CN103449602A - Method of reducing salinity accumulation in forward osmosis membrane-bioreactor - Google Patents
Method of reducing salinity accumulation in forward osmosis membrane-bioreactor Download PDFInfo
- Publication number
- CN103449602A CN103449602A CN2013104204785A CN201310420478A CN103449602A CN 103449602 A CN103449602 A CN 103449602A CN 2013104204785 A CN2013104204785 A CN 2013104204785A CN 201310420478 A CN201310420478 A CN 201310420478A CN 103449602 A CN103449602 A CN 103449602A
- Authority
- CN
- China
- Prior art keywords
- membrane
- micro
- reactor
- forward osmosis
- salinity
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- 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
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention belongs to the field of water and waste water treatment and especially relates to a method of reducing salinity accumulation in forward osmosis membrane-bioreactor by extracting soluble salts via a micro-filtration membrane. The method is realized by placing the micro-filtration membrane with a single water outlet system and a conductivity controller into a reactor, and implementing in-site extraction of soluble salts in the reactor by controlling the water yield of the micro-filtration membrane so as to maintain the salinity in the forward osmosis membrane-bioreactor stable and improve the running flux of the forward osmosis membrane-bioreactor. The method is realized without need of structural improvement on the former forward osmosis membrane-bioreactor but addition of the micro-filtration membrane; the method is wide in the application scope and can be applied to the forward osmosis membrane-bioreactor for treating the waste water and also micro-polluted water, and is convenient for operation and management and easy for promotion and application.
Description
Technical field
The present invention relates to a kind ofly by microfiltration membrane, extract the method that salt assigns to alleviate salinity accumulation in forward osmosis membrane-bio-reactor, belong to water and field of waste water treatment.
Background technology
Forward osmosis membrane-bio-reactor (Osmotic Membrane Bioreactor, be called for short OMBR) be a kind of novel film-bioreactor technology, that the renewable circulating sewage that activated sludge process and forward osmosis membrane (Forward Osmosis is called for short FO) combine is processed new technology.In the FO process, the product water of film is sidelong to put and is drawn liquid, utilizes the permeable pressure head of film both sides to produce the water side for motivating force makes water flow into from stock liquid, without additional energy consumption.With traditional film-bioreactor, compare, OMBR adopts the FO film that aperture is Nano grade to replace microfiltration membrane or ultra-filtration membrane, has improved the holding back of suspended particle, mineral ion, organic pollutant and microorganism, and effluent quality is better.Because the FO film is to rely on the partial potential of film both sides to realize that the purification of sewage, the film of OMBR are polluted and energy consumption is all less.Therefore, consider the advantage of OMBR aspect sewage disposal and reuse, it has become current study hotspot.But the very important problem of OMBR is exactly to produce very high salinity accumulation in operational process at present.The high salinity accumulated in reactor can reduce effective permeable pressure head, thereby reduces effective motivating force, causes declining to a great extent of membrane flux, and simultaneously, the accumulation of salinity also can affect microorganisms, causes the OMBR operating performance to descend.
In OMBR, the accumulation of salinity is mainly efficiently holding back the solvability salt due to the reverse salt penetration of FO film and FO film.The reverse salt penetration ability of FO film is main relevant with the character of film, and material that in theory can be by the change film and the thickness of film slow down the reverse salt penetration of film, can cause reducing of membrane flux although it is so.Yet triacetate fiber at present commonly used and the FO film of polymeric amide all can not well be controlled reverse salt penetration when maintaining former flux.In addition, also can delay to a certain extent the accumulation of salinity by the sludge retention time that shortens OMBR.But too short sludge retention time is unfavorable for the growth of nitrobacteria, can affect the normal operation of OMBR.So far, also there is no a kind of method that well alleviates salinity accumulation in OMBR.Therefore, find and a kind ofly normally move under prerequisite the method that alleviates salinity accumulation and just seem particularly urgent not affecting OMBR.
Summary of the invention
Problem for salinity accumulation in above-mentioned existing OMBR, the invention provides a kind of investment low, and working cost is little, and convenient operation and management meets through engineering approaches and applies, and by microfiltration membrane, the extraction of solvability salt is used for alleviating the method for salinity accumulation in OMBR.
