CN1256286C - Membrane aeration and membrane separation coupled sewage treatment device and method - Google Patents
Membrane aeration and membrane separation coupled sewage treatment device and method Download PDFInfo
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- CN1256286C CN1256286C CNB2004100205544A CN200410020554A CN1256286C CN 1256286 C CN1256286 C CN 1256286C CN B2004100205544 A CNB2004100205544 A CN B2004100205544A CN 200410020554 A CN200410020554 A CN 200410020554A CN 1256286 C CN1256286 C CN 1256286C
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- aeration
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- oxygen
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- 238000005273 aeration Methods 0.000 title claims abstract description 63
- 239000012528 membrane Substances 0.000 title claims abstract description 36
- 239000010865 sewage Substances 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title claims abstract description 10
- 238000000926 separation method Methods 0.000 title abstract description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 36
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 36
- 239000001301 oxygen Substances 0.000 claims abstract description 36
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 32
- 239000010802 sludge Substances 0.000 claims abstract description 13
- 238000010992 reflux Methods 0.000 claims abstract description 7
- 230000008878 coupling Effects 0.000 claims abstract description 6
- 238000010168 coupling process Methods 0.000 claims abstract description 6
- 238000005859 coupling reaction Methods 0.000 claims abstract description 6
- 230000002209 hydrophobic effect Effects 0.000 claims abstract description 4
- 239000000835 fiber Substances 0.000 claims description 13
- 239000012141 concentrate Substances 0.000 claims description 6
- 230000000694 effects Effects 0.000 claims description 6
- 239000011259 mixed solution Substances 0.000 claims description 6
- 238000011068 loading method Methods 0.000 claims description 4
- 230000004907 flux Effects 0.000 claims description 3
- 239000012510 hollow fiber Substances 0.000 claims description 3
- 230000008676 import Effects 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 230000008901 benefit Effects 0.000 abstract description 5
- 238000012545 processing Methods 0.000 abstract description 4
- 230000005540 biological transmission Effects 0.000 abstract description 2
- 239000012535 impurity Substances 0.000 abstract description 2
- 238000006065 biodegradation reaction Methods 0.000 abstract 1
- 230000007613 environmental effect Effects 0.000 abstract 1
- 238000010008 shearing Methods 0.000 abstract 1
- UEKDBDAWIKHROY-UHFFFAOYSA-L bis(4-bromo-2,6-ditert-butylphenoxy)-methylalumane Chemical compound [Al+2]C.CC(C)(C)C1=CC(Br)=CC(C(C)(C)C)=C1[O-].CC(C)(C)C1=CC(Br)=CC(C(C)(C)C)=C1[O-] UEKDBDAWIKHROY-UHFFFAOYSA-L 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- 239000007788 liquid Substances 0.000 description 5
- 244000005700 microbiome Species 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- 239000002351 wastewater Substances 0.000 description 5
- 238000009792 diffusion process Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000001351 cycling effect Effects 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 230000002503 metabolic effect Effects 0.000 description 1
- 230000004060 metabolic process Effects 0.000 description 1
- 230000002906 microbiologic effect Effects 0.000 description 1
- 239000012982 microporous membrane Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000003206 sterilizing agent Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 238000009736 wetting Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/20—Activated sludge processes using diffusers
- C02F3/208—Membrane aeration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2688—Biological processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/26—Specific gas distributors or gas intakes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2319/00—Membrane assemblies within one housing
- B01D2319/06—Use of membranes of different materials or properties within one module
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/18—Use of gases
- B01D2321/185—Aeration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2325/00—Details relating to properties of membranes
- B01D2325/36—Hydrophilic membranes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2325/00—Details relating to properties of membranes
- B01D2325/38—Hydrophobic membranes
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Life Sciences & Earth Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Activated Sludge Processes (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The present invention provides a device and a method for processing sewage by coupling of membrane aeration and membrane separation, which belongs to the technical field of sewage processing and water reutilization of environmental engneering. The present invention is characterized in that a hydrophobic membrane for aeration and a hydrophilic membrane for separation are arranged in the same cylindrical reactor to form a membrane aeration separating reactor; in addition, a bioreactor is arranged on a reflux pipeline, and thus, the processed sewage flows between the two reactors cyclically to realize coupling of no-bulb aeration, membrane separation and biodegradation. The present invention has the advantages that the membrane aeration can make the oxygen utilization efficiency reach or approach to 100%, dissolved oxygen is sufficient to improve the volume load of the bioreactor, the separation membrane can remove suspended impurities thoroughly, effluent water does not need to be sterilized, the quantity of excess sludge is reduced when the active sludge is trapped to the biological quantity, the membrane pollution of the separation membrane can be alleviated by the shearing action generated from a reflux pump, and simultaneously, oxygen transmission can not be blocked by the thickness of a surface biomembrane of the aeration membrane. The present invention also has the advantages of small land occupation and low cost.
