CN102863075A - External membrane bioreactor with self-suction jet nozzle aerating function - Google Patents
External membrane bioreactor with self-suction jet nozzle aerating function Download PDFInfo
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- CN102863075A CN102863075A CN2011101887146A CN201110188714A CN102863075A CN 102863075 A CN102863075 A CN 102863075A CN 2011101887146 A CN2011101887146 A CN 2011101887146A CN 201110188714 A CN201110188714 A CN 201110188714A CN 102863075 A CN102863075 A CN 102863075A
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- 239000012528 membrane Substances 0.000 title claims abstract description 67
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 40
- 238000005273 aeration Methods 0.000 claims abstract description 31
- 239000012530 fluid Substances 0.000 claims description 35
- 238000005842 biochemical reaction Methods 0.000 claims description 22
- 239000010802 sludge Substances 0.000 claims description 18
- 238000005406 washing Methods 0.000 claims description 8
- 239000010865 sewage Substances 0.000 claims description 7
- 238000010992 reflux Methods 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 18
- 230000008569 process Effects 0.000 abstract description 18
- 238000000926 separation method Methods 0.000 abstract description 15
- 238000005516 engineering process Methods 0.000 abstract description 13
- 239000002351 wastewater Substances 0.000 abstract description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 6
- 239000001301 oxygen Substances 0.000 abstract description 6
- 229910052760 oxygen Inorganic materials 0.000 abstract description 6
- 238000012423 maintenance Methods 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000012546 transfer Methods 0.000 abstract description 2
- 238000004065 wastewater treatment Methods 0.000 abstract 2
- 230000007774 longterm Effects 0.000 abstract 1
- 239000011259 mixed solution Substances 0.000 description 19
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 238000001914 filtration Methods 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 230000000813 microbial effect Effects 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 238000010008 shearing Methods 0.000 description 3
- 241000894006 Bacteria Species 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000693 micelle Substances 0.000 description 2
- 238000006213 oxygenation reaction Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- FRXSZNDVFUDTIR-UHFFFAOYSA-N 6-methoxy-1,2,3,4-tetrahydroquinoline Chemical compound N1CCCC2=CC(OC)=CC=C21 FRXSZNDVFUDTIR-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000002427 irreversible effect Effects 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 230000002503 metabolic effect Effects 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000010841 municipal wastewater Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
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- 239000000725 suspension Substances 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
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Classifications
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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
本发明提供一种利用生化技术和膜分离技术处理废水的设备，特别涉及一种自吸式射流喷头曝气外置式膜生物反应器废水处理设备。该设备由集成生物反应器、自吸式射流喷头曝气单元和外置式膜分离单元组成。本发明集成深层曝气、生物流化床、射流曝气、膜分离及SBR脱氮除磷工艺等多种水处理技术的优点，氧转移利用效率高，不需鼓风曝气设备，剩余污泥少，可实现低能耗下长时间稳定运行。该设备出水水质好，工艺紧凑，占地面积小，设备投资少，便于检修维护，易于实现自动控制，在废水处理及回用领域有较好的应用前景。
The invention provides a device for treating waste water using biochemical technology and membrane separation technology, in particular to a self-priming jet nozzle aeration external membrane bioreactor waste water treatment device. The equipment consists of an integrated bioreactor, a self-priming jet nozzle aeration unit and an external membrane separation unit. The invention integrates the advantages of various water treatment technologies such as deep aeration, biological fluidized bed, jet aeration, membrane separation and SBR denitrification and dephosphorization technology, and has high oxygen transfer and utilization efficiency, no need for blower aeration equipment, and residual pollution With less mud, it can achieve long-term stable operation with low energy consumption. The equipment has good effluent quality, compact process, small footprint, low equipment investment, easy maintenance and automatic control, and has a good application prospect in the field of wastewater treatment and reuse.
Description
Technical field
The invention belongs to the equipment that utilizes biochemical technology and membrane separation technique to process waste water, particularly a kind of Self-priming jet aeration external membrane bioreactor sewage treatment equipment.
