CN204281406U - A kind of membrane bioreactor based on fouling membrane in-situ control - Google Patents
A kind of membrane bioreactor based on fouling membrane in-situ control Download PDFInfo
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- CN204281406U CN204281406U CN201420738968.XU CN201420738968U CN204281406U CN 204281406 U CN204281406 U CN 204281406U CN 201420738968 U CN201420738968 U CN 201420738968U CN 204281406 U CN204281406 U CN 204281406U
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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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Abstract
The utility model provides a kind of membrane bioreactor based on fouling membrane in-situ control, comprise reaction tank, membrane module, top flow deflector, sidepiece flow deflector and aerating apparatus is provided with in described reaction tank, wherein, described top flow deflector is arranged on described membrane module, described sidepiece flow deflector is arranged on the outside of described membrane module, described aerating apparatus is arranged under described membrane module, be provided with the diversion outlet supplying water and flow out between described top flow deflector, sidepiece flow deflector, between described sidepiece flow deflector, aerating apparatus, be provided with the directed fluid inlet supplying water and flow into.The beneficial effects of the utility model are: by top flow deflector, sidepiece flow deflector and aerating apparatus formed in reaction tank center to upper reaches, the defluent circulating water flow of sidepiece, center flows through membrane module to the current at upper reaches, can the reversible membrane fouling on effective controlling diaphragm surface.
Description
Technical field
The utility model relates to sewage disposal, particularly relates to a kind of membrane bioreactor based on fouling membrane in-situ control in sewage disposal.
Background technology
Biological treatment combines with membrane sepn by membrane bioreactor, realizes the separating controlling of hydraulic detention time and sludge age, can greatly improve microbial biomass in reactor, is conducive to the growth of specific function bacterium and the removal of pollutent.There is floor space little, stable effluent quality, easily realize the advantages such as control automatically, increasing in the application in water and wastewater treatment field.Film is as the core of membrane bioreactor, and residing for it, environment is very severe.Owing to there is the suspended substance of high density, organism and microorganism and mucilage secretion in bio-reactor, cause the irreversible membrane fouling ubiquity of film, had a strong impact on the application of membrane bioreactor.Therefore, how while strengthening pollutant removal, controlling diaphragm pollutes the critical bottleneck becoming membrane bioreactor development.
For the treatment effect of reinforced film biological reactor and controlling diaphragm pollute, the method adding filler can be adopted to increase microbial biomass, the pollution layer on the filler of fluidized also film surface capable of washing, reduces fouling membrane.Domestic relevant main patent has: waste water treating apparatus with circulating membrane bioreactor and method of wastewater treatment (Authorization Notice No. CN 100429160C), remove pollutent mainly through the engineering bacteria on fixing filler or zymin, utilize film to carry out solid-liquid separation simultaneously; A kind ofly study membrane bioreactor system that filler improves fouling membrane and quantize testing method and application (Authorization Notice No. CN 102642920B), mainly through three groups of membrane bioreactors run parallel to evaluate the impact of different floating stuffing on fouling membrane, for design new packing provides basis; Add fluidized bed type film-bioreactor and the water treatment method (Authorization Notice No. CN 1164507C) of filler, by guiding device, reaction tank is divided into up-flow district and Jiang Liu district, membrane module is placed in up-flow district, by aeration, filler is flowed, controlling diaphragm pollutes, intensifying treatment effect; Mixed liquor characteristics regulate and control method (publication number CN 1600705A) in a kind of membrane bioreactor that controlling diaphragm pollutes, makes the change of mixed liquor characteristics in reactor thus controlling diaphragm pollutes mainly through adding ozone; The novel method (publication number CN 102276055A) of fouling membrane in a kind of controlling diaphragm bio-reactor, by adding filler as biomembranous carrier in reactor, optimize aeration mode and control microbial metabolism, thus decelerating membrane pollution, a kind of flat ceramic ultrafiltration membrane bioreactor (publication number CN 103304021A), by utilizing ceramic membrane and fixing FSB bio-carrier, conventional membrane bioreactor is transformed, make microorganism flco be attached to biologic packing material surface, effectively alleviate fouling membrane.
