CN102773021A - Method for prolonging cleaning period of immersed ultra filtration membrane - Google Patents
Method for prolonging cleaning period of immersed ultra filtration membrane Download PDFInfo
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- CN102773021A CN102773021A CN2012100608342A CN201210060834A CN102773021A CN 102773021 A CN102773021 A CN 102773021A CN 2012100608342 A CN2012100608342 A CN 2012100608342A CN 201210060834 A CN201210060834 A CN 201210060834A CN 102773021 A CN102773021 A CN 102773021A
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Abstract
The invention relates to a method for prolonging the cleaning period of an immersed ultra filtration membrane, which comprises the coupling of stock solution pretreatment, cross flow, air vibration, low-power consumption ultrasonic cleaning and other methods. The method can be realized through one of the four methods or randomly combining the methods. The stock solution pretreatment method comprises pre-filtering, destabilization agent adding or the combined use of the pre-filtering and the destabilization agent adding; the cross flow method has the ratio of backflow rate to ultra filtration membrane inflow rate is (5:100)-(30:100); the air vibration method has the aeration intensity of 10-100m<3>m<minus 2>h<minus 1>, the aeration time of 1-5 minutes and the aeration interval time of 20-180 minutes; and the low-power consumption ultrasonic cleaning method has the ultrasonic power of 10-50kHz, the ultrasonic sound intensity of 10-80Wm<minus 2>, the ultrasonic duration of 1-5 minutes and the ultrasonic interval time of 20-180 minutes.
Description
Technical field
The present invention relates to a kind of method that prolongs the submerged ultrafiltration cleaning frequency, be meant especially, a kind of method that prolongs the submerged ultrafiltration cleaning frequency of using in the drinking water treatment.
Background technology
The membrane separating method that with the polymeric membrane for separation is representative is to use more separation method in the engineering fields such as current chemical industry, food, water treatment as a kind of novel fluid separation element method of operating.Wherein, the film pollution is the key factor of restriction film method large-scale application.In engineering of water treatment,, cause film to pollute more easily and influence the long-term stability of film unit in engineering and move because pollutant component complicacy, character differ in the water source.
Film pollutes and be meant that some component in the feed liquid deposits in film surface or fenestra, the phenomenon that causes film infiltration flow rate to descend.The duct that comprises film is increased by big molecule solute obstruction causing resistance of membrane filtration; Solute is inwall absorption in the hole; Face forms gel layer and increases resistance to mass tranfer.When film polluted extremely to a certain degree, film unit just was difficult to normally move and guarantee treatment effect.At this moment, must in time clean to ensure its normal operation film.But then, frequent film cleaning operation is with the time and the energy of labor, and the system that influences normally moves.Therefore, effectively alleviate film pollute, prolong the film cleaning frequency be promote film method in engineering large-scale application need one of key issue of solution badly.
At present, the pollution of alleviation controlling diaphragm, the method for prolongation film cleaning frequency mainly contain: select suitable pollution-resistant membrane material; Select the film in suitable aperture; Material liquid is carried out preliminary treatment; Design resistant to pollution membrane module etc.In addition, introducing the intensive filtration measure also is the effective means that controlling diaphragm pollutes.Common intensive filtration measure comprise adopt utilize that the cross-flow filtration mode is improved the hydrodynamics condition of face, biphase gas and liquid flow method, strengthened, the selection of other operating conditions etc.
Material liquid is carried out preliminary treatment be meant that filtering forward direction in stoste wherein adds suitable medicament, changing the character of feed liquid or solute, or it is flocculated, filters, removing some suspended particulates or colloid substance, thereby alleviate the load and the pollution of membrane process.The selection of pretreatment mode should be carried out according to the character of feed liquid and the character of film material.For containing suspended particulates, jelly or organic feed liquid, can adopt methods such as sand filtration pre-filtering or dosing coagulant, flocculant, Powdered Activated Carbon, microorganism.
