CN100558655C - A kind of back-flushing operation method of bioreactor of dynamic membrane - Google Patents
A kind of back-flushing operation method of bioreactor of dynamic membrane Download PDFInfo
- Publication number
- CN100558655C CN100558655C CNB2006100438223A CN200610043822A CN100558655C CN 100558655 C CN100558655 C CN 100558655C CN B2006100438223 A CNB2006100438223 A CN B2006100438223A CN 200610043822 A CN200610043822 A CN 200610043822A CN 100558655 C CN100558655 C CN 100558655C
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- China
- Prior art keywords
- dynamic membrane
- membrane
- water outlet
- back flushing
- bioreactor
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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
Abstract
The invention discloses a kind of back-flushing operation method of bioreactor of dynamic membrane, belong to technical field of sewage.The reactor middle part is provided with the membrane module of being made by bolting silk, and aerating apparatus is installed in its below, through the dynamic membrane filtering water outlet, make the aerating apparatus of membrane module below, provide oxygen for the top mixed solution on the one hand, promote mixed solution to flow on the other hand, by mobile increase the washing away and disturbance of bubble and mixed solution to Dynamic Membrane; In the bioreactor of dynamic membrane operational process, in the time of the needs back flushing, close water outlet, the back flushing aeration tube to be opened, the back flushing air pump provides 1.6～8.0m
3/ (m
2* gas h).Use the present invention, can improve back flushing efficient greatly, reduce aeration intensity and aeration time, thereby reduce process cost; Compare with the high pressure water cleaning, can onlinely carry out, do not influence the reactor operation, can reduce destructiveness simultaneously, shorten Dynamic Membrane and recover the needed time Dynamic Membrane.
Description
Technical field
The present invention relates to a kind of back-flushing operation method of bioreactor of dynamic membrane, belong to technical field of sewage.
Background technology
The bioreactor of dynamic membrane of using all is that a baffle plate is set in reactor at present, and baffle plate is divided into two portions with reactor, and two portions all communicate up and down.Membrane module at one end is housed, and the other end water inlet is at the feed-water end aeration; At the other end membrane module is set, utilizes the head difference water outlet between reactor liquid level and the membrane module water outlet.In the operational process of bioreactor of dynamic membrane, along with the microbial growth breeding, Dynamic Membrane is long-pending more thick more, and this can cause the increase of resistance of membrane filtration, and the water outlet head constantly increases.When the water outlet head is excessive, just need carry out backwash operation to bioreactor of dynamic membrane.Empty aeration or high pressure water mode is clearly all adopted in the back flushing of bioreactor of dynamic membrane at present.Empty aeration i.e. aeration below membrane module, can cause the shake of mould material, and play the souring to Dynamic Membrane, thereby destroy Dynamic Membrane, reduces film and pollutes.It promptly is that membrane module is taken out that high pressure water cleans, and utilizes high pressure water directly to wash Dynamic Membrane, by the erosion damage Dynamic Membrane of current, reduces film and pollutes.The shortcoming of aforesaid operations mode: the reactor mixed solution is not enough to washing away of Dynamic Membrane, causes that easily film pollutes; The efficient of aeration back flushing is very low, need very big aeration rate and aeration time, especially, Dynamic Membrane is carried out back flushing in the mode of empty aeration for being the bioreactor of dynamic membrane of base material with the non-woven fabrics, base material is difficult to further reduced the efficient of back flushing by disturbance.High pressure water cleans and membrane module need be taken out, and reactor is out of service when back flushing, and the membrane module taking-up is needed to increase power-equipment, is unsuitable for large-scale reactor.High pressure water cleans too thorough to the destruction of Dynamic Membrane, and the time that the recovery of Dynamic Membrane needs after the back flushing is long.
Summary of the invention
In order to overcome the shortcoming of above-mentioned operation scheme, the present invention proposes a kind of back-flushing operation method of bioreactor of dynamic membrane, is promptly carrying out aeration below the membrane module in the operational process: during in back flushing, reversed reaction device water outlet direction is carried out aeration.Effective decelerating membrane pollution, and can especially be that the bioreactor of dynamic membrane of base material carries out back flushing efficiently with the non-woven fabrics to bioreactor of dynamic membrane, and shortened the needed time of recovery of Dynamic Membrane.