Because the aperture of FO film is nano level, almost solute molecule used all is trapped within reactor.In the FO operational process, the salt that draws the liquid middle and high concentration also can enter in reactor by inverse osmosis in addition.In the OMBR operational process, the unique approach that can discharge salinity is exactly the discharge of the excess sludge that carries out every day.Yet, the solute molecule that the salinity that the discharge of excess sludge brings reduces to hold back much smaller than FO and the salt of inverse osmosis, this has just caused salinity accumulation to occur at OMBR.Along with the prolongation of working time, the salinity of accumulation is more and more higher.Too high salinity can have a negative impact to the operating performance of OMBR and the activity of active sludge.The aperture of considering microfiltration membrane is micron order, can allow the salt dissolved to see through, therefore, the present invention is by place the micro-filtration membrane module of certain area in the OMBR reactor, just can realize extracting from OMBR the method for the solvability salt of different quantities by the adjustment to the microfiltration membrane water production rate.This just means, just can arbitrarily control the salinity of discharging OMBR by the variation of microfiltration membrane water production rate, thereby realizes alleviating the purpose of salinity accumulation in OMBR.
The present invention is achieved in that in conventional OMBR bio-reactor, the micro-filtration membrane module that the placement aperture is 0.1-0.4 μ m, and FO membrane module and micro-filtration membrane module are respectively equipped with independent outlet system.Conductivitimeter is set in bio-reactor and controls the switching of micro-filtration membrane water outlet pump.The effect of FO membrane module is mainly conventional filtration water outlet, and the operating parameter adopted is consistent with conventional OMBR; And micro-filtration membrane module is mainly used in the discharge of solvability salt in reactor.In the process of operation, salinity in the OMBR reactor is during higher than set(ting)value, and conductivitimeter will be opened the water pump that of microfiltration membrane, starts to discharge the high salinity water outlet, until reactor in salinity reach set(ting)value after, conductivitimeter will cut out the water pump that of microfiltration membrane.
The invention has the advantages that: micro-filtration membrane module is set in reactor the salinity of OMBR is controlled, can: 1, alleviate the accumulation of salinity in reactor, reactor is moved under stable Low-salinity condition; 2, shorten hydraulic detention time, do not change sludge retention time, be conducive to the growth of active sludge in reactor and the cultivation of nitrobacteria simultaneously.In addition, the inventive method need not be carried out structural transformation to original OMBR, has advantages of convenient operation and management and be convenient to promote.And the inventive method range of application is wider, the OMBR that both can be applied to dispose of sewage, also can be for the treatment of the OMBR of micro-polluted water.
The accompanying drawing explanation
Fig. 1 is the structural representation of realizing forward osmosis membrane-bioreactor device of the present invention.
Fig. 2 is the comparison schematic diagram of realizing that the present invention and conventional forward osmosis membrane-bio-reactor internal conductance rate change.
Fig. 3 is the comparison schematic diagram of realizing operating flux in the present invention and conventional forward osmosis membrane-bio-reactor.
In figure, pump sump 1, intake pump 2, air pump 3, bio-reactor 4, micro-filtration membrane module 5, forward osmosis membrane assembly 6, specific conductivity controller 7, draw liquid pool 8, draws liquid pump 9, goes out water pump 10.
Embodiment
The OMBR pump sump 1 that the inventive method adopts, intake pump 2, air pump 3, bio-reactor 4, micro-filtration membrane module 5, forward osmosis membrane assembly 6, specific conductivity controller 7, draw liquid pool 8, draws liquid pump 9 and go out water pump 10 compositions such as grade.Under the prerequisite that maintains the 6 normal operations of FO membrane module, when the specific conductivity in reactor 4 is greater than set(ting)value, what conductivitimeter 7 will start micro-filtration membrane module 5 goes out water pump 10, make micro-filtration membrane module 5 according to certain flux operation, the salinity of reactor 4 interior accumulation is discharged, until the specific conductivity in reactor 4 return to set(ting)value, what conductivitimeter 7 cut out micro-filtration membrane module 5 automatically goes out water pump 10, maintained the Low-salinity in reactor, thereby made the FO film can realize high-throughout steady running.