Based on above-mentioned discussion, the problem existing for visible existing method and apparatus is: 1) aeration and the filler added only can slow down the reversible membrane fouling on film surface, and helpless to the pollution in fenestra; 2) the film major part adopted is the organic membrane of low mechanical strength, cannot stand the scraping of hard filler, and the aeration of atm number also can cause the jitter amplitude of film to increase, and accelerates the aging of film and damages; 3) reactor is without sludge settling and sludge drainage system; 4) PPCPs in water cannot be removed and some has the industrial micropollutant of endocrine.
Summary of the invention
In order to solve the problems of the prior art, the utility model provides a kind of membrane bioreactor based on fouling membrane in-situ control.
The utility model provides a kind of membrane bioreactor based on fouling membrane in-situ control, comprise reaction tank, membrane module, top flow deflector, sidepiece flow deflector and aerating apparatus is provided with in described reaction tank, wherein, described top flow deflector is arranged on described membrane module, described sidepiece flow deflector is arranged on the outside of described membrane module, described aerating apparatus is arranged under described membrane module, be provided with the diversion outlet supplying water and flow out between described top flow deflector, sidepiece flow deflector, between described sidepiece flow deflector, aerating apparatus, be provided with the directed fluid inlet supplying water and flow into.
As further improvement of the utility model, dividing plate is provided with in described reaction tank, described dividing plate is arranged along the horizontal plane, described reaction tank is separated into reaction zone and buffer zone by described dividing plate, described reaction zone is positioned on described dividing plate, described buffer zone is positioned under described dividing plate, and described membrane module, top flow deflector, sidepiece flow deflector and aerating apparatus are all arranged in described reaction zone.
As further improvement of the utility model, the bottom of described reaction tank is provided with mud district, and described mud district is positioned under described buffer zone, and the delivery port in described mud district is provided with mud valve.
As further improvement of the utility model, described sidepiece flow deflector is around the sidepiece guide shell of the circumference formation upper and lower opening of described membrane module, and the bottom of described sidepiece guide shell is provided with expansion mouth, and described aerating apparatus is arranged in described expansion mouth.
As further improvement of the utility model, described top flow deflector is coniform, and the summit of described top flow deflector is near described membrane module, and the bottom surface of described top flow deflector is near the top of described reaction tank.
As further improvement of the utility model, described reaction tank is connected with water feed apparatus, and described membrane module is connected with discharging device, and the water-in of described water feed apparatus is arranged between the sidewall of described reaction tank, sidepiece flow deflector.
As further improvement of the utility model, described water feed apparatus comprises water inlet pipe, and described water inlet pipe is connected with coagulant dosage device.
As further improvement of the utility model, described discharging device is connected with the top of described membrane module, the micro-pore aeration rod that described aerating apparatus comprises source of oxygen, the ozonizer be connected with described source of oxygen and is connected with described ozonizer, described micro-pore aeration rod is arranged under described membrane module.
As further improvement of the utility model, described coagulant dosage device comprises coagulating agent hold-up vessel, store with described coagulating agent tank connected coagulant dosage pump and be connected with described coagulant dosage pump add pipe, described in add pipe and be connected with described water inlet pipe.
As further improvement of the utility model, be filled with suspension type filler in described reaction tank, described aerating apparatus is the aerating apparatus of ozone, pure oxygen mixing.