Background technology
Membrane bioreactor is the combination of traditional activated sludge process and membrane separation technique.Microbial Communities in Activated Sludge carries out biological degradation to organism in the former water, reaches to remove organic purpose.Film separation unit has replaced the second pond in the traditional technology, can hold back suspended solid in the former water, colloidalmaterial etc., guarantees high-quality and stable effluent quality.Membrane bioreactor has been compared following advantage with traditional water technology: floor space is little, only is 1/3～1/2 of traditional technology; Effluent quality is good, but reuse; Turbidity is starkly lower than traditional technology, for the removals of colibacillus, phage and poisonous Micropollutants clearly; Sludge concentration is high in the biological processing unit, and mud is long age, and is high to organic removal rate; For nitrogen and phosphorus pollutants higher removal effect is arranged; Compare with traditional technology, the surplus sludge volume that membrane bioreactor produces is few, has reduced the expense that excess sludge is disposed.Membrane biological reactor process is simple, volume is little, operational management is convenient, be easy to realize automatic control.
According to the relative position of membrane module and bio-reactor, membrane bioreactor is divided into submerged membrane bioreactor and external membrane bioreactor.
External membrane bioreactor is separated bio-reactor and membrane module, the mixed solution of bio-reactor enters membrane module after supercharging, see through under pressure film and obtain system's water outlet, active sludge then is trapped, and is back to (Fig. 5) in the bio-reactor with concentrated solution.The external membrane bioreactor characteristics are stable and reliable operations, be easy to membrane washing, change and set up, and membrane flux is generally larger.But known external membrane bioreactor adopts blast aeration to provide metabolic needed air for active sludge more, and works the effect of mixing.Be that biological reaction tank configuration blast aeration system needs expensive investment, caused the membrane bioreactor system fixed investment too high with the membrane separation plant of high cost.The blast aeration process needs lot of energy, also is difficult for carrying out the denitrification process operation.Under the general condition, for reducing pollutent in the deposition on film surface, prolong the membrane washing cycle, external film separation unit needs recycle pump that higher face cross-flow flow velocity is provided, the water circulation amount is large, power charge is high, it is reported, existing known external membrane bioreactor unit consumption of energy is very high, generally at 3～5kWh/m
3, approximately be 10～15 times of conventional activated sludge process.Membrane bioreactor utilizes the concentrated characteristic of membrane sepn to improve the sludge concentration of biological reaction tank, thereby increases the removal ability of biological reaction tank, is easy to form film and pollutes but sludge concentration is too high, and under certain condition, sludge concentration is higher, and membrane flux is lower; Have research to think, the face cross-flow velocity is not more high better, and the increase of crossflow velocity is so that the attenuation of film surface contamination layer might cause irreversible pollution, and the shearing force that the high speed rotating of pump produces can make the certain micro-organisms thalline produce deactivation phenomenom.Therefore, should manage existing external membrane bioreactor wastewater processing technology is improved, solve the problems such as present known external membrane bioreactor investment is high, working cost is high.
Summary of the invention
The object of the invention is to overcome the defectives such as the investment of known external membrane bioreactor is high, working cost is high, and a kind of easy handling and maintenance, self-priming fluid jet nozzle aeration external membrane bioreactor that the investment working cost is lower are provided.
Equipment of the present invention is comprised of integrated bio reactor, external membrane separating unit and self-priming fluid jet nozzle aeration unit.
Described integrated bio reactor is comprised of the degassed pond on the deep aerating biochemical reaction tank that is positioned at the bottom and top.In biochemical reaction tank, be provided with center water conservancy diversion inner core, the water conservancy diversion inner core is for falling the stream pipe, circular channel between pool wall and inner core is upspout, circulation force (forcing) pump water sucking mouth is arranged in the degassed pond, self-priming fluid jet nozzle (3) water outlet is downward, be installed in inner core central upper portion position, raw water inlet is installed in self-priming fluid jet nozzle (3) below.Described external membrane separating unit is comprised of membrane module, circulation force (forcing) pump, membrane module washing unit, pipeline, valve, instrument and electrical control etc.; Described membrane module adopts the external placed type filtered version, and pore size filter is between (micro-filtration) between 0.1～0.4 μ m and 0.05～0.1 μ m (ultrafiltration); The necessary membrane module washing unit of membrane module configuration, this device can be combined into a whole set of equipment with membrane bioreactor as required, also can be designed to mobile unit, and realization one cover washing unit is served a plurality of film bioreactor devices.
