CN102001796A - Novel membrane bioreactor and treatment process thereof for industrial waste - Google Patents
Novel membrane bioreactor and treatment process thereof for industrial waste Download PDFInfo
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- CN102001796A CN102001796A CN 201010575807 CN201010575807A CN102001796A CN 102001796 A CN102001796 A CN 102001796A CN 201010575807 CN201010575807 CN 201010575807 CN 201010575807 A CN201010575807 A CN 201010575807A CN 102001796 A CN102001796 A CN 102001796A
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Abstract
The invention discloses the treatment process for industrial waste of a membrane bioreactor, which comprises two stages: 1, a stage of continuous filling and pumping and aeration, in which water is filled in and pumped out from the membrane bioreactor continuously while aeration is performed, and after operation for a certain period, the membrane bioreactor enters other stage; and 2, a stage of aeration, in which water filling and pumping are stopped, aeration is continued, fine gas flow formed by aeration flushes the membrane of a membrane component in the membrane bioreactor, and after operating for a certain period in the stage, the membrane bioreactor operates again in the first stage. As the aeration process is performed, the gas flow formed by the aeration can flush the membrane and relieve membrane pollution and has obvious effects on the recovery of membrane flux. The invention also discloses a novel membrane bioreactor (MBR), which has an air distribution pipe the conventional MBR lacks; and the air distribution holes on the air distribution pipe realize aeration.
Description
Technical field
The present invention relates to a kind of Industrial Wastewater Treatment equipment and treatment process, refer to a kind of new membrane bio-reactor and the treatment process in trade effluent thereof especially.
Background technology
Membrane bioreactor (MBR) is a kind of new technology that membrane separation technique combines with bio-reactor.Membrane separation technique is exactly the technological method that utilizes certain special semi-permeable membranes that the heterogeneity in the liquid is carried out selective separation, concentrated or purify, and is a kind of of materilization freatment method.Bio-reactor is the technological method that utilizes the microorganism in the active sludge that the organic pollutant in the waste water is degraded and disposed of sewage to reach.Therefore, membrane bioreactor is a kind of typical combination of biochemical treatment process and materilization freatment method.American scholar combined activated sludge process and be applied to membrane separation technique the removal of organic pollutant in the waste water at first the sixties in 20 century, membrane bioreactor can prolong the sewage sludge solid residence time effectively with it subsequently, and the characteristics that increase sludge concentration have caused water treatment field scholar's extensive concern.
Bio-reactor and membrane module have special separately function: 1. in bio-reactor degrading organic pollutant by microbiological degradation; 2. microorganism is trapped in the waste water during membrane module filtered wastewater, film constitutes physical barriers one to suspended particle, makes active sludge not had suspended particle, bacterium and virus by bio-reactor recycle and water outlet.
Membrane module divides two kinds of Configuration Types: built-in and external placed type.The filtration of external placed type is under pressure, and membrane module filters mixed solution; Built-in membrane module then is immersed in the aeration tank, by suction function waste water is filtered.The membrane flux of external membrane bioreactor is generally at 50-120L/ (hm
2), transmembrane pressure is between 1-4bar.The permeation flux of built-in membrane bioreactor is at 10-50L/ (hm
2), transmembrane pressure approximately is 0.5bar.Owing to do not need recycle pump, aeration generates a tangential mobile liquid membrane, and operational conditions is comparatively simple, and it is lower to stride membrane resistance value and tangential velocity, and built-in membrane bioreactor energy consumption is relatively low.
Membrane bioreactor is than the advantage of traditional active sludge treatment system: 1. traditional second pond is replaced by membrane module.The membrane module structure compactness, and the sludge settling speed of stable water flow quality and variation is irrelevant.2. the membrane bioreactor microbial biomass that can carry is than traditional treatment system height.People such as Jefferson utilize the biomass of 20g/L to handle waste water; People such as Yamamoto utilize 30g/L to handle.And the biomass concentration of traditional technology utilization is less than 5g/L to avoid the concentrated sedimentation of biological floe.Except avoiding biological floe to concentrate sedimentation, the MBR biological degradation is more thorough, and processing efficiency is higher.But, people such as Lubbecke point out, increase biological concentration and can cause reducing of oxygen transfer speed, and this have depend on the type of the waste water of handling and reactor.The advantage of membrane bioreactor others is:
1, because the biomass of high density can rest in the reactor, the aeration tank capacity also can correspondingly reduce.
2, the disposal of mud acquires a certain degree of difficulty, and sludge yield reduces 2-3 doubly, thereby has reduced running cost.
3, membrane bioreactor widespread use in Industrial Wastewater Treatment because waste water can directly be handled at the scene, utilizes water again, reduces water consumption, thereby reduces manufacturing cost.