The cross-flow filtration method is to improve a kind of method of face hydrodynamics condition.Feed liquid is from film surface current mistake; Can play the effect of sluicing to the film surface of influent side, form certain shearing force, can make the particulate Returning fluid main body that has deposited on the surface of film; Reduce face fluid boundary layer thickness; Reduce concentration polarization, delay the formation of gel layer, reduce film and pollute.
The biphase gas and liquid flow method is meant in the membrane filtration process continuously or tangential air stream intermittently, to produce high shear force and fluid instability, stops particle on the film surface, to deposit, thereby reaches stable filter operation, improves the purpose of filter efficiency.
Low power ultrasound ripple cleaning method is meant mechanical oscillation and the microturbulence phenomenon of utilizing ultrasonic wave in water, to produce, and polluter is broken away from from the film surface, to reach the development of control concentration polarization, improves the diactinic purpose of film.
Above-mentioned the whole bag of tricks can alleviate or alleviate the film pollution in varying degrees, prolongs film operation and cleaning frequency.Problems such as but said method exists cleaning insufficient, and the film pollution level is still higher, and the cleaning frequency is short.
The present invention proposes the method for a kind of efficient prolongation submerged ultrafiltration cleaning frequency; This method is introduced processes such as stoste preliminary treatment, small throughput, cross-flow, air vibration, low frequency ultrasonic wave in the film system; And through coupling between the method and synergy effect; The pollutant that promotes efficiently to hold back in the membrane filtration processes is from film surfacial spalling, disengaging and desorb, thereby keeps membrane superficial tissue and through performance for a long time surely, reaches the requirement of abundant prolongation film cleaning frequency.
Summary of the invention
The purpose of this invention is to provide a kind of method that film pollutes, prolongs the milipore filter cleaning frequency of alleviating.
The method scheme that the present invention taked is following:
The method of prolongation submerged ultrafiltration cleaning frequency provided by the invention comprises one of stoste preliminary treatment, small throughput operation, cross-flow, air vibration, the cleaning of low power ultrasound ripple or any one above combination; Be able to prolong the milipore filter cleaning frequency through said method and Combination application thereof.
Described stoste preliminary treatment comprises and adds that coagulant is handled and/or pre-filtering is handled; When employing simultaneously adds coagulant processing and pre-filtering processing, add coagulant and handled before pre-filtering is handled;
Adding coagulant handles to refer to through adding the pollutant that macromolecule and the coagulant identical with the film surface electrical behavior promote milipore filter to hold back and comes off from the film surface;
Described coagulant is meant ferric trichloride, ferric sulfate, aluminum sulfate, aluminium chloride, aluminium polychloride, polymeric ferric aluminum, polymeric aluminium ferrum silicate, potassium permanganate, activated silicic acid, polyacrylamide and/or Powdered Activated Carbon; Wherein, the throwing weight range of ferric trichloride, ferric sulfate, aluminum sulfate, aluminium chloride, aluminium polychloride, polymeric ferric aluminum, polymeric aluminium ferrum silicate is to make that the throwing amount of aluminium and/or iron is 0～20mgL
-1It is 0～2.0mgL that potassium permanganate is thrown weight range
-1, it is 0～10mgL that activated silicic acid is thrown weight range
-1, it is 0～0.15mgL that polyacrylamide is thrown weight range
-1, it is 0～150mgL that Powdered Activated Carbon is thrown weight range
-1
Described pre-filtering is handled and is meant pending current through the granule filter material layer;
Described filtrate is meant quartz sand, zeolite, haydite, granular activated carbon, manganese sand, anthracite or magnetic iron ore; The particle diameter of filter medium scope is 0.4mm～2mm, and the depth of packing scope is 0.50m～1.5m; Current through the filtering velocity scope of filtering reactor between 2m/h～15m/h;
Described small throughput operation is meant milipore filter operating flux scope is controlled at 15Lm
-2H
-1～25Lm
-2H
-1Between, thereby reduce osmotic pressure, reduce the absorption of solute at film surface holes inwall to film, help the disengaging of attachment;
The filtration water yield that described membrane flux is meant the elementary membrane area, passes through in the unit interval.