The utility model additionally provides a kind of technique based on fouling membrane in-situ control, comprises the following steps:
S1, membrane module is arranged on below the flow deflector of top, the inner side of sidepiece flow deflector, above aerating apparatus, aeration is carried out by aerating apparatus, make current direction upper reaches, and through membrane module, by sidepiece flow deflector by the water water conservancy diversion to upper reaches inside sidepiece flow deflector, be to dirty by top flow deflector by the water water conservancy diversion to upper reaches, by top flow deflector, sidepiece flow deflector by defluent water water conservancy diversion outside sidepiece flow deflector, the center that formed in reaction tank to upper reaches, the defluent circulating water flow of sidepiece;
S2, to dosing coagulant in reaction tank.
As further improvement of the utility model, step S1 also comprises: by horizontally disposed dividing plate, reaction tank is divided into reaction zone, buffer zone, and reaction zone is positioned on dividing plate, and buffer zone is positioned under dividing plate, under buffer zone, arrange mud district, described circulating water flow is positioned at reaction zone; Step S2 is: form coagulation water to water feed apparatus dosing coagulant, between being injected into by this coagulation water outside reaction tank sidewall, sidepiece flow deflector, the water inlet direction of this coagulation water is vertically downward.
The beneficial effects of the utility model are: pass through such scheme, by top flow deflector, sidepiece flow deflector and aerating apparatus formed in reaction tank center to upper reaches, the defluent circulating water flow of sidepiece, center flows through membrane module to the current at upper reaches, can the reversible membrane fouling on effective controlling diaphragm surface.
Accompanying drawing explanation
Fig. 1 is the structural representation of a kind of membrane bioreactor based on fouling membrane in-situ control of the utility model;
Fig. 2 is the sectional view A-A of Fig. 1;
Fig. 3 is the sectional view B-B of Fig. 1.
Embodiment
To illustrate below in conjunction with accompanying drawing and embodiment further illustrates the utility model.
Drawing reference numeral in Fig. 1 to Fig. 3 is: reaction tank 1; Top flow deflector 11; Sidepiece flow deflector 12; Filler 13; Water inlet pipe 14; Dividing plate 15; Mud valve 16; Coagulant dosage pump 2; Coagulating agent hold-up vessel 21; Add pipe 22; Ozonizer 3; Micro-pore aeration rod 31; Source of oxygen 32; Membrane module 4; Water outlet suction pump 41; Rising pipe 42;
For solving current membrane bioreactor Problems existing, the utility model provide a kind of can the membrane bioreactor of in-situ control fouling membrane and technique, by to water inlet dosing coagulant, suspension type filler is placed in membrane bioreactor, use ozone/pure oxygen aeration, under the effect of special-shaped flow deflector, realize the in-situ control of film surface and fenestra internal contamination, utilize ozone/pure oxygen to strengthen the removal effect of emerging pollutent simultaneously.
As shown in Figure 1 to Figure 3, a kind of membrane bioreactor based on fouling membrane in-situ control, comprise reaction tank 1, membrane module 4 is provided with in described reaction tank 1, top flow deflector 11, sidepiece flow deflector 12 and aerating apparatus, wherein, described top flow deflector 11 is vertically arranged on described membrane module 4, described sidepiece flow deflector 12 is arranged on the outside of described membrane module 4, described aerating apparatus is arranged under described membrane module 4, described top flow deflector 11, the diversion outlet supplying water and flow out is provided with between sidepiece flow deflector 12, described sidepiece flow deflector 12, the directed fluid inlet supplying water and flow into is provided with between aerating apparatus.
As shown in Figure 1 to Figure 3, filler 13 is provided with in described reaction tank 1, described filler 13 is preferably suspension type filler, in reaction tank, preferably fill half suspension type filler, the diameter of described half suspension filler needs to match with the gap of diversion outlet, directed fluid inlet, adjacent membranes assembly 4, and described filler 13 is made for sludge proof flexibility or rigidity material.
As shown in Figure 1 to Figure 3, described aerating apparatus is preferably the aerating apparatus of ozone, pure oxygen mixing.
As shown in Figure 1 to Figure 3, described membrane module 4 is preferably the ceramic film component of resistance to oxidation, high mechanical strength.
