CN2905773Y - Air ascending circulation flow type film biological reactor - Google Patents
Air ascending circulation flow type film biological reactor Download PDFInfo
- Publication number
- CN2905773Y CN2905773Y CNU2006200419783U CN200620041978U CN2905773Y CN 2905773 Y CN2905773 Y CN 2905773Y CN U2006200419783 U CNU2006200419783 U CN U2006200419783U CN 200620041978 U CN200620041978 U CN 200620041978U CN 2905773 Y CN2905773 Y CN 2905773Y
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- Prior art keywords
- membrane
- gas lift
- membrane bioreactor
- membrane module
- cycling stream
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Separation Using Semi-Permeable Membranes (AREA)
- Activated Sludge Processes (AREA)
Abstract
A biological reactor with gas ascending circulation membranes comprises a tank body, membrane components on the tank, a segregation plate between the tank body and the membrane components on the tank and a aerator. Wherein, a descending area is formed between the tank walls and the segregation plate, a ascending area is formed between the segregation plate and the membrane components, the ascending area and the descending area are communicated, the aerator is arranged below the membrane components. The reactor has advantages of low energy consumption, convenient cleaning and maintenance, compact structure and strong ability of anti-pollution; and can be used in domestic sewage and industrial sewage treatment.
Description
Technical field
The present invention relates to membrane bioreactor, particularly gas lift cycling stream membrane bioreactor.
Background technology
Membrane bioreactor be a kind of be to combine extensively in order to handle the device of sanitary sewage or trade effluent by biochemical reactor and membrane module, this reactor combines the advantage of membrane separation technique efficiently and traditional activated sludge process.The membrane filtration of the sewage that active sludge treatment is crossed (treating water) in reactor held back materials such as suspended substance in the water and colloid, crosses directly qualified discharge or enter in the advanced treatment workshop section of next section of cleaner liquid, makes it to reach the standard of reuse water.The efficient crown_interception of film is trapped in the reactor microorganism fully simultaneously, helps long, propagation microbial growth and enrichments more slowly generation time such as nitrobacteria, has solved the sludge loss problem fully; And improved the degradation efficiency of active sludge to hardly degraded organic substance.
According to the position difference that membrane module is provided with, can be divided into separate film biological reactor and built-in membrane bioreactor two classes in membrane bioreactor.Separate film biological reactor is that membrane module and bio-reactor branch are arranged, and generally adopts recycle pump to make processing waste water and active sludge carry out on the membrane module surface flowing fast, and shearing force that is produced or turbulent flow are come decelerating membrane pollution thus.In order to keep the stable permeability rate of film, the water flow velocity on film surface is generally greater than 2m/s, thereby quantity of circulating water that need be higher, and energy consumption is higher.
And built-in membrane bioreactor is that membrane module directly is immersed in the sewage in the bio-reactor, handles the suction of waste water by pump, extracts out from film.By aeration, the mixed solution of waste water and active sludge stirs up and down with air-flow, comes decelerating membrane pollution by mixed solution at the formed reciprocating shear in film surface.But such shearing force can not stop pollutants in sewage constantly to deposit on the film surface, bacterium is constantly to the inner breeding of film, its metabolic product constantly sticks to the film surface, and then cause that very easily fenestra stops up, thereby cause the flux of film to descend, membrane lifetime shortens, and the clean and maintenance difficulty increases, and the economy of technology operation just can not embody advantage.The mode that while waste water and active sludge roll up and down with air-flow is easy to stay the dead angle in reactor, causes active sludge not to be utilized fully.Thereby the pollution that how to slow down film in the built-in bio-reactor is its key point of effectively utilizing.
Exactly because existing built-in membrane bioreactor has the film contamination resistance poor, the reactor dead angle is many, effectively do not utilize living microorganism to come many disadvantages such as organism in the degrading waste water, so when it is used in some composition complexity, when being difficult to the processing of biodegradable trade effluent, often effect is undesirable, and stopping up appears in film easily, for example the coked waste water of steelworks.