The objective of the invention is to be achieved through the following technical solutions.A kind of back-flushing operation method of bioreactor of dynamic membrane, its method is as follows:
1, is provided with the membrane module of making by bolting silk at the reactor middle part, and aerating apparatus is installed below membrane module, mixing sludge is under the effect of pressure reduction between liquid level and the water outlet, through the dynamic membrane filtering water outlet, the aerating apparatus of membrane module below provides oxygen for the top mixed solution on the one hand, promotes mixed solution to flow on the other hand, mobile increase by bubble and mixed solution is washed away and disturbance Dynamic Membrane, reaches the purpose of effective decelerating membrane pollution.
2, in the bioreactor of dynamic membrane operational process, in the time of the needs back flushing, close water outlet, the back flushing aeration tube is opened.The back flushing air pump provides 1.6～8.0m
3/ (m
2* gas h), gas enters membrane module by water outlet, sees through the Dynamic Membrane base material then and enters reactor.During gas process film base material, be ground into small bubble, Dynamic Membrane is destroyed by micro-bubble, pollutes thereby reduce film.After recoil 5～15min, reactor water outlet head greatly reduces, and membrane flux can recover substantially.
Use the present invention, can improve back flushing efficient greatly, reduce aeration intensity and aeration time, thereby reduce process cost; Compare with the high pressure water cleaning, can onlinely carry out, do not influence the reactor operation, can reduce destructiveness simultaneously, shorten Dynamic Membrane and recover the needed time Dynamic Membrane.Compared with prior art, use existing operation scheme: gas-water ratio is 20: 1, and the water outlet head of 25 days left and right sides reactors promptly reaches 12cm, needs back flushing; During back flushing, aeration intensity is 20m
3/ (m
2* aeration time 15min h).Using the general gas-water ratio of the present invention is 15: 1, and reactor can move about 50 days.Aeration intensity can be reduced to 3.2m during back flushing
3/ (m
2* h), aeration time 10min can reach former effect.
Description of drawings
Accompanying drawing is a setting drawing synoptic diagram of the present invention.
Wherein, 1, water-in, 2, aerating apparatus, 3, water outlet, 4, the back flushing aeration tube, 5, membrane module
Embodiment
Embodiment 1:
Structure as shown in drawings, bioreactor of dynamic membrane adopts permanent flux to filter, the MLSS of reactor is that 5000mg/L, DO are that 2.0～4.0mg/L, water inlet are 50mg/L for COD200mg/L, influent ammonia nitrogen.Gas-water ratio is 60: 1 o'clock in the operational process, and water outlet COD is that 25mg/L, water outlet ammonia nitrogen are that 1.0mg/L, delivery turbidity are 4NTU, and after the reactor steady running 60d, water outlet water head reaches 12cm, need carry out back flushing.Back washing strength is 3.2m
3/ (m
2* h), backwashing time is 5min.60min after the back flushing, reactor effluent quality ease down to the level before the back flushing and tend towards stability, and Dynamic Membrane is recovered fully, and reactor water outlet head is reduced to 1.5cm.
Embodiment 2:
The reactor operational conditions is basic identical with example 1 with influent quality.Gas-water ratio is 60: 1 in the operational process, and after the reactor steady running 60d, water outlet water head reaches 12cm, need carry out back flushing.Back washing strength is 3.2m
3/ (m
2* h), backwashing time is 20min.90min after the back flushing, the reactor water outlet reaches stable, and Dynamic Membrane is recovered fully, and reactor water outlet head is reduced to 0.7cm.
Embodiment 3:
The reactor operational conditions is basic identical with example 1 with Inlet and outlet water water quality.Gas-water ratio is 60: 1 in the operational process, and after the reactor steady running 60d, water outlet water head reaches 12cm, need carry out back flushing.Back washing strength is 3.2m
3/ (m
2* h), backwashing time is 12min.75min after the back flushing, the reactor water outlet reaches stable, and Dynamic Membrane is recovered fully, and reactor water outlet head is reduced to 1.0cm.
Embodiment 4:
The reactor operational conditions is basic identical with example 1 with Inlet and outlet water water quality.Gas-water ratio is 40: 1 in the operational process, and after the reactor steady running 50d, water outlet water head reaches 12cm, need carry out back flushing.Back washing strength is 8.0m
3/ (m
2* h), backwashing time is 5min.90min after the back flushing, the reactor water outlet reaches stable, and Dynamic Membrane is recovered fully, and reactor water outlet head is reduced to 0.6cm.