Description
Technical field
The invention belongs to field of environment engineering technology, relate to sewage disposal and technology of middle water recycle, the sewage water treatment method of particularly a kind of film aeration and membrane sepn coupling device.
Background technology
China is one of 13 poor-water states in the world, a lack of water surplus in the of existing 400 in the city surplus in the of 600, because of the industrial output value that lack of water reduces annual above 1,200 hundred million yuan.Use water quality and the water price middle water low than Drinking Water is afforested, carwash, flushing sanitation utensil etc., water resources that can saves valuable relaxes the imbalance between supply and demand of municipal water, also can reduce the burden of sewerage system.Film-separation biological reactor (membrane separationbioreactor MSBR) is considered to one of the most rising wastewater treatment and reuse technology, itself can substitute three technologies in activated sludge tank, second pond, filter tank in the traditional wastewater processing, water outlet only need add a small amount of sterilizing agent (avoiding taking place secondary pollution) just can realize reuse, and excess sludge production is low, and is easy to operate.But resistance is bigger when seeing through liquid-gas interface owing to oxygen, causes the utilising efficiency of oxygen low, has the oxygen of 80%-90% to overflow from mixed solution during aeration, is not utilized; MSBR sludge concentration height has bigger demand to oxygen, and the method that increases aeration rate not only can increase power consumption and cost of equipment, also can make bubble enter the membrane module outlet conduit, influences the normal operation of film separating system.Therefore, it is very necessary to seek new oxygen supply mode.
Film aeration and biological reactor (membrane aeration bioreactor MABR) utilizes hydrophobic microporous membrane to the microorganism oxygen supply.Under the oxygen pressure effect, oxygen in the tubular fibre tube chamber diffuses into waste water by the micropore on membranous wall or the membranous wall, because the membranous wall micropore size is very little, and maintenance oxygen pressure in service is lower than bubbling pressure, so no naked eyes visible bubble in bubble is called foamless oxygen-supplying in the liquid.In foamless oxygen-supplying, oxygen directly diffuses into liquid with molecularity, and oxygen transfer efficiency is near a hundred per cent, and simultaneously, unit volume hollow fiber film assembly contact area is bigger, is more conducive to the diffusion of oxygen.In MABR, sufficient because speed of oxygen supply is fast, also can accelerate biochemical reaction speed, thereby improve the sewage treatment capacity of reactor, equipment volume is reduced, floor space is little, reduce cost, but the excess sludge production of MABR is big and effluent quality is not good.When MABR handles carbon containing sewage, because microorganism growth speed is fast, be mingled with not removed as yet suspended substance in the organism that comes off in a large number and the sewage in the water outlet, Hsieh points out that MABR is not suitable for handling carbon containing sewage; Need before the MABR water outlet water sample analysis in people's such as Hibiy and Hsieh the test to reduce wherein suspended solids and microorganism with 0.22 μ m membrane filtration, Semmens then makes the MABR water outlet handle through settling pond again and guarantees water quality.
Film-separation biological reactor and film aeration and biological reactor all are a kind of of membrane bioreactor (MBR), and be all with the obvious advantage, but the problem that exists do not allow to avoid yet, in fact yoke the promotion and application of two kinds of technologies.