Summary of the invention
Because the above-mentioned defective of prior art, technical problem to be solved in the utility model provides that a kind of contamination resistance is strong, less energy-consumption, clean and maintenance are convenient, the built-in membrane bioreactor one gas lift cycling stream membrane bioreactor of compact construction.
For achieving the above object, gas lift cycling stream membrane bioreactor described in the utility model, comprise in casing, the described casing and be provided with membrane module, be provided with between the box body wall of described casing and the described membrane module and cut apart plate, also comprise aerator, form between the box body wall of described casing and the described division plate and fall the stream district, form the up-flow district between described division plate and the described membrane module, described top and the bottom that falls stream district and described up-flow district communicates, and described aerator is arranged on the below of membrane module.
Preferably, described division plate is vertical with described bottom half.
Preferably, distolateral (a) of described division plate and (b) be close to the box body wall of described casing.
Preferably, described casing is rectangular parallelepiped or right cylinder.
Preferably, described division plate is two rectangular clapboards.
Preferably, described division plate is two rectangular clapboards that be arranged in parallel.
Preferably, the top of described division plate and bottom grow the top and the bottom of membrane module respectively.
Preferably, described membrane module is positioned at the three-dimensional regional centre that described division plate and described box body wall surrounds.
Preferably, described aerator be arranged on membrane module under.
Preferably, described aerator is a micro-hole aerator.
Preferably, the shared same pipeline of water inlet pipe of filtering rising pipe of described membrane module and film cleaning.
Preferably, the film in the described membrane module adopts ultra-filtration membrane or microfiltration membrane.
The principle of work of the utility model gas lift cycling stream membrane bioreactor:
(1) in the sewage disposal: the biochemical reactor air supply source is from the aerator of film bottom, make whole box body form the up-flow district behind system's air feed and flow the district with falling, pending waste water enters from the top that the stream district falls in described casing, rapidly and the active sludge thorough mixing in the casing, enter the up-flow district from the bottom that falls the stream district, after mixed solution enters the up-flow district, under gas drives in the up-flow district fast rise, and enter from the top in up-flow district and to fall the stream district, mixed solution circulates repeatedly falling stream district and up-flow district under the drive of gas like this, circulates the shearing force that is produced and has slowed down the film pollution greatly; While circulates repeatedly gas, pending waste water and active sludge is mixed fully, has improved the transfer efficiency of oxygen in the mixed solution, and then has improved the utilization ratio of oxygen; Strengthened the contact probability of waste water and active sludge, the utilization ratio of living microorganism is also improved greatly; Thereby the solubility in the sewage, hardly degraded organic substance are fully degraded by microorganism, have improved effluent quality.
(2) the processed back of sewage: after biochemical reaction was fully finished, treating water was filtered discharge by the suction of pump through film.
Described active sludge can be this area active sludge commonly used, for example contains the active sludge of various colloids, floss and microorganism (overwhelming majority is various bacteriums).
Native system adopts the filtration of certain hour (30-60min) and the back flushing of certain hour (30-60s) to move continuously, and back flushing can be adopted filtered water, pure water or certain density film to pollute sustained release dosage and enter membrane module from the wash tube of membrane module and clean.Described film pollutes the film pollution sustained release dosage that sustained release dosage can be this area routine.
As required, membrane bioreactor of the present utility model can carry out series combination, for example can adopt the series connection of two-stage membrane bioreactor to use, the water outlet of first membrane bioreactor enters in second membrane bioreactor and further handles, to improve the quality of final outflow water.Also the sewage treatment equipment of bio-reactor of the present utility model with routine can be used in combination, so that use the utility model membrane bioreactor flexibly effectively.
Compared with prior art, the utlity model has following advantage:
1, the mixed solution of pending waste water and active sludge composition, under the aeration of certain intensity, described membrane bioreactor stream district falls and the up-flow district circulates repeatedly, waste water is able to fully contact mixing with active sludge, in mixed solution, contain under the situation of active sludge of big concentration the pollution that not only slows down film effectively; And waste water is contacted fully with active sludge, strengthened the degradation efficiency of active sludge greatly.