As shown in Figure 1 to Figure 3, dividing plate 15 is provided with in described reaction tank 1, described dividing plate 15 is preferably porous barrier, described dividing plate 15 is arranged along the horizontal plane, described reaction tank 1 is separated into reaction zone and buffer zone by described dividing plate 15, described reaction zone is positioned on described dividing plate 15, and described buffer zone is positioned under described dividing plate 15, and described membrane module 4, top flow deflector 11, sidepiece flow deflector 12 and aerating apparatus are all arranged in described reaction zone.
As shown in Figure 1 to Figure 3, the bottom of described reaction tank is provided with mud district, and described mud district is positioned under described buffer zone, and the delivery port in described mud district is provided with mud valve 16.
As shown in Figure 1 to Figure 3, reaction zone and mud distinguish by the dividing plate 15 in reaction tank 1, partial sludge flco can enter the mud district under grid under mass force does use, and filler 13 is still retained in reaction zone, filler 13 also can make biofilm detachment aging on filler 13 enter mud district with the collision of dividing plate 15, maintain biomembranous high reactivity, the mud in mud district is got rid of by mud valve 16, the hydraulic detention time 0.5-1h of reaction tank 1.
As shown in Figure 1 to Figure 3, described sidepiece flow deflector 11 is around the sidepiece guide shell of the circumference formation upper and lower opening of described membrane module 4, and the bottom of described sidepiece guide shell is provided with expansion mouth, and described expansion mouth is similar horn-like, and described aerating apparatus is arranged in described expansion mouth.
As shown in Figure 1 to Figure 3, described top flow deflector 11 is coniform, and the summit of described top flow deflector 11 is near described membrane module 4, and the bottom surface of described top flow deflector 11 is near the top of described reaction tank 1.
As shown in Figure 1 to Figure 3, described reaction tank 1 is connected with water feed apparatus, and described membrane module 4 is connected with discharging device, and the water-in of described water feed apparatus is arranged between the sidewall of described reaction tank 1, sidepiece flow deflector 12.
As shown in Figure 1 to Figure 3, described water feed apparatus comprises water inlet pipe 14, and described water inlet pipe 14 is connected with coagulant dosage device.
As shown in Figure 1 to Figure 3, described coagulant dosage device comprise coagulating agent hold-up vessel 21, the coagulant dosage pump 2 be connected with described coagulating agent hold-up vessel 21 and be connected with described coagulant dosage pump 2 add pipe 22, coagulating agent directly enters water inlet pipe 14 by adding pipe 22, in water inlet pipe 14 He in reaction tank 1, complete coagulation process.
As shown in Figure 1 to Figure 3, described discharging device is connected with the top of described membrane module 4.
As shown in Figure 1 to Figure 3, described discharging device comprises the water outlet suction pump 41 be connected with the top of described membrane module 4 and the described rising pipe 42 be connected with water outlet suction pump 41, water outlet suction pump 41 can provide the suction pressure of-80kPa and the lift of 200kPa pressure, and water outlet suction pump 41 can simultaneously as producing water pump and backwashing pump use.
As shown in Figure 1 to Figure 3, the micro-pore aeration rod 31 that described aerating apparatus comprises source of oxygen 32, the ozonizer 3 be connected with described source of oxygen 32 and is connected with described ozonizer 3, described micro-pore aeration rod 31 is arranged under described membrane module 4, source of oxygen 32 can provide pressure to be the dry pure oxygen of 40-100kPa, can produce ozone, the pure oxygen mixed gas of ozone concn at 30-100mg/L after ozonizer 3, ozone can be distributed in bottom reaction tank 1 by micro-pore aeration rod 31 uniformly.