Case study on implementation
In OMBR, adopt dull and stereotyped FO film as FO membrane module 6, dull and stereotyped microfiltration membrane is as micro-filtration membrane module 5.FO membrane module 6 is the cellulose acetate material, and dull and stereotyped micro-filtration membrane module 5 is polyvinylidene difluoride (PVDF) (PVDF) material, and aperture is 0.2 μ m left and right.In addition, draw the sodium chloride solution that liquid is 1M, the effective film area of FO membrane module 6 is 0.056m
2, initial flux is 7.5L/ (m
2h); The effective film area of dull and stereotyped micro-filtration membrane module 5 is 0.060m
2, setting operating flux is 5L/ (m
2h).The aeration rate of OMBR is 0.3m
3/ h, sludge retention time is 10d, mixed solution suspension concentration is the 4g/L left and right.And processed the comparison of sanitary sewage with the OMBR of the routine that adopts dull and stereotyped FO film, investigate both changing conditions of specific conductivity (specific conductivity can characterize the size of salinity in reactor) and FO film operating flux in reactor under the operational conditions of 20 ℃.
The OMBR (reactor 2) that Fig. 2 shows the inventive method and the Conductivity Ratio of conventional OMBR (reactor 1) when processing sanitary sewage are, adopt the salinity of the reactor 2 of the inventive method to obtain good control, maintain all the time a lower concentration level.Fig. 3 shows that the OMBR (reactor 2) of the inventive method and the operating flux of conventional OMBR (reactor 1) when processing sanitary sewage compare, and the flux stabilized of the FO film of reactor 2 is at 6L/ (m
2h) left and right, be 3 times of reactor 1, this just the salinity accumulation of reactor 2 obtained the inevitable outcome of alleviating.This shows that the method that adds micro-filtration membrane module to alleviate salinity accumulation in OMBR is feasible.
Claims (6)
1. one kind alleviates by microfiltration membrane the method that in forward osmosis membrane-bio-reactor, salinity accumulates, it is characterized in that: be by micro-filtration membrane module (5) is set in forward osmosis membrane-bio-reactor (4), when the conductivity value in reactor (4) is greater than set(ting)value, what specific conductivity controller (7) will start micro-filtration membrane module (5) goes out water pump (10), make micro-filtration membrane module (5) according to certain flux operation, the solvability salt of accumulation is discharged, until the specific conductivity in reactor (4) returns to set(ting)value.
2. a kind of method that alleviates salinity accumulation by microfiltration membrane according to claim 1, it is characterized in that: forward osmosis membrane-bio-reactor (4) comprises immersion and external placed type.
3. according to claim 1 a kind of by adding microfiltration membrane to alleviate the method for salinity accumulation, it is characterized in that: micro-filtration membrane module (5) comprises various forms of microfiltration membrane, such as flat sheet membrane, hollow-fibre membrane, tubular membrane etc.
4. according to claim 1 a kind of by adding microfiltration membrane to alleviate the method for salinity accumulation, it is characterized in that: the pore diameter range of microfiltration membrane (5) is 0.1-0.4 μ m.
5. according to claim 1 a kind of by adding microfiltration membrane to alleviate the method for salinity accumulation, it is characterized in that: the switching of micro-filtration membrane water outlet pump (10) is controlled by conductivitimeter (7).