2, because the intravital division plate of case plays the local enhanced effect of aeration effect, and gas-liquid-solid three phase flow increases at the flow velocity on film surface, shearing force strengthens, and has slowed down the film pollution greatly.
3, the mixed solution of pending waste water and active sludge composition circulates repeatedly falling between stream district and the up-flow district of described membrane bioreactor, under same aeration tolerance, the effect of division plate has in addition improved the transfer efficiency of oxygen in reactor, thereby has increased the utilization ratio of oxygen.Therefore under same aerobic condition, can reduce the aeration rate of reactor, reduce the technology cost.
4, the shared pipeline of the water inlet pipe of filtering rising pipe and backwashing water in the membrane module, the back flushing of the filtration of certain hour (30-60min) and certain hour (30-60s) is regularly switched, and clean and maintenance is convenient, has saved the space, has reduced the technology cost.
Description of drawings
Be described further below with reference to the technique effect of accompanying drawing, to understand the purpose of this utility model, feature and effect fully design of the present utility model, concrete structure and generation.Wherein:
Fig. 1 is the front view of the utility model embodiment;
Fig. 2 is the cross sectional plan view of Fig. 1 along the A-A line.
Embodiment
As depicted in figs. 1 and 2 be one preferred embodiment of the utility model gas lift cycling stream membrane bioreactor, comprise casing 1, be provided with membrane module 2 in the described rectangular parallelepiped casing 1, two rectangle division plates 3 that be arranged in parallel between the box body wall of described casing 1 and the described membrane module 2, form between described box body wall and the described division plate 3 and fall stream district 5, form up-flow district 6 between described division plate 3 and the described membrane module 2, described top and the bottom that falls stream district 5 and described up-flow district 6 communicates; Also comprise micro-hole aerator 4.
As shown in Figure 1, the top of described division plate 3 and bottom grow the top and the bottom of membrane module 2 respectively; Distolateral (a) of described division plate 3 and (b) be close to the box body wall of described casing 1; As depicted in figs. 1 and 2, described membrane module 2 is positioned at the centre in box body wall surrounded the three-dimensional zone of described division plate 3 and described casing 1, like this so that mixed solution in the up-flow district 6 and fall the preferable fluid effect of stream district 5 formation.
Described division plate 3 and described casing 1 bottom vertical.Division plate 3 plays the local effect that strengthens the aeration effect more effectively in up-flow district 6, the three-phase mixed solution is increased at the film surface velocity, and shearing force strengthens, and has slowed down the film pollution greatly.
In the present embodiment, described aerator 4 be arranged on membrane module 2 under; For the shearing force that the gas-liquid-solid three-phase mixed solution is circulated produced acts on the surface of film as much as possible, the more effective effect of decelerating membrane pollution improves the contamination resistance of the film in the reactor.
In the present embodiment, described aerator 4 adopts the micro-pore aeration bodies, also can adopt the aerator of this area routine, and rotary mixing type aerator for example as long as gas-liquid-solid three-phase can be mixed fully, and can circulate effectively and gets final product.
In the present embodiment, casing 1 also can adopt other shape, as cylindrical, circulates as long as be convenient to gas-liquid-solid three-phase, reduces the dead angle in circulating, handled easily person's operation simultaneously or with being connected of another reactor or the conventional sewage disposal device in this area.
In the utility model, division plate 3 also can adopt other shape, as right cylinder, circulates as long as be convenient to gas-liquid-solid three-phase, can play the local enhanced effect of tolerance simultaneously and get final product.
In the present embodiment, water inlet pipe 7 shared same pipelines when rising pipe 7 when membrane module 2 filters and film back flushing, the manufacturing cost of further saving reactor.
In the present embodiment, the film in the described membrane module 2 is a microfiltration membrane, and described microfiltration membrane adopts the microfiltration membrane of smaller aperture due; Film in the membrane module 2 described in the utility model also can adopt ultra-filtration membrane, and described ultra-filtration membrane can adopt the ultra-filtration membrane of big molecular weight cut-off.