Summary of the invention
The purpose of this invention is to provide the be coupled sewage water treatment method of device of a kind of film aeration and membrane sepn, its required device is called film aeration separating bio reactor, form by film aeration separate reactor and bio-reactor two portions, the elite of the novel sewage water treatment method of this kind comprehensive film aeration and biological reactor and two kinds of technologies of film-separation biological reactor, and remedied defective separately, thereby it is good to have effluent quality simultaneously, oxygen transfer efficiency height, advantage such as floor space is little, excess sludge production is low.
Realize that the be coupled technical scheme of sewage water treatment method of device of film aeration of the present invention and membrane sepn is:
Wetting ability separatory membrane and hydrophobicity aeration film are placed in the same cylindrical reactor, are called film aeration separate reactor, utilize the diffusion system of aeration film, improve the utilising efficiency of oxygen as oxygen; Utilize separatory membrane to system water outlet filter, guarantee the effluent quality high-quality and safety.Film aeration separate reactor is assembled first part by three parts: the cylindrical reactor central vertical is installed hydrophobic hollow fiber aeration film bundle, and every fiber tip concentrates in the cylindric end socket, and shut the end socket outside, and inner hollow connects aerated conduit; The fiber bottom concentrates in another cylindric end socket, the tip sealing.Second section: around aeration film bundle, hydrophilic hollow fibre separatory membrane bundle is installed vertically in the form of a ring, every fiber bottom concentrates in the annulus column end socket, and shut the end socket outside, and inner hollow connects outlet conduit; Fiber tip concentrates in another annulus column end socket, the tip sealing.Aeration film and separatory membrane all make it take place when installing small loosening, and the root root is independent between the fiber, waves and does not disturb mutually, can alleviate obstruction.Third part: cylindrical shell makes reactor monolith be air-tight state, and circulation line is established in the film aeration separate reactor outside.This three part of moduleization, but ease of assembly.
Film aeration separate reactor outside circulation line is provided with bio-reactor, and stirrer is set in the reactor, keeps active sludge to be in suspended state.
Oxygen imports from the upper end of film aeration separate reactor, flows in aeration film tubular fibre tube chamber, and under the effect of certain pressure, oxygen diffusion enters returned sluge, thereby enters bio-reactor, satisfies microbiological oxidation degradable organic pollutant oxygen consumption demand; Sewage and returned sluge enter from bio-reactor top, mix with wherein active sludge, and the metabolism by microorganism is purified sewage; Reacted mixed solution is sent into from film aeration separate reactor bottom through the reflux pump effect, carries out solid-liquid separation, and the clear water that sees through separatory membrane can discharge or reuse, and concentrated solution is re-used as returned sluge and sends bio-reactor back to.
The separatory membrane membrane flux is at 20-50L/hm
2Mixed solution cross-flow flow velocity is 2-4m/s in the film aeration separate reactor; Cycling rate (inflow-rate of water turbine/transit dose) is 25-75; For guaranteeing bubble-free aeration, keep oxygen pressure≤1bar; Because of oxygen transfer speed is fast sufficient, the volumetric loading rate of bio-reactor can be increased to 5-10kgCOD/m
3D; The oxygen mass transfer coefficients of tubular fibre hydrophobicity aeration film is at 10gO in the turbulent flow liquid
2/ m
2About hbar.
Effect of the present invention and benefit are:
1. the bubble-free aeration coefficient of oxygen utilization also can make it to be complementary with oxygen requirement by the control oxygen-supplying amount near absolutely, cuts down the consumption of energy; Owing to speed of oxygen supply is fast and sufficient, also can improve the sewage treatment capacity of bio-reactor, improve load, reduce occupation of land, reduce cost.
2. returned sluge dissolved oxygen concentration height in film aeration separate reactor, enter bio-reactor, dissolved oxygen concentration reduces gradually, by suitable control, active sludge is moved in circles in aerobic, anoxic and anaerobic environment, significantly improve system's denitrogenation dephosphorizing function.
In the system owing to there is separatory membrane, can thoroughly remove suspended impurity, water outlet need not be sterilized, and system do not influence by the mud expansible, and reduces the excess sludge growing amount.
