aeration head is located in aeration mixing zone, aeration head is by the external blower fan of gas pipeline, and gas pipeline is provided with gas meter; Aerobic fluidized bed bottom is also provided with mud valve.
9. a kind of electrochemistry-biological fluidized-bed reactor according to claim 1, it is characterized in that, described anaerobic fluidized bed in, the first water-in is by the external former tank of the first peristaltic pump, first water inlet is provided with the first water intaking valve, and the exit end of the first peristaltic pump is provided with the first rotor under meter;
In aerobic fluidized bed, second water inlet is provided with the second water intaking valve, and the second water outlet picks out tank, and the bottom of effluent trough is provided with outlet valve, the top of effluent trough is connected with the first anaerobic fluidized bed water-in by the second peristaltic pump, and the exit end of the second peristaltic pump is provided with the second spinner-type flowmeter.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104860397A (en) * | 2015-05-14 | 2015-08-26 | 华南理工大学 | Electrochemical-biological fluidized bed reactor and wastewater treatment method |
| CN110382682A (en) * | 2017-01-18 | 2019-10-25 | 挪威东南大学 | For handling wet organic substance to generate the device and method of biogas |
-
2015
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104860397A (en) * | 2015-05-14 | 2015-08-26 | 华南理工大学 | Electrochemical-biological fluidized bed reactor and wastewater treatment method |
| CN110382682A (en) * | 2017-01-18 | 2019-10-25 | 挪威东南大学 | For handling wet organic substance to generate the device and method of biogas |
| CN110382682B (en) * | 2017-01-18 | 2023-05-05 | 挪威东南大学 | Apparatus and method for treating wet organic matter to produce biogas |
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