The self-priming fluid jet nozzle aeration of the present invention external membrane bioreactor is processed the waster water process flow process:
Pending waste water at first enters the self-priming fluid jet nozzle in deep aerating biochemical reaction tank central draft tube top (3) below by raw water inlet (11); What the circulation force (forcing) pump produced injects the reaction tank central draft tube through the concentrated cycle of higher pressure liquid of membrane module behind self-priming fluid jet nozzle (3) aeration, make the fluid jet nozzle below form the High Speed Turbulent shear zone, fluid jet nozzle utilizes cycle of higher pressure liquid to produce the negative pressure air amount and make it be dispersed into micro-bubble through shower nozzle, the water inlet of carrying the fluid jet nozzle below secretly forms the mixed solution that is rich in oxygen and active sludge and flows downward along central draft tube, carry out simultaneously the high-efficiency aerobic biochemical reaction, after arriving reactor bottom, upwards backflow through annular upspout again and arrive annular upspout top, most of oxygen is consumed by biochemical reaction in the mixed solution at this moment, a part of mixed solution jet under shearing wherein, operation so moves in circles, so, sewage is by repeatedly oxygenation, bubble and microbial bacteria micelle are constantly sheared refinement, form fine and close tiny flocs unit, carry out the efficient biochemical reaction in the reciprocation cycle process, the organic pollution materials in the waste water is degraded; It more than is biochemical reaction cycle process.
Another part mixed solution enters degassed pond, sloughs the air pocket in the mixed solution, is beneficial to enter the membrane sepn recycle system and carries out jet-flow aeration; Simultaneously, mud in the mixed solution has part and sinks at the bottom of the degassed pond, and pool bottom sludge backflash with a slope is slipped to the biochemical reaction tank central draft tube through degassed pond, the biochemical working cycle of sustainable participation, this process can reduce the circulation fluid sludge concentration that enters film separation unit, is conducive to alleviate film and pollutes; Mixed solution after the degassed and mud-water separation enters membrane module and carries out filtering separation after the supercharging of circulation force (forcing) pump, concentrated solution after the filtration enters the biochemistry pool central draft tube and continues biochemical working cycle behind the fluid jet nozzle aeration, film separating system sees through liquid and is system's water outlet; It more than is the membrane sepn working cycle.
Above two processes are moved continuously, move in circles, and can realize continuous flow and make that organism is purified by aerobic oxidation in the waste water.
Beneficial effect of the present invention is:
1. in the outlet of external placed type film separation unit circulation fluid self-priming fluid jet nozzle aeration is set and replaces blast aeration, save the aerating system facility investment, self-priming fluid jet nozzle is simple in structure, cost is low, Maintenance and Repair are convenient.
2. utilize circulation force (forcing) pump energy more than needed and fluid jet nozzle to carry out aeration, save the large energy that the blast aeration process consumes, the advantage of biochemical reaction tank is integrated biological fluidized bed and two kinds of water technologies of deep aerating, mud is the suspension fluidized state in the reactor, mixed solution muddy water gas three-phase is mixed more even, the transfer efficiency of oxygen is higher, improves biochemical reaction efficient, so the reactor total energy consumption is lower, reduced ton water treatment running cost.
3. most of biochemical circulation mixed solution enters degassed pond from upspout and sloughs air pocket, carries out simultaneously simple precipitation, and the sludge concentration that enters film separation unit with reduction enters membrane module and filters after the supercharging of circulation force (forcing) pump; High pressure mixing liquid easily reaches turbulence state, can make membrane sepn long-play and be difficult for film and pollute under the cross-flow velocity of lower film surface, prolongs film cleaning interval and work-ing life, reduces energy consumption, reduces film cleaning, maintenance and replacement charge.
Description of drawings
Fig. 1 is self-priming fluid jet nozzle aeration external membrane bioreactor process flow sheet
Fig. 2 is self-priming fluid jet nozzle aeration unit (b) schematic diagram
Fig. 3 is external membrane assembly unit (c) schematic diagram
Fig. 4 is integrated bio reactor (a) schematic diagram
Fig. 5 is existing external membrane bioreactor schematic diagram
A-integrated bio reactor among the figure, the self-priming fluid jet nozzle aeration unit of b-, c-external membrane separating unit, 1-deep aerating biochemical reaction tank, the degassed pond of 2-, the self-priming fluid jet nozzle of 3-, the 4-air flowmeter, 5-circulation force (forcing) pump, 6-tensimeter, 7-external membrane assembly, the 8-Graceful mouth of a river, 9-membrane module washing unit, 10-clean water basin, the 11-raw water inlet, 12-circulation force (forcing) pump water sucking mouth.
Embodiment:
Below in conjunction with accompanying drawing technological process of the present invention is further described.