4. the reflux pump effect makes that mixed solution is turbulent shape state in the film aeration separate reactor, when delaying the separatory membrane film and polluting, can guarantee that aeration film surface biological film thickness can not cause obstruction to the transmission of oxygen.
The present invention can save energy and be simple to operate, and stable effluent quality, reliable can be widely used in the processing of high oxygen requirement waste water, as percolate, high ammonia concentration waste water etc.
Description of drawings
Accompanying drawing is a film aeration separating bio reactor synoptic diagram.
Among the figure: 1 separatory membrane; 2 aeration films; 3 film aeration separate reactors; 4 bio-reactors; 5 stirrers; 6 reflux pumps.
Embodiment
Below in conjunction with technical scheme and accompanying drawing, describe the specific embodiment of the invention in detail.
Embodiment
The amount of disposing of sewage is by 10m
3/ d meter, COD concentration is 500mg/l.Oxygen imports from the upper end of film aeration separate reactor 3, diffuses into returned sluge through aeration film 2, enters bio-reactor 4 with returned sluge; Sewage and returned sluge enter from bio-reactor 4 tops, utilize stirrer 5 to stir, mix mutually with active sludge wherein, metabolic activity by microorganism is purified waste water, reacted mixed solution is sent into from film aeration separate reactor bottom through reflux pump 6, carry out solid-liquid separation, the clear water that sees through separatory membrane 1 can discharge or reuse, and concentrated solution is sent bio-reactor again back to.
Film aeration separate reactor is of a size of φ 0.1 * 1.5m, and wherein hydrophobicity aeration film and clear water separatory membrane all adopt the tubular fibre of diameter 1mm, length 1.2m; When separatory membrane quantity was got 3000, as calculated, its membrane flux was 37L/hm
2, at 20-50L/hm
2Scope within; Getting aeration film oxygen mass transfer coefficients is 10gO
2/ m
2Hbar, oxygen pressure are 1bar, and the COD500mg/l of then will intaking is degraded to water outlet COD20mg/l, 3200 of the aeration films of need φ 0.01 * 1.2m; Calculating aeration film and separatory membrane volume adds and accounts for 49.6% of film aeration separate reactor volume.When the cross-flow flow velocity was 2m/s, the cycling rate of film aeration separate reactor was 51.5, within the 25-75 scope.The bio-reactor volumetric loading is got 5kgCOD/m
3D, then the bio-reactor useful volume is 1m
3, get it and specifically be of a size of 1m * 1m * 1.2m (length), available depth 1m.Strengthen if handle the water yield, identical film aeration separate reactor parallel running then can be set, and bio-reactor is calculated by volumetric loading and makes its volume do corresponding increase to get final product.
Claims (2)
1. the sewage water treatment method of film aeration and membrane sepn coupling device is characterized in that:
A) in the film aeration separate reactor, in reactor center, the fiber upper end concentrates in the cylindric end socket aeration with hydrophobic hollow fiber film bundle positioned vertical, and end socket is connected to aerated conduit, oxygen pressure requirement≤1.0bar;
B) in the film aeration separate reactor, separate and use hydrophilic hollow fibre film bundle to center on aeration film bundle positioned vertical ringwise, the fiber lower end concentrates in the annulus column end socket, and end socket is connected to outlet conduit, and the separatory membrane membrane flux is 20-50L/hm
2
C) on the circulation line of the film aeration separate reactor outside bio-reactor is arranged, the volumetric loading of bio-reactor is 5-10kgCOD/m
3D;
D) oxygen imports from the upper end of film aeration separate reactor, diffuses into returned sluge through the aeration film, enters bio-reactor with returned sluge;
E) sewage and returned sluge enter from bio-reactor top, mix with active sludge; Reacted mixed solution is sent into film aeration separate reactor through the reflux pump effect from the bottom.