Described cross-flow is meant being back to the stoste porch by certain reflux ratio continuously through processing or undressed concentrate, makes the film end still keep certain surface velocity to suppress particle at the surperficial cake layer that forms of film to reduce through hydraulic action;
Described concentrate is meant the suspension that does not see through milipore filter that milipore filter is held back; Described reflux ratio is meant the ratio of return flow and membrane cisterna flow of inlet water; The reflux ratio scope is 5: 100～30: 100.
Described air vibration is meant in membrane stack bottom or side lays aerator; Aerator will get into membrane stack after will having the air of pressure through boring aeration pipe or aeration head aeration continuously or intermittently; Gas ducks in drink, and rising flows causes the vibration of ambient water, and washes away the film surface through the hydraulic shear effect;
Wherein, aeration intensity is 10～100m3m-2h-1, and aeration time is 1～5min, and the aeration intermittent time is 0～180min.
Described low-power consumption ultrasonic waves for cleaning is characterized in that, lays the low-power consumption supersonic generator in membrane cisterna bottom or side, and the low-power consumption supersonic generator carries out ultrasonic to membrane stack continuously or intermittently; The ultrasonic frequency scope is 10～50kHz, and ultrasonic wave sound intensity scope is 10～80Wm-2, the ultrasonic 1～5min that is lasted for, and the ultrasonic intermittent time is 20～180min.
The method effect that the present invention realizes is following:
1, the method for the prolongation submerged ultrafiltration cleaning frequency that the present invention relates to, wherein stoste preliminary treatment, small throughput operation, cross-flow, air vibration and low-power consumption ultrasonic wave can be realized in same reactor.
2, the method for the prolongation submerged ultrafiltration cleaning frequency that the present invention relates to; Can be directed against characteristics such as pending raw water quality, water supply scale, select one or more the combined method in stoste preliminary treatment, small throughput operation, cross-flow, air vibration, the low-power consumption ultrasonic method to use neatly.
3, the method for the prolongation submerged ultrafiltration cleaning frequency that the present invention relates to can alleviate film effectively and pollute, and prolong hyperfiltration membrane assembly physics and clean and the Chemical cleaning cycle, and prolongation milipore filter service life.
4, the method for the prolongation submerged ultrafiltration cleaning frequency that the present invention relates to can reach the prolongation cleaning frequency, is substituted in the purpose of linearize cleaning process, thereby improves the producing water ratio of film system.
Description of drawings
Fig. 1 is that the realization that the present invention relates to prolongs the reactor of submerged ultrafiltration cleaning frequency method
Reference numeral:
1. coagulant adds pipe 2. return lines 3. aerating pipelines
4. supersonic generator 5. submerged ultrafiltrations 6. film outlet pipelines
The specific embodiment
Embodiment 1:
Submerged ultrafiltration filters certain water factory's sedimentation basin water outlet, and the membrane cisterna influent turbidity is 2.87-3.24NTU, COD
MnContent is 2.89-3.04mgL
-1, water temperature is 15.5-16.8 ℃, membrane flux is 25Lm
-2H
-1Do not add coagulant in the water, reflux ratio is 10%, and aeration intensity is 45m
3M
-2H
-1, aeration time is 3min, and the aeration intermittent time is 30min, and ultrasonic and aeration carries out simultaneously, and the ultrasonic wave power consumption is 40kHz, the sound intensity is 50Wm
-2Behind the film operation 150h, flux is reduced to 10Lm
-2H
-1, descend 60%.At this moment, stop to filter, film is cleaned blowdown.