Described microfiltration membrane or the raw material that ultra-filtration membrane adopted are resistant to pollution mould materials, can be polyolefins, polyether sulfone and inclined to one side tetrafluoroethylene etc.
Chemical oxygen demand (COD) (COD) is 1500mg/L, ammonia nitrogen (NH
3-N) be 150mg/L, volatile phenol is 30mg/L, colourity (extension rate) is 250, suspended solids (SS) is the coked waste water of the steelworks of 100mg/L, enter the casing 1 that useful volume is 160L from the top that falls stream district 5 of described gas lift cycling stream membrane bioreactor, activated sludge concentration in the described casing 1 is 10000-15000mg/L, and the aeration rate of aerator 4 is 0.6-1.4m
3/ h, the temperature of mixed solution remains on 25-35 ℃ in the casing 1.Enter the up-flow district 6 of casing 1 like this behind waste water and the mud thorough mixing by the passage of division plate 3 bottoms, mixed solution under the drive of gas in the up-flow district of casing 16 fast rise, and by the extremely described stream district 5 that falls of overhead stream, mixed solution just circulates repeatedly falling between stream district 5 and the up-flow district 6 like this, and waste water progressively is degraded by microorganisms in this process.
Handle the suction filtration of waste water, discharge from the rising pipe 7 of micro-filtration membrane module 2 through pump.Active sludge then continues to stay described casing 1 and circulates.After testing, the content of COD is below 100mg/L in the filtered water, and ammonia-nitrogen content is below 5mg/L, and volatile phenol does not detect, and SS does not detect, and colourity at 60-120 doubly.Find out significantly from above data: filter water outlet and can enter next step advanced treatment, and COD, ammonia nitrogen, phenol have reached national industrial discharge secondary standard.
The potassium bichromate degestion is adopted in the detection of COD in the above-mentioned filtered water; The mensuration of ammonia nitrogen adopts the nessler reagent spectrophotometry; The detection method of volatile phenol adopts distillation back 4-aminoantipyrene spectrophotometry; Colourity adopts the extension rate method; Weighting method is adopted in the detection of suspended solids.
Simultaneity factor adopts the operation method of 30 minutes filter 23s back flushing in 0 second.During back flushing, will filter water outlet, pure water or film pollution sustained release dosage and squeeze into the membrane module 2 by pump, carry out the 30s back flushing from water inlet pipe 7.
Gas lift cycling stream membrane bioreactor of the present utility model is 10500mg/L at activated sludge concentration, and aeration rate is 1.0m
3Under/the h, the transmembrane pressure (TMP) in a filtration cycle (30-60min) of the film in the described membrane module 2 has only increased 0.020-0.100Kpa, and through after the 30s back flushing, TMP can return to its initial level rapidly.After filtration moved 120 days continuously repeatedly with back flushing, TMP had only increased 0.05-0.63Kpa.
This specification sheets is described to be preferred embodiment of the present utility model.In every case those skilled in the art of the present technique comply with change or the modification that design of the present utility model is made, and all should drop in the utility model claim protection domain.
Claims (12)
1, a kind of gas lift cycling stream membrane bioreactor, comprise in casing, the described casing and be provided with membrane module, be provided with between the box body wall of described casing and the described membrane module and cut apart plate, also comprise aerator, it is characterized in that, form between the box body wall of described casing and the described division plate and fall the stream district, form the up-flow district between described division plate and the described membrane module, described top and the bottom that falls stream district and described up-flow district communicates, and described aerator is arranged on the below of membrane module.
2, a kind of gas lift cycling stream membrane bioreactor as claimed in claim 1 is characterized in that described division plate is vertical with described bottom half.
3, a kind of gas lift cycling stream membrane bioreactor as claimed in claim 1 is characterized in that, distolateral (a) of described division plate and (b) be close to the box body wall of described casing.