Different with traditional activated sludge process, membrane bioreactor utilizes membrane sepn, be trapped in all biologies in the bio-reactor fully, thereby control and prolonged sludge retention time, make sludge retention time not influenced by hydraulic detention time, high sludge retention time has increased mud and has concentrated and organic loading, has therefore improved the degradation rate of pollutent.
The structural representation of conventional film bio-reactor (board-like film) as shown in Figure 1, it is provided with membrane module 2 within tank 1, this membrane module 2 comprises sheet frame 21 and is arranged on some filtration lamina membranaceas 22 on the sheet frame 21, filters lamina membranacea 22 and is provided with two diaphragms, forms the dialyzate passage between two diaphragms.Below tank 1, be provided with the water inlet pipe 3 that communicates with tank, the top be provided with filter that lamina membranacea 22 inner dialyzate passages communicate give water pipe 4.Bottom at tank 1 also is provided with aeration tube 5, and this aeration tube 5 is provided with some solarization air caps, and this aeration tube 5 links to each other with an air pump (not shown).The below of described tank 1 also is provided with a shore pipe 6.
The operational process of described membrane bioreactor is: put into active sludge in tank 1, intake continuously and continuous pumpage in tank 1 then, open air pump simultaneously and carry out aeration.In operational process, the microorganism in the active sludge can be degraded to the organic pollutant in the waste water, and the waste water after the degraded sees through the diaphragm that filters on the lamina membranacea 22 again and carries out filtering separation, and the gained dialyzate is discharged from rising pipe 4.The effect of aeration is to make that active sludge is more uniform to be riddled in the tank, rather than is deposited in bottom of gullet, and microorganism is fully contacted with sewage, obtains better treatment effect.
If the operation scheme succession running of conventional film bio-reactor, diaphragm pollutes comparatively serious, and membrane flux descends very fast, often change the filtration lamina membranacea.For this reason, conventional film bio-reactor operation scheme mostly is intermittent suction formula or intermittent aeration formula etc., in intermittent process, can alleviate film to a certain extent and pollute, but the decline of membrane flux still comparatively obviously and do not have a recovery.
And the conventional film bio-reactor does not have good effect in denitrogenation dephosphorizing, especially in high density used water difficult to degradate such as dyeing waste water are handled, the removal of total nitrogen is difficult to reach emission standard especially.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of new membrane bio-reactor and the treatment process in trade effluent thereof, this treatment process and novel membrane bioreactor can be alleviated film and pollute, membrane flux to a certain degree is being restored, with the work-ing life of membrane component and prolong down.
Another technical problem to be solved by this invention is to provide the treatment process of a kind of membrane bioreactor in trade effluent, this treatment process can improve the processing efficiency of high density used water difficult to degradate such as handling printing and dyeing mill's waste water, factory's finishing waste water, improve nitrogen removal rate, make effluent quality reach the recirculated cooling water standard, realize sewage recycling.
For solving the problems of the technologies described above, technical solution of the present invention is:
The treatment process of a kind of membrane bioreactor in trade effluent comprises following two stages:
One, be back to back water and aeration phase:
In membrane bioreactor, intake continuously and continuous pumpage, carry out aeration simultaneously, enter next stage after operation for some time;
Two, sky exposes to the sun the stage:
Close Inlet and outlet water, continue aeration, aeration forms tiny air-flow the diaphragm of membrane module in the membrane bioreactor is washed away, and this stage repeats the fs after moving for some time.
The treatment process of a kind of membrane bioreactor in trade effluent comprises following three phases:
One, be back to back water and aeration phase:
In membrane bioreactor, intake continuously and continuous pumpage, carry out aeration simultaneously, enter next stage after operation for some time;
Two, the anoxic stage:
Close Inlet and outlet water and aeration, make active sludge be in anoxic condition, repeat the fs after operation for some time.
Three, sky exposes to the sun the stage:
Open aeration, make the diaphragm of membrane module in the formed airflow scouring membrane bioreactor of aeration, repeat the fs after operation for some time.
The described sky stage of exposing to the sun is carried out the sky aeration by the original aeration tube of membrane bioreactor.
The optimum operation duration of described three phases is: be back to back water and aeration phase 120-180 minute, in 60-120 minute anoxic stage, sky exposed to the sun stage 10-30 minute.
A kind of new membrane bio-reactor is provided with membrane module within tank, membrane module comprises the dialyzate passage that forms in diaphragm and the diaphragm; Be provided with the water inlet pipe that communicates with tank below tank, the top is provided with the water pipe that gives that communicates with the dialyzate passage; The bottom of tank also is provided with aeration tube, and this aeration tube is provided with some solarization air caps; Increasing in the described tank has gas distribution pipe, has some qi-emitting holes on this gas distribution pipe, and this qi-emitting hole is positioned at diaphragm-operated below or side.
The described sky stage of exposing to the sun is carried out the sky aeration by described gas distribution pipe.