6. according to claim 1 a kind of by adding microfiltration membrane to alleviate the method for salinity accumulation, it is characterized in that: the 20%-80% that the aquifer yield of micro-filtration membrane module (5) is forward osmosis membrane assembly (6).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013104204785A CN103449602A (en) | 2013-09-17 | 2013-09-17 | Method of reducing salinity accumulation in forward osmosis membrane-bioreactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013104204785A CN103449602A (en) | 2013-09-17 | 2013-09-17 | Method of reducing salinity accumulation in forward osmosis membrane-bioreactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103449602A true CN103449602A (en) | 2013-12-18 |
Family
ID=49732504
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013104204785A Pending CN103449602A (en) | 2013-09-17 | 2013-09-17 | Method of reducing salinity accumulation in forward osmosis membrane-bioreactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103449602A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106007223A (en) * | 2016-07-15 | 2016-10-12 | 江南大学 | Forward osmosis membrane and MF (microfiltration) membrane coupling anaerobic sewage treatment method |
| CN106045035A (en) * | 2016-07-15 | 2016-10-26 | 江南大学 | Ternary sewage treatment method coupling anaerobic acidogenesis, FO (Forward Osmosis) and MFC (Microbial Fuel Cell) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009072766A (en) * | 2007-08-30 | 2009-04-09 | Toray Ind Inc | Water treating method |
| CN101786768A (en) * | 2010-03-09 | 2010-07-28 | 天津膜天膜工程技术有限公司 | Forward osmosis membrane bioreactor |
| CN102745776A (en) * | 2012-07-03 | 2012-10-24 | 上海中科高等研究院 | Method and apparatus for treatment of concentrated reverse osmosis drainage through coupled forward osmosis and reverse osmosis |
| CN103102038A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Immersion type double membrane bioreactor and salt-containing sewage treatment method |
-
2013
- 2013-09-17 CN CN2013104204785A patent/CN103449602A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009072766A (en) * | 2007-08-30 | 2009-04-09 | Toray Ind Inc | Water treating method |
| CN101786768A (en) * | 2010-03-09 | 2010-07-28 | 天津膜天膜工程技术有限公司 | Forward osmosis membrane bioreactor |
| CN103102038A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Immersion type double membrane bioreactor and salt-containing sewage treatment method |
| CN102745776A (en) * | 2012-07-03 | 2012-10-24 | 上海中科高等研究院 | Method and apparatus for treatment of concentrated reverse osmosis drainage through coupled forward osmosis and reverse osmosis |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106007223A (en) * | 2016-07-15 | 2016-10-12 | 江南大学 | Forward osmosis membrane and MF (microfiltration) membrane coupling anaerobic sewage treatment method |
| CN106045035A (en) * | 2016-07-15 | 2016-10-26 | 江南大学 | Ternary sewage treatment method coupling anaerobic acidogenesis, FO (Forward Osmosis) and MFC (Microbial Fuel Cell) |
| WO2018010217A1 (en) * | 2016-07-15 | 2018-01-18 | 江南大学 | Ternary sewage treatment method coupling anaerobic acidogenesis, forward osmosis, and microbial fuel cell |
| US10384968B2 (en) | 2016-07-15 | 2019-08-20 | Jiangnan University | Ternary sewage treatment method integrating microbial fuel cells with anaerobic acidification and forward osmosis membrane |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102372403B (en) | Treatment process of oil-containing sewage in low-permeability oil field | |
| US10384968B2 (en) | Ternary sewage treatment method integrating microbial fuel cells with anaerobic acidification and forward osmosis membrane | |
| CN103102038B (en) | Immersion type double membrane bioreactor and salt-containing sewage treatment method | |
| CN101759324A (en) | Biological filter-ceramic membrane biological reactor device and water purifying application method thereof | |
| CN101333038B (en) | Anaerobic dynamic film bio sewage treating process | |
| CN204174044U (en) | Landfill leachate treatment and recycling system | |
| CN104496129A (en) | System for deeply treating sewage in rural areas | |
| CN204058193U (en) | A kind of garbage percolation liquid treating system | |
| CN109467285A (en) | A kind of sewage plant Tailwater Depth is handled to the system and method for III class water quality standard of earth's surface | |
| CN204022592U (en) | A kind of Treated sewage reusing treatment facility | |
| CN101830597B (en) | Treatment method of printing and dying wastewater | |
| CN107188365B (en) | Method for advanced treatment of landfill leachate | |
| CN103449602A (en) | Method of reducing salinity accumulation in forward osmosis membrane-bioreactor | |
| CN202688146U (en) | Domestic sewage purifying recycling device | |
| CN209481424U (en) | A kind of sewage plant Tailwater Depth is handled to the system of III class water quality standard of earth's surface | |
| CN202576103U (en) | Aeration tank | |
| CN203728683U (en) | High-concentration organic wastewater treatment system | |
| CN202671352U (en) | Integrated aerobic granule sludge dynamic membrane bio-reaction waste water treatment device | |
| CN202744420U (en) | Novel sewage treatment device | |
| CN212610161U (en) | Full-flow treatment system for leachate of waste incineration plant | |
| CN202829779U (en) | Reclaimed water reuse system for sewage treatment | |
| CN103102048B (en) | Textile wastewater treatment method and device | |
| CN205346956U (en) | Immobilized microorganism aeration biological filtering tank | |
| CN207671865U (en) | A kind of processing system for landfill leachate treatment | |
| CN202808541U (en) | Membrane bioreactor convenient for being cleaned |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20131218 |