4, a kind of gas lift cycling stream membrane bioreactor as claimed in claim 1 is characterized in that described casing is rectangular parallelepiped or right cylinder.
5, a kind of gas lift cycling stream membrane bioreactor as claimed in claim 1 is characterized in that, described division plate is two rectangular clapboards.
6, a kind of gas lift cycling stream membrane bioreactor as claimed in claim 1 is characterized in that, described division plate is two rectangular clapboards that be arranged in parallel.
7, a kind of gas lift cycling stream membrane bioreactor as claimed in claim 1 is characterized in that the top of described division plate and bottom grow the top and the bottom of membrane module respectively.
8, a kind of gas lift cycling stream membrane bioreactor as claimed in claim 1 is characterized in that, described membrane module is positioned at the three-dimensional regional centre that described division plate and described box body wall surrounds.
9, a kind of gas lift cycling stream membrane bioreactor as claimed in claim 1 is characterized in that, described aerator be arranged on membrane module under.
10, a kind of gas lift cycling stream membrane bioreactor as claimed in claim 1 is characterized in that described aerator is a micro-hole aerator.
11, a kind of gas lift cycling stream membrane bioreactor as claimed in claim 1 is characterized in that, the shared same pipeline of water inlet pipe that filtering rising pipe of described membrane module and film clean.
As the arbitrary described a kind of gas lift cycling stream membrane bioreactor of claim 1～11, it is characterized in that 12, the film in the described membrane module adopts ultra-filtration membrane or microfiltration membrane.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2006200419783U CN2905773Y (en) | 2006-05-22 | 2006-05-22 | Air ascending circulation flow type film biological reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2006200419783U CN2905773Y (en) | 2006-05-22 | 2006-05-22 | Air ascending circulation flow type film biological reactor |
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| Publication Number | Publication Date |
|---|---|
| CN2905773Y true CN2905773Y (en) | 2007-05-30 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNU2006200419783U Expired - Lifetime CN2905773Y (en) | 2006-05-22 | 2006-05-22 | Air ascending circulation flow type film biological reactor |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102786188A (en) * | 2012-08-29 | 2012-11-21 | 哈尔滨工业大学 | Forward osmosis membrane bioreactor with magnetic nanoparticles serving as driving liquid |
| CN107986436A (en) * | 2017-12-29 | 2018-05-04 | 清华大学 | A kind of biology membrane-membrane biological coupling sewage-treatment plant |
| CN111439849A (en) * | 2020-05-19 | 2020-07-24 | 西安建筑科技大学 | Plate frame immersed dynamic membrane bioreactor |
| CN114735832A (en) * | 2022-06-15 | 2022-07-12 | 清研环境科技股份有限公司 | Modular sewage treatment system, treatment method and application thereof |
-
2006
- 2006-05-22 CN CNU2006200419783U patent/CN2905773Y/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102786188A (en) * | 2012-08-29 | 2012-11-21 | 哈尔滨工业大学 | Forward osmosis membrane bioreactor with magnetic nanoparticles serving as driving liquid |
| CN102786188B (en) * | 2012-08-29 | 2013-10-30 | 哈尔滨工业大学 | Forward osmosis membrane bioreactor with magnetic nanoparticles serving as driving liquid |
| CN107986436A (en) * | 2017-12-29 | 2018-05-04 | 清华大学 | A kind of biology membrane-membrane biological coupling sewage-treatment plant |
| CN107986436B (en) * | 2017-12-29 | 2024-02-06 | 清华大学 | Biological membrane-membrane biological coupling sewage treatment device |
| CN111439849A (en) * | 2020-05-19 | 2020-07-24 | 西安建筑科技大学 | Plate frame immersed dynamic membrane bioreactor |
| CN114735832A (en) * | 2022-06-15 | 2022-07-12 | 清研环境科技股份有限公司 | Modular sewage treatment system, treatment method and application thereof |
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| CX01 | Expiry of patent term |
Granted publication date: 20070530 |
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| EXPY | Termination of patent right or utility model |