As shown in Figure 1, raw water inlet (11) is positioned at self-priming fluid jet nozzle (3) below on deep aerating biochemical reaction tank (1) central draft tube top, and circulation force (forcing) pump water sucking mouth (12) is arranged in degassed pond (2); Mixed solution was by external membrane assembly (7) filtering separation after the circulation force (forcing) pump sucked degassed and simple precipitation by the water sucking mouth, high speed flow concentrated solution after the filtration is injected the biochemistry pool central draft tube behind self-priming fluid jet nozzle (3) aeration, can below shower nozzle, form the High Speed Turbulent shear zone, the gas that ejector is sucked further is dispersed into tiny bubble, and the former water of carrying the shower nozzle below secretly is intake, the combined sewage that oxygen and active sludge are rich in formation flows downward along guide shell, carries out simultaneously the high-efficiency aerobic biochemical reaction; After the sewage mixed solution arrives reactor bottom, upwards backflow through annular upspout again and arrive the upspout top, most of oxygen is consumed by biochemical reaction in the mixed solution at this moment, a part of mixed solution jet under shearing wherein, operation so moves in circles, so, the sewage mixed solution is by repeatedly oxygenation, bubble and microbial bacteria micelle are constantly sheared refinement, and the fine and close tiny flocs unit of formation, carry out the efficient biochemical reaction in the reciprocation cycle process, the organic pollution materials in the waste water obtains degraded and removes; Another part mixed solution enters degassed pond, slough the air pocket in the mixed solution, simultaneously, the mud in the mixed solution has part and sinks at the bottom of the pond, pool bottom sludge backflash with a slope is slipped to the biochemical reaction tank central draft tube through degassed pond, the biochemical working cycle of sustainable participation; Mixed solution after the degassed and simple precipitation enters membrane module and carries out filtering separation after the supercharging of circulation force (forcing) pump, concentrated solution enters next time biochemical working cycle of biochemistry pool central draft tube continuation again after filtering behind self-priming fluid jet nozzle (3) aeration, membrane filtration sees through liquid and is system's water outlet, and water outlet enters clean water basin (10).Above process is moved continuously, moves in circles, and can realize continuous flow and Organic Pollutants in Wastewater is degraded and is purified.Membrane module washing unit (9) cleans membrane module as required.
Below be illustrated for example, but claim scope of the present invention is not limited only to this.
| Project | Influent quality | Effluent quality | Degree for the treatment of (%) |
| BOD 5(mg/L) | 100～180 | ≤10 | ≥90～94.4 |
| COD(mg/L) | 250～450 | ≤15 | ≥80～89.00 |
| pH | 6～9 | 6～9 | / |
| PO 4-P(mg/L) | 3～6 | ≤0.5 | ≥83.3～87.5 |
| Total nitrogen (mg/L) | 24～45 | ≤15 | ≥40～66.7 |
| Ammonia nitrogen (mg/L) | 20～35 | ≤5 | ≥75～85.7 |
Treatment effect is higher than GB18918-2002 one-level A standard, and stable water outlet.
Treatment effect is better than GB18918-2002 one-level A standard, and stable water outlet.
| Project | Influent quality | Effluent quality | Degree for the treatment of (%) |
| COD(mg/L) | 500～600 | ≤40 | ≥90～92.00 |
| pH | 6～9 | 6～9 | / |
| PO 4-P(mg/L) | 5～8 | ≤0.5 | ≥90～93 |
| Total nitrogen (mg/L) | 30～45 | ≤14 | ≥40～66.7 |
| Ammonia nitrogen (mg/L) | 20～25 | ≤5 | ≥75～80 |
Claims (3)
1. a self-priming fluid jet nozzle aeration external membrane bioreactor sewage treatment equipment is characterized in that this equipment is comprised of integrated bio reactor (a), self-priming fluid jet nozzle aeration unit (b) and external membrane separating unit (c).Described integrated bio reactor (a) is comprised of two portions: the one, be positioned at the deep aerating biochemical reaction tank (1) of bottom, and the 2nd, superposed degassed pond (2); Center water conservancy diversion inner core is set in the deep aerating biochemical reaction tank, and the water conservancy diversion inner core is for falling the stream pipe, and the circular channel between biochemical reaction tank urceolus and inner core is upspout.Described Self-priming jet aeration unit (b) is comprised of self-priming fluid jet nozzle (3) and under meter (4) etc.Described external membrane separating unit (c) is comprised of external membrane assembly (7), circulation force (forcing) pump (5), membrane module washing unit (9), pipeline, valve, instrument (6) and electrical control etc.