Embodiment 2:
Submerged ultrafiltration filters certain water factory's sedimentation basin water outlet, and the membrane cisterna influent turbidity is 2.79-3.12NTU, COD
MnContent is 2.91-3.14mgL
-1, water temperature is 14.5-17.2 ℃, membrane flux is 25Lm
-2H
-1Do not add coagulant in the water, reflux ratio is 10%, and aeration intensity is 45m
3M
-2H
-1, aeration time is 3min, and the aeration intermittent time is 30min, and ultrasonic wave does not adopt.Behind the film operation 90h, flux is reduced to 10Lm
-2H
-1, descend 60%.At this moment, stop to filter, film is cleaned blowdown.
Embodiment 3:
Submerged ultrafiltration filters certain water factory's sedimentation basin water outlet, and the membrane cisterna influent turbidity is 2.85-3.37NTU, COD
MnContent is 2.69-2.97mgL
-1, water temperature is 16.5-17.2 ℃, membrane flux is 30Lm
-2H
-1Do not add coagulant in the water, reflux ratio is 10%, does not adopt aeration, and the ultrasonic wave power consumption is 40kHz, and the sound intensity is 50Wm
-2, the ultrasonic intermittent time is 30min.Behind the film operation 60h, flux is reduced to 15Lm
-2H
-1, descend 50%.At this moment, stop to filter, film is cleaned blowdown.
Embodiment 4:
Submerged ultrafiltration filters certain water factory's sedimentation basin water outlet, and the membrane cisterna influent turbidity is 2.76-3.09NTU, COD
MnContent is 2.78-3.01mgL
-1, water temperature is 14.6-16.7 ℃, membrane flux is 25Lm
-2H
-1Do not add coagulant in the water, reflux ratio is 0, and aeration intensity is 45m
3M
-2H
-1, aeration time is 3min, and the aeration intermittent time is 30min, and ultrasonic and aeration uses simultaneously, and the ultrasonic wave power consumption is 40kHz, the sound intensity is 50Wm
-2Behind the film operation 90h, flux is reduced to 10Lm
-2H
-1, descend 60%.At this moment, stop to filter, film is cleaned blowdown.
Embodiment 5:
The contaminated former water of submerged ultrafiltration Direct Filtration, the membrane cisterna influent turbidity is 10.59-12.75NTU, COD
MnContent is 5.83-6.24mgL
-1, water temperature is 17.0-17.8 ℃, membrane flux is 25Lm
-2H
-1Do not add coagulant in the water, reflux ratio is 0, and aeration intensity is 45m
3M
-2H
-1, aeration time is 3min, and the aeration intermittent time is 15min, and ultrasonic and aeration carries out simultaneously, and the ultrasonic wave power consumption is 40kHz, the sound intensity is 30Wm
-2Behind the film operation 72h, flux is reduced to 10Lm
-2H
-1, descend 60%.At this moment, stop to filter, film is cleaned blowdown.
Embodiment 6:
The contaminated former water of submerged ultrafiltration Direct Filtration, the membrane cisterna influent turbidity is 10.32-11.78NTU, COD
MnContent is 5.34-6.17mgL
-1, water temperature is 16.8-17.3 ℃, membrane flux is 25Lm
-2H
-1Do not add coagulant in the water, reflux ratio is 10%, and aeration intensity is 45m
3M
-2H
-1, aeration time is 3min, and the aeration intermittent time is 15min, and ultrasonic and aeration carries out simultaneously, and the ultrasonic wave power consumption is 40kHz, the sound intensity is 40Wm
-2Behind the film operation 96h, flux is reduced to 10Lm
-2H
-1, descend 60%.At this moment, stop to filter, film is cleaned blowdown.
Embodiment 7:
Submerged ultrafiltration filters contaminated former water, and the membrane cisterna influent turbidity is 13.45-15.73NTU, COD
MnContent is 5.21-6.75mgL
-1, water temperature is 15.0-15.9 ℃, membrane flux is 25Lm
-2H
-1Add 5mgL in the water
-1Ferric trichloride, reflux ratio are 0, and aeration intensity is 45m
3M
-2H
-1, aeration time is 3min, and the aeration intermittent time is 15min, and ultrasonic and aeration carries out simultaneously, and the ultrasonic wave power consumption is 40kHz, the sound intensity is 30Wm
-2Behind the film operation 80h, flux is reduced to 15Lm
-2H
-1, descend 40%.At this moment, stop to filter, film is cleaned blowdown.