As shown in Figure 1 to Figure 3, a kind of technique based on fouling membrane in-situ control, comprises the following steps:
S1, membrane module 4 is arranged on below top flow deflector 11, the inner side of sidepiece flow deflector 12, above aerating apparatus, aeration is carried out by aerating apparatus, make current direction upper reaches, and through membrane module 4, by sidepiece flow deflector 12 by the water water conservancy diversion to upper reaches in the inner side of sidepiece flow deflector 12, be to dirty by top flow deflector 11 by the water water conservancy diversion to upper reaches, by top flow deflector 11, sidepiece flow deflector 12 by defluent water water conservancy diversion in the outside of sidepiece flow deflector 12, in reaction tank 1 formation center to upper reaches, the defluent circulating water flow of sidepiece;
S2, to dosing coagulant in reaction tank 1.
As shown in Figure 1 to Figure 3, step S1 also comprises: by horizontally disposed dividing plate 15, reaction tank 1 is divided into reaction zone, buffer zone, reaction zone is positioned on dividing plate, and buffer zone is positioned under dividing plate, under buffer zone, arrange mud district, described circulating water flow is positioned at reaction zone; Step S2 is: form coagulation water to water feed apparatus dosing coagulant, and between the outside this coagulation water being injected into the sidewall of reaction tank 1, sidepiece flow deflector 12, the water inlet direction of this coagulation water is vertically downward.
A kind of membrane bioreactor based on fouling membrane in-situ control that the utility model provides and technique thereof have the following advantages:
1, the coagulation water after dosing coagulant directly enters reaction tank 1, tiny flocculation process is realized in reaction tank 1, membrane filtration can retain the particulate matter in most coagulation water, and certain density flco can be formed in reaction tank 1, flco can stay longer, itself be exactly a kind of " filler ", the microorganism be attached on flco can be degraded to pollutent;
2, membrane module 4 filters and carries out ozone to the coagulation water in reaction tank 1 simultaneously, pure oxygen aeration, gas drives water body and filler 13 to run, at top flow deflector 11, formation center is formed in reaction tank 1 to upper reaches under the acting in conjunction of sidepiece flow deflector 12, the defluent circulating water flow of sidepiece, complete coagulation process, filler 13 for set state microorganism carrier is provided while can reduce the reversible membrane fouling resistance on film surface, the oxidable Organic substance in water of ozone, remove colourity and stink, and the Organic pollutants in the hole of controlled membrane module 4, therefore, the double effects of pollutant removal and controlling diaphragm pollution can be realized,
3, by ozone, pure oxygen aeration, the ozone amount added is 1-5mg/L, and the dissolved oxygen concentration of reaction zone can maintain about 10-15mg/L; Under the centrifugation of dividing plate 15, filler 13 is positioned at the reaction zone of reaction tank 1 all the time; Under mass force and action of gravity, part flco forms mud by dividing plate 15 in mud district, reduces the spoil disposal water yield, improves producing water ratio.
A kind of membrane bioreactor based on fouling membrane in-situ control that the utility model provides, need through the microorganism culturing of certain hour before commencement of commercial operation, and incubation time is depending on envrionment temperature and condition of water quality.
One of key issue that the utility model solves is: how effectively controlling diaphragm pollutes.Its principle is: 1) aeration makes filler 13 in fluidized, filler 13 and current have higher frictional force and shearing force respectively, in conjunction with the adjustment in filler 13 diameter and adjacent membranes assembly 4 gap, flco and filler 13, can the reversible membrane foulings on effective controlling diaphragm surface under circulating water flow drives; 2) ozone decomposable asymmetric choice net larger molecular organics, increase organic wetting ability, be conducive to the degraded of membrane cisterna internal contamination thing on the one hand, solubilised state ozone can enter fenestra on the one hand, react with the organism in membrane module 4 hole, thus the irreversible Organic pollutants of physics in masking hole, extend the matting cycle of film; 3) reaction tank 1 is provided with buffer zone and mud district, is conducive to controlling the flco concentration in reaction zone, avoids flco concentration in reaction process continue to increase and increase the weight of the pollution of film.