2. the sewage water treatment method of a kind of film aeration according to claim 1 and membrane sepn coupling device is characterized in that: film aeration separate reactor is cylindric closed reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100205544A CN1256286C (en) | 2004-05-13 | 2004-05-13 | Membrane aeration and membrane separation coupled sewage treatment device and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100205544A CN1256286C (en) | 2004-05-13 | 2004-05-13 | Membrane aeration and membrane separation coupled sewage treatment device and method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1569682A CN1569682A (en) | 2005-01-26 |
| CN1256286C true CN1256286C (en) | 2006-05-17 |
Family
ID=34479743
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004100205544A Expired - Fee Related CN1256286C (en) | 2004-05-13 | 2004-05-13 | Membrane aeration and membrane separation coupled sewage treatment device and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1256286C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2024171001A1 (en) | 2023-02-15 | 2024-08-22 | Greco Giovambattista | Micro-ultrafiltration system with tubular membranes |
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| CN100457650C (en) * | 2007-02-05 | 2009-02-04 | 哈尔滨工业大学 | Integrated bubble-free aeration biological composite film film-separation biological reactor |
| CN101074141B (en) * | 2007-06-20 | 2010-05-19 | 大连春兴水处理科技发展有限公司 | Process for regenerating, recovering and reutilizing low-concentration organic waste water |
| CN101274810B (en) * | 2008-05-20 | 2013-10-16 | 北京汉青天朗水处理科技有限公司 | Sewage treating device and process |
| ES2384544T3 (en) * | 2008-07-28 | 2012-07-06 | Aptwater, Inc. | Radial flow membrane biofilm reactor |
| US7875176B2 (en) * | 2009-03-06 | 2011-01-25 | Porous Media Corporation | Membrane module for fluid filtration |
| CN102531153B (en) * | 2011-12-21 | 2014-06-25 | 大连大学 | Integrated bubbleless aeration membrane bioreactor |
| CN102559480B (en) * | 2011-12-27 | 2013-02-06 | 浙江大学 | Anaerobic methane oxidation bacteria enriching device by using external methane bubbleless aeration biomembrane and method therefor |
| CN102897905A (en) * | 2012-09-26 | 2013-01-30 | 冯秀娟 | Activated sludge reactor |
| KR102706720B1 (en) | 2013-02-22 | 2024-09-12 | 비엘 테크놀러지스 인크. | Membrane assembly for supporting a biofilm |
| US10160679B2 (en) * | 2014-03-20 | 2018-12-25 | Bl Technologies, Inc. | Wastewater treatment with primary treatment and MBR or MABR-IFAS reactor |
| CN105036449A (en) * | 2015-04-22 | 2015-11-11 | 南京大学 | Degradation-resistant nitrile compound industrial sewage treatment method |
| CN108430936A (en) * | 2015-09-30 | 2018-08-21 | 株式会社拜特奇 | Wastewater treatment carrier, wastewater treatment carrier module, wastewater treatment carrier element and wastewater treatment equipment |
| CN106396091A (en) * | 2016-10-18 | 2017-02-15 | 天津膜天膜科技股份有限公司 | Hollow fiber membrane module, and sewage treatment system thereof |
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| CN107285466A (en) * | 2017-07-10 | 2017-10-24 | 天津城建大学 | The sewage-treatment plant and processing method of bubble-free aeration bioreactor synchronous nitration and denitrification |
| CN108128886B (en) * | 2018-01-11 | 2021-02-05 | 安徽泛湖生态科技股份有限公司 | Membrane filtration and aeration integrated device |
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| WO2020152680A1 (en) * | 2019-01-24 | 2020-07-30 | Fluence Water Products And Innovation Ltd | Methods for treating waste activated sludge with a membrane-aerated biofilm reactor |
| CN113666491A (en) * | 2021-09-29 | 2021-11-19 | 内蒙古蒙一环保科技有限责任公司 | Side-arranged cross-flow aeration membrane bioreactor |
-
2004
- 2004-05-13 CN CNB2004100205544A patent/CN1256286C/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2024171001A1 (en) | 2023-02-15 | 2024-08-22 | Greco Giovambattista | Micro-ultrafiltration system with tubular membranes |
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| Publication number | Publication date |
|---|---|
| CN1569682A (en) | 2005-01-26 |
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