After adopting such scheme, treatment process of the present invention is compared with traditional MBR treatment process, has the following advantages:
1. technology of the present invention has increased the sky process of exposing to the sun, and forms the intermittent type Inlet and outlet water on the one hand, makes that membrane flux can keep stablizing in longer for some time; The empty on the other hand air-flow that forms that exposes to the sun can wash away diaphragm, makes the part pollutent break away from diaphragm, and the recovery of membrane flux is had obvious effect, and whole process membrane flux rate of descent is 10.9%, and average flux is 9.58L/ (hm
2);
2.MBR added a gas distribution pipe in the equipment below diaphragm, effect is to add the sky process of exposing to the sun, and makes diaphragm under the washing away of tiny bubble, pollution is eased, and flux is restored.
3. technology of the present invention also can add the anoxic process, make the microorganism in the active sludge have suitable condition and time to carry out nitrification and denitrification, can improve nitrogen removal rate, the no anoxic process TN clearance of tradition only is 63.1%, and this technology TN clearance can reach 80.2%, therefore adopt the processing efficiency that should treatment process can improve high density used water difficult to degradate such as handling printing and dyeing mill's waste water, factory's finishing waste water, make effluent quality reach the recirculated cooling water standard, realize sewage recycling.
4. be example with the dyeing waste water, because MBR poor effect aspect waste water decoloring, the water outlet after MBR handles can be passed through little electrolysis again, colourity can be removed substantially fully, and through after the combined treatment, the COD clearance can reach more than 96%, and the TN clearance can reach more than 90%.
Description of drawings
Fig. 1 is the structural representation of conventional film bio-reactor (board-like film);
Fig. 2 is the treatment process first embodiment schema of the present invention;
Fig. 3 is the structural representation of membrane bioreactor of the present invention;
Fig. 4 is the treatment process second embodiment schema of the present invention;
Fig. 5 is that the present invention adopts the described method sampling of second embodiment to record the COD clearance of each time point;
Fig. 6 is that the present invention adopts the described method sampling of second embodiment to record the TN clearance of each time point;
Fig. 7 is the TN clearance that the sampling of conventional film bio-reactor operation scheme records each time point;
Fig. 8 is that the membrane flux that the present invention adopts the described method sampling of second embodiment to record each time point changes;
Fig. 9 is the membrane flux variation that the sampling of conventional film bio-reactor operation scheme records each time point.
Embodiment
The invention will be further described below in conjunction with the drawings and specific embodiments.
Disclosed is the treatment process of a kind of membrane bioreactor in trade effluent, as shown in Figure 2, be the flow process of the present invention's first preferred embodiment.Described treatment process can adopt traditional membrane bioreactor, and the structure of conventional film bio-reactor can be referring to as shown in Figure 1 and referring to background technology, and its treatment process comprises following two stages:
One, be back to back water and aeration phase:
In membrane bioreactor, intake continuously and continuous pumpage, carry out aeration with seasonal aeration tube.This stage is carried out biochemical treatment to waste water, carries out physical sepn simultaneously, and the gained dialyzate is discharged from rising pipe 4.Enter next stage after this operation for some time in stage.
Two, sky exposes to the sun the stage:
Close Inlet and outlet water, continue aeration, in this sky exposed to the sun the stage, aeration formed tiny air-flow and can wash away the diaphragm that filters lamina membranacea 22 down, makes the part pollutent break away from diaphragm, makes film pollute and is eased, and membrane flux obtains recovery to a certain degree.Repeat the fs after this operation for some time in stage.
This sky stage of exposing to the sun can be finished by the aeration tube 5 of membrane bioreactor, promptly opens the aeration air pump, makes the airflow scouring diaphragm of the solarization air cap formation of aeration tube 5, alleviates the effect of polluting to reach.Yet because the main effect of aeration tube is in order to stir active sludge, so the solarization air cap aperture of offering on it is bigger, uses aeration tube to carry out sky and exposes to the sun and wash away diaphragm, and effect is bad, and for this reason, the present invention can adopt following follow-on membrane bioreactor.
As shown in Figure 3, be the follow-on membrane bioreactor of the present invention, described membrane bioreactor is compared with traditional MBR, increasing has gas distribution pipe 7, have some tiny qi-emitting holes on this gas distribution pipe 7, the position of this qi-emitting hole can be arranged on the below of filtering lamina membranacea 22, also can be arranged on the side of filtering profile 22.This gas distribution pipe 7 links to each other with an air pump in addition, described air pump can be same air pump with the air pump that is connected aeration tube 5, also can be independent air pump, if gas distribution pipe 7 and aeration tube 5 shared air pumps need to be provided with Y-tube so and valve be set so that switch between two pipelines.Other structure of described membrane bioreactor is all identical with conventional film bio-reactor shown in Figure 1 with label.