Embodiment 8:
Submerged ultrafiltration filters contaminated former water, and the membrane cisterna influent turbidity is 11.23-13.20NTU, COD
MnContent is 4.89-5.74mgL
-1, water temperature is 16.2-17.4 ℃, membrane flux is 25Lm
-2H
-1Add 5mgL in the water
-1Ferric trichloride, reflux ratio are 10%, and aeration intensity is 45m
3M
-2H
-1, aeration time is 3min, and the aeration intermittent time is 15min, and ultrasonic and aeration carries out simultaneously, and the ultrasonic wave power consumption is 40kHz, the sound intensity is 50Wm
-2Behind the film operation 120h, flux is reduced to 10Lm
-2H
-1, descend 60%.At this moment, stop to filter, film is cleaned blowdown.
Embodiment 9:
Submerged ultrafiltration filters contaminated former water, and the membrane cisterna influent turbidity is 9.53-11.21NTU, COD
MnContent is 4.78-5.37mgL
-1, water temperature is 15.8-17.2 ℃, membrane flux is 25Lm
-2H
-1Add 5mgL in the water
-1Ferric trichloride, reflux ratio are 10%, and aeration intensity is 45m
3M
-2H
-1, aeration time is 3min, and the aeration intermittent time is 30min, and ultrasonic and aeration carries out simultaneously, and ultrasonic frequency is 40kHz, the sound intensity is 40Wm
-2Behind the film operation 90h, flux is reduced to 10Lm
-2H
-1, descend 60%.At this moment, stop to filter, film is cleaned blowdown.
Embodiment 10:
Submerged ultrafiltration filters contaminated former water, and the membrane cisterna influent turbidity is 12.13-15.47NTU, COD
MnContent is 4.88-5.85mgL
-1, water temperature is 17.8-19.6 ℃, membrane flux is 25Lm
-2H
-1Dosing coagulant not in the water, reflux ratio is 10%, aeration intensity is 45m
3M
-2H
-1, aeration time is 3min, and the aeration intermittent time is 30min, and ultrasonic wave does not adopt.Behind the film operation 48h, flux is reduced to 10Lm
-2H
-1, descend 60%.At this moment, stop to filter, film is cleaned blowdown.
Claims (6)
1. a method that prolongs the submerged ultrafiltration cleaning frequency is characterized in that, comprises one of stoste preliminary treatment, small throughput operation, cross-flow, air vibration and/or low-power consumption ultrasonic waves for cleaning or any one above combination.
2. stoste preliminary treatment according to claim 1 comprises adding coagulant processing and/or pre-filtering processing; When employing simultaneously adds coagulant processing and pre-filtering processing, add coagulant and handled before pre-filtering is handled;
Described coagulant is meant ferric trichloride, ferric sulfate, aluminum sulfate, aluminium chloride, aluminium polychloride, polymeric ferric aluminum, polymeric aluminium ferrum silicate, potassium permanganate, activated silicic acid, polyacrylamide and/or Powdered Activated Carbon; Wherein, the throwing weight range of ferric trichloride, ferric sulfate, aluminum sulfate, aluminium chloride, aluminium polychloride, polymeric ferric aluminum, polymeric aluminium ferrum silicate is to make that the throwing amount of aluminium and/or iron is 0～20mgL
-1It is 0～2.0mgL that potassium permanganate is thrown weight range
-1, it is 0～10mgL that activated silicic acid is thrown weight range
-1, it is 0～0.15mgL that polyacrylamide is thrown weight range
-1, it is 0～150mgL that Powdered Activated Carbon is thrown weight range
-1
Described pre-filtering is handled and is meant pending current through the granule filter material layer;
Described filtrate is meant quartz sand, zeolite, haydite, granular activated carbon, manganese sand, anthracite or magnetic iron ore; The particle diameter of filter medium scope is 0.4mm～2mm, and the depth of packing scope is 0.50m～1.5m; Current through the filtering velocity scope of filtering reactor between 2m/h～15m/h;
3. small throughput operation according to claim 1 is characterized in that, milipore filter operating flux scope is controlled at 15～25Lm
-2H
-1Between.