Embodiment 5:
The reactor operational conditions is basic identical with example 1 with Inlet and outlet water water quality.Gas-water ratio is 20: 1 in the operational process, and after the reactor steady running 40d, water outlet water head reaches 12cm, need carry out back flushing.Back washing strength is 5.6m
3/ (m
2* h), backwashing time is 5min.75min after the back flushing, the reactor water outlet reaches stable, and Dynamic Membrane is recovered fully, and reactor water outlet head is reduced to 1.1cm.
Claims (1)
1, a kind of back-flushing operation method of bioreactor of dynamic membrane, it is characterized in that, method is as follows: A, will reactor the middle part be provided with the membrane module of making by bolting silk, and aerating apparatus is installed below membrane module, by mixing sludge differential pressure action between liquid level and water outlet, through the dynamic membrane filtering water outlet, make the aerating apparatus of membrane module below, provide oxygen for the top mixed solution on the one hand, promote mixed solution to flow on the other hand, mobile increase by bubble and mixed solution is washed away and disturbance Dynamic Membrane, reaches the purpose of effective decelerating membrane pollution; B, in the bioreactor of dynamic membrane operational process, in the time of the needs back flushing, close water outlet, reversed reaction device water outlet direction is carried out aeration, makes gas enter membrane module by water outlet, the back flushing air pump provides 1.6～8.0m
3/ (m
2* gas h), the recoil time is 5～15min.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100438223A CN100558655C (en) | 2006-04-19 | 2006-04-19 | A kind of back-flushing operation method of bioreactor of dynamic membrane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100438223A CN100558655C (en) | 2006-04-19 | 2006-04-19 | A kind of back-flushing operation method of bioreactor of dynamic membrane |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1843971A CN1843971A (en) | 2006-10-11 |
| CN100558655C true CN100558655C (en) | 2009-11-11 |
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|---|---|---|---|
| CNB2006100438223A Expired - Fee Related CN100558655C (en) | 2006-04-19 | 2006-04-19 | A kind of back-flushing operation method of bioreactor of dynamic membrane |
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Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102417250B (en) * | 2011-10-10 | 2013-03-20 | 北京建筑工程学院 | Dynamic membrane purification reactor and method for removing phosphorus from regenerated water |
| CN102417273B (en) * | 2011-10-10 | 2013-06-05 | 北京建筑工程学院 | Dynamic membrane purifying reactor and method for removing ammonia nitrogen and organic matters from reclaimed water |
| CN112573623A (en) * | 2020-12-11 | 2021-03-30 | 南京信息工程大学 | Continuous dynamic membrane system operation device and working method thereof |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2310066Y (en) * | 1997-09-24 | 1999-03-10 | 天津大学 | Hollow fibre membrane biological reaction sewage treatment apparatus |
| CN2496859Y (en) * | 2001-09-07 | 2002-06-26 | 天津市津南区环保产业协会 | Sewage re-use treatment apparatus by separating bio-reaction of hollow fiber film |
| JP2003053370A (en) * | 2001-08-20 | 2003-02-25 | Mitsubishi Heavy Ind Ltd | Dynamic filter device |
| JP2003260485A (en) * | 2002-03-08 | 2003-09-16 | Kurita Water Ind Ltd | Biological treatment apparatus |
| CN1554596A (en) * | 2003-12-23 | 2004-12-15 | 南开大学 | Device and method for heavy metal waste water treatment and heavy metal recovery |
| JP2005279495A (en) * | 2004-03-30 | 2005-10-13 | Toray Ind Inc | Immersed membrane separator, washing method for diffuser, and membrane separation method |
-
2006
- 2006-04-19 CN CNB2006100438223A patent/CN100558655C/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2310066Y (en) * | 1997-09-24 | 1999-03-10 | 天津大学 | Hollow fibre membrane biological reaction sewage treatment apparatus |
| JP2003053370A (en) * | 2001-08-20 | 2003-02-25 | Mitsubishi Heavy Ind Ltd | Dynamic filter device |
| CN2496859Y (en) * | 2001-09-07 | 2002-06-26 | 天津市津南区环保产业协会 | Sewage re-use treatment apparatus by separating bio-reaction of hollow fiber film |
| JP2003260485A (en) * | 2002-03-08 | 2003-09-16 | Kurita Water Ind Ltd | Biological treatment apparatus |
| CN1554596A (en) * | 2003-12-23 | 2004-12-15 | 南开大学 | Device and method for heavy metal waste water treatment and heavy metal recovery |
| JP2005279495A (en) * | 2004-03-30 | 2005-10-13 | Toray Ind Inc | Immersed membrane separator, washing method for diffuser, and membrane separation method |
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|---|---|
| CN1843971A (en) | 2006-10-11 |
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