Compared with prior art, remarkable advantage of the present utility model is that the flco that filler 13 and coagulating agent are formed all can be used as microorganism carrier, and the specific surface area of flco is far above filler, add microbial biomass, ozone, pure oxygen aeration process have higher oxygen partial pressure than traditional air aeration simultaneously, improve the mass-transfer efficiency of oxygen.The high mass transfer efficiency of high-biomass and oxygen ensure that the degradation rate of pollutent, improves the organism volumetric loading of reactor.
When utilizing the utility model process micro-polluted raw or low-concentration organic waste water, tool has the following advantages: after 1) adopting coagulation process, finite concentration flco is formed in reaction tank 1, flco and filler 13 can simultaneously for microorganism growth provide carrier, be conducive to the microorganism of length generation time as the breeding of nitrobacteria, the pollutent of all right absorbed portion water inlet of flco, flco and filler 13, under circulating water flow drives, reduce the pollutant load of membrane module 4; 2) adopt ozone, pure oxygen aeration, make filler 13 be in fluidized and can distinguish irreversible Organic pollutants of physics in the reversible membrane fouling of controlling diaphragm assembly 4 and membrane module 4 hole, realize the in-situ control of fouling membrane; 3) ozone decomposable asymmetric choice net is unfavorable for the larger molecular organics of microbial decomposition, strengthens organic removal effect; 4) use of ozone, pure oxygen aeration accelerates the mass transfer of oxygen, reduces energy consumption; 5) reaction tank 1 subregion is reaction zone, buffer zone, mud district, and sludge concentration in reaction zone can be made unlikely too high and increase the weight of fouling membrane.
Two experiments are below provided, further illustrate the utility model.
Experiment 1
Test the utility model is to the control effects of fouling membrane, and be 400L/h at aeration rate, ozone dosage is 2mg/L, and membrane flux is 100L/m
2h, processes micro-polluted raw under the operating mode of hydraulic detention time 0.5h, and does not add ozone and compares with the membrane bioreactor of filler, and the matting cycle of film can extend to 20 days by 7 days.
Experiment 2
Test the utility model is to the removal effect of organism, ammonia nitrogen, PPCPs and Taste and odor compounds, and be 400L/h at aeration rate, ozone dosage is 2mg/L, and membrane flux is 100L/m
2h, under the operating mode of hydraulic detention time 0.5h, the dissolved oxygen in reaction tank 1 water can be increased to 15-20mg/L by 4mg/L, and the clearance of PPCPs and Taste and odor compounds is more than 95%, organic clearance is about 50%, can reach 3-4mg/L and without the accumulation of nitrite to the absolute removal amount of ammonia nitrogen.
Above content is in conjunction with concrete preferred implementation further detailed description of the utility model, can not assert that concrete enforcement of the present utility model is confined to these explanations.For the utility model person of an ordinary skill in the technical field, without departing from the concept of the premise utility, some simple deduction or replace can also be made, all should be considered as belonging to protection domain of the present utility model.
Claims (10)
1. the membrane bioreactor based on fouling membrane in-situ control, it is characterized in that: comprise reaction tank, membrane module, top flow deflector, sidepiece flow deflector and aerating apparatus is provided with in described reaction tank, wherein, described top flow deflector is arranged on described membrane module, described sidepiece flow deflector is arranged on the outside of described membrane module, described aerating apparatus is arranged under described membrane module, be provided with the diversion outlet supplying water and flow out between described top flow deflector, sidepiece flow deflector, between described sidepiece flow deflector, aerating apparatus, be provided with the directed fluid inlet supplying water and flow into.