4. cross-flow according to claim 1 is meant process processing or undressed concentrate is back to the stoste porch continuously that the reflux ratio scope is 5: 100～30: 100;
Described concentrate is meant the suspension that does not see through milipore filter that milipore filter is held back; Described reflux ratio is meant the ratio of return flow and membrane cisterna flow of inlet water.
5. air vibration according to claim 1 is meant in membrane cisterna bottom or aerator is laid in the side, and aerator is aeration continuously or intermittently; Aeration intensity is 10～100m
3M
-2H
-1, aeration time is 1～5min, the aeration intermittent time is 0～180min.
6. low-power consumption ultrasonic waves for cleaning according to claim 1 is characterized in that, lays the low-power consumption supersonic generator in membrane cisterna bottom or side, and the low-power consumption supersonic generator carries out ultrasonic to membrane stack continuously or intermittently; The ultrasonic frequency scope is 10～50kz, and ultrasonic wave sound intensity scope is 10～80Wm
-2, the ultrasonic 1～5min that is lasted for, the ultrasonic intermittent time is 20～180min.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100608342A CN102773021A (en) | 2012-03-09 | 2012-03-09 | Method for prolonging cleaning period of immersed ultra filtration membrane |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100608342A CN102773021A (en) | 2012-03-09 | 2012-03-09 | Method for prolonging cleaning period of immersed ultra filtration membrane |
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|---|---|
| CN102773021A true CN102773021A (en) | 2012-11-14 |
Family
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|---|---|---|---|
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104524980A (en) * | 2014-11-28 | 2015-04-22 | 北京碧水源膜科技有限公司 | Membrane element post-treatment system and method |
| CN104667862A (en) * | 2013-11-28 | 2015-06-03 | 沈阳市天泉水处理设备有限责任公司 | Filter material and preparation method and using method thereof |
| CN105347506A (en) * | 2015-11-14 | 2016-02-24 | 常州大学 | Method for reducing membrane pollution of immersed membrane bioreactor |
| CN112337884A (en) * | 2020-10-15 | 2021-02-09 | 郑州恒博环境科技股份有限公司 | Automatic cleaning device for pH meter of aluminum processing waste emulsion treatment system and control method |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104667862A (en) * | 2013-11-28 | 2015-06-03 | 沈阳市天泉水处理设备有限责任公司 | Filter material and preparation method and using method thereof |
| CN104667862B (en) * | 2013-11-28 | 2017-07-28 | 沈阳市天泉水处理设备有限责任公司 | A kind of filtrate and preparation method thereof and application method |
| CN104524980A (en) * | 2014-11-28 | 2015-04-22 | 北京碧水源膜科技有限公司 | Membrane element post-treatment system and method |
| CN105347506A (en) * | 2015-11-14 | 2016-02-24 | 常州大学 | Method for reducing membrane pollution of immersed membrane bioreactor |
| CN105347506B (en) * | 2015-11-14 | 2017-10-24 | 哈尔滨工业大学环境股份有限公司 | A kind of method of fouling membrane in mitigation Nets impregnated |
| CN112337884A (en) * | 2020-10-15 | 2021-02-09 | 郑州恒博环境科技股份有限公司 | Automatic cleaning device for pH meter of aluminum processing waste emulsion treatment system and control method |
| CN112337884B (en) * | 2020-10-15 | 2023-10-27 | 郑州恒博环境科技股份有限公司 | Automatic cleaning device for pH meter of aluminum processing waste emulsion treatment system and control method |
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Application publication date: 20121114 |