2. a kind of self-priming fluid jet nozzle aeration external membrane bioreactor according to claim 1, it is characterized in that: described Self-priming jet aeration unit (b) is comprised of self-priming fluid jet nozzle (3) and under meter (4) etc., aerating apparatus is self-priming fluid jet nozzle (3), and self-priming fluid jet nozzle (3) is installed in the circulation fluid exit.
3. a kind of self-priming fluid jet nozzle aeration external membrane bioreactor according to claim 1, it is characterized in that: deep aerating biochemical reaction tank urceolus bottom, described integrated bio reactor (a) bottom is closed and repaiies the garden by the current streamline, center water conservancy diversion inner core open at both ends, connect degassed pond (2) at the biochemical reaction tank top, degassed pond is provided with the sludge reflux groove at the bottom of the pond, and backflash is with certain slope slope aspect biochemical reaction tank central draft tube; Circulation force (forcing) pump water sucking mouth (12) is arranged in the degassed pond, water outlet is installed self-priming fluid jet nozzle (3), the shower nozzle water outlet is downward, is arranged in central draft tube top centre, and raw water inlet (11) is arranged in self-priming fluid jet nozzle (3) below.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2011101887146A CN102863075A (en) | 2011-07-07 | 2011-07-07 | External membrane bioreactor with self-suction jet nozzle aerating function |
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| CN2011101887146A CN102863075A (en) | 2011-07-07 | 2011-07-07 | External membrane bioreactor with self-suction jet nozzle aerating function |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104192989A (en) * | 2014-09-22 | 2014-12-10 | 武汉兴天宇环境工程有限公司 | Jet circulation reactor for sewage treatment |
| CN110713252A (en) * | 2018-07-13 | 2020-01-21 | 南通星辰合成材料有限公司 | Efficient biological aerobic reaction device and sewage treatment method thereof |
| CN110734135A (en) * | 2019-11-25 | 2020-01-31 | 上海世渊环保科技有限公司 | anaerobic membrane bioreactors |
| CN111542500A (en) * | 2018-02-20 | 2020-08-14 | 栗田工业株式会社 | Aerobic biological treatment device and operation method thereof |
| CN113754073A (en) * | 2021-09-16 | 2021-12-07 | 华夏碧水环保科技有限公司 | Microorganism carrier solidification generator |
| CN114890521A (en) * | 2022-06-02 | 2022-08-12 | 上海熊猫机械(集团)有限公司 | Integrated vertical flocculation water purification equipment |
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|---|---|---|---|---|
| CN101941757A (en) * | 2010-09-06 | 2011-01-12 | 河南工业大学 | Air supply type jet aerating external membrane bioreactor |
| CN101941778A (en) * | 2010-09-06 | 2011-01-12 | 河南工业大学 | Self-priming jet aeration external membrane bioreactor |
-
2011
- 2011-07-07 CN CN2011101887146A patent/CN102863075A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101941757A (en) * | 2010-09-06 | 2011-01-12 | 河南工业大学 | Air supply type jet aerating external membrane bioreactor |
| CN101941778A (en) * | 2010-09-06 | 2011-01-12 | 河南工业大学 | Self-priming jet aeration external membrane bioreactor |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104192989A (en) * | 2014-09-22 | 2014-12-10 | 武汉兴天宇环境工程有限公司 | Jet circulation reactor for sewage treatment |
| CN104192989B (en) * | 2014-09-22 | 2016-03-02 | 武汉兴天宇环境工程有限公司 | A kind of injection circulation reactor for sewage disposal |
| CN111542500A (en) * | 2018-02-20 | 2020-08-14 | 栗田工业株式会社 | Aerobic biological treatment device and operation method thereof |
| CN110713252A (en) * | 2018-07-13 | 2020-01-21 | 南通星辰合成材料有限公司 | Efficient biological aerobic reaction device and sewage treatment method thereof |
| CN110734135A (en) * | 2019-11-25 | 2020-01-31 | 上海世渊环保科技有限公司 | anaerobic membrane bioreactors |
| CN113754073A (en) * | 2021-09-16 | 2021-12-07 | 华夏碧水环保科技有限公司 | Microorganism carrier solidification generator |
| CN114890521A (en) * | 2022-06-02 | 2022-08-12 | 上海熊猫机械(集团)有限公司 | Integrated vertical flocculation water purification equipment |
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Application publication date: 20130109 |