2. the membrane bioreactor based on fouling membrane in-situ control according to claim 1, it is characterized in that: in described reaction tank, be provided with dividing plate, described dividing plate is arranged along the horizontal plane, described reaction tank is separated into reaction zone and buffer zone by described dividing plate, described reaction zone is positioned on described dividing plate, described buffer zone is positioned under described dividing plate, and described membrane module, top flow deflector, sidepiece flow deflector and aerating apparatus are all arranged in described reaction zone.
3. the membrane bioreactor based on fouling membrane in-situ control according to claim 2, is characterized in that: the bottom of described reaction tank is provided with mud district, and described mud district is positioned under described buffer zone, and the delivery port in described mud district is provided with mud valve.
4. the membrane bioreactor based on fouling membrane in-situ control according to claim 1, it is characterized in that: described sidepiece flow deflector is around the sidepiece guide shell of the circumference formation upper and lower opening of described membrane module, the bottom of described sidepiece guide shell is provided with expansion mouth, and described aerating apparatus is arranged in described expansion mouth.
5. the membrane bioreactor based on fouling membrane in-situ control according to claim 1, it is characterized in that: described top flow deflector is coniform, the summit of described top flow deflector is near described membrane module, and the bottom surface of described top flow deflector is near the top of described reaction tank.
6. the membrane bioreactor based on fouling membrane in-situ control according to claim 1, it is characterized in that: described reaction tank is connected with water feed apparatus, described membrane module is connected with discharging device, and the water-in of described water feed apparatus is arranged between the sidewall of described reaction tank, sidepiece flow deflector.
7. the membrane bioreactor based on fouling membrane in-situ control according to claim 6, it is characterized in that: described discharging device is connected with the top of described membrane module, the micro-pore aeration rod that described aerating apparatus comprises source of oxygen, the ozonizer be connected with described source of oxygen and is connected with described ozonizer, described micro-pore aeration rod is arranged under described membrane module.
8. the membrane bioreactor based on fouling membrane in-situ control according to claim 6, it is characterized in that: described water feed apparatus comprises water inlet pipe, described water inlet pipe is connected with coagulant dosage device.
9. the membrane bioreactor based on fouling membrane in-situ control according to claim 8, it is characterized in that: described coagulant dosage device comprises coagulating agent hold-up vessel, store with described coagulating agent tank connected coagulant dosage pump and be connected with described coagulant dosage pump add pipe, described in add pipe and be connected with described water inlet pipe.
10. the membrane bioreactor based on fouling membrane in-situ control according to claim 1, is characterized in that: be filled with suspension type filler in described reaction tank, and described aerating apparatus is the aerating apparatus of ozone, pure oxygen mixing.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104445600A (en) * | 2014-11-28 | 2015-03-25 | 深圳中清环境科技有限公司 | Membrane pollution in-situ control based membrane bioreactor and technology thereof |
| CN112387118A (en) * | 2019-08-19 | 2021-02-23 | 北京奥博水处理有限责任公司 | Online self-cleaning ceramic membrane filter |
| CN114506965A (en) * | 2020-11-17 | 2022-05-17 | 湖南盛世丰花生物科技有限公司 | Three-phase biological fluidized bed for treating high-concentration organic wastewater |
-
2014
- 2014-11-28 CN CN201420738968.XU patent/CN204281406U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104445600A (en) * | 2014-11-28 | 2015-03-25 | 深圳中清环境科技有限公司 | Membrane pollution in-situ control based membrane bioreactor and technology thereof |
| CN112387118A (en) * | 2019-08-19 | 2021-02-23 | 北京奥博水处理有限责任公司 | Online self-cleaning ceramic membrane filter |
| CN114506965A (en) * | 2020-11-17 | 2022-05-17 | 湖南盛世丰花生物科技有限公司 | Three-phase biological fluidized bed for treating high-concentration organic wastewater |
| CN114506965B (en) * | 2020-11-17 | 2023-12-19 | 湖南盛世丰花生物科技股份有限公司 | Three-phase biological fluidized bed for treating high-concentration organic wastewater |
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| GR01 | Patent grant |