Described membrane bioreactor increases after the gas distribution pipe 7, can be independent of aeration tube 5 and carry out sky and expose to the sun, and that is to say, exposes to the sun the stage at sky, closes Inlet and outlet water and closes aeration tube simultaneously, makes gas distribution pipe carry out sky exposing to the sun and open gas distribution pipe 7.Because gas distribution pipe 7 is the pipelines that are independent of aeration tube 5, on it less qi-emitting hole can be set, and can increase and wash away strength, and gas distribution pipe 7 can be arranged at diaphragm-operated below or side, more close diaphragm, scouring effect is better, can increase the recovery rate of membrane flux.
As shown in Figure 4, be the schema of the method for the invention second preferred embodiment.The membrane bioreactor that the described treatment process of present embodiment adopts is follow-on as shown in Figure 3 structure.
Present embodiment the treating method comprises following three phases:
One, be back to back water and aeration phase:
In membrane bioreactor, intake continuously and continuous pumpage, open the aeration air pump simultaneously and make aeration tube carry out aeration.This stage is carried out biochemical treatment to waste water, carries out physical sepn simultaneously, and the gained dialyzate is discharged from rising pipe 4.Enter next stage after this operation for some time in stage.
Two, the anoxic stage:
Close Inlet and outlet water and aeration air pump, make the active sludge in the tank 1 be in anoxic condition, can increase hydraulic detention time to a certain extent like this, the nitrification and denitrification effect that strengthens microorganism finally can improve the nitric efficiency of equipment.Continue next stage after this operation for some time in stage.
Three, sky exposes to the sun the stage:
Open the gas distribution air pump, make the qi-emitting hole of gas distribution pipe 7 form tiny air-flow.Add this sky and expose to the sun after the stage, the washing away of the tiny bubble that the diaphragm of described filtration lamina membranacea 22 can form at qi-emitting hole make the part pollutent break away from diaphragm down, makes the film pollution be eased, and membrane flux obtains recovery to a certain degree.Simultaneously, because described membrane bioreactor recovers air feed, will recover the good oxygen condition of microorganism, for next stage gets ready.The described sky stage of exposing to the sun repeats the fs after moving for some time.
Can be provided with arbitrarily according to actual needs the working time of above-mentioned three phases, will provide the Best Times setting in the following example.
The embodiment of the invention all is that the membrane bioreactor with board-like film membrane module is an example, and technology of the present invention also can be applied in the membrane bioreactor of hollow-fibre membrane membrane module.
Below be example with printing and dyeing mill's waste water, adopt the concrete operating scheme of described equipment of above-mentioned second embodiment and method as follows:
Table 1 periodic running experimental program
After the sampling, measure pH, DO, T, COD, TN and water flow, and calculate membrane flux (membrane area 0.8m2), every mud index sees Table 2 when initial.
Initial mud of table 2 and supernatant liquor activity index thereof
Annotate: DO---dissolved oxygen; SV---sludge settling ratio; MLSS---mixed liquor suspended solid, MLSS concentration;
SVI---sludge volume index; TN---total nitrogen; HRT---hydraulic detention time
After the equipment operation, the same intervals time point taken a sample records the COD clearance as shown in Figure 5.By among Fig. 5 as can be seen, in the operation starting stage, the COD clearance remains on about 93%, along with the carrying out of experiment, microorganism adapts to new environment gradually, last clearance is about 95%, and the average removal rate of whole process also reaches 94.4%, and devices illustrated running condition is stable, and kept higher COD clearance, because water inlet COD higher (3530mg/L) so water outlet COD numerical value is higher relatively, needs just can reach emission request through further processing.
The same intervals time point is taken a sample, can get the TN clearance,, be respectively the TN clearance that adopts the described method and apparatus of second embodiment of the invention and legacy equipment and operation method as Figure 6 and Figure 7.
Traditional succession running scheme is the water of being back to back among Fig. 7, no anoxic stage and sky expose to the sun the stage, compare with operating scheme of the present invention, average removal rate has only 63.1%, and the present invention is in service, and starting stage TN clearance remains on about 84%, and is basicly stable 78% to the later stage clearance, the average removal rate of whole process is 80.2%, has TN removal effect preferably.
Shown in Fig. 8,9, be respectively the membrane flux that adopts described scheme of second embodiment of the invention and traditional scheme to record and change.
By Fig. 8 and Fig. 9 contrast as can be known, operating scheme membrane flux of the present invention be changed to restorative decline, after one-period finished, after promptly sky exposed to the sun and finishes, membrane flux recovered to some extent, and whole process membrane flux variable quantity is less relatively, variable quantity is 1.12L/ (hm
2), rate of descent is about 10.9%, and the average film flux is 9.58L/ (hm
2); In the tradition succession running process, flux descends comparatively obvious, and does not have recovery, and variable quantity is 7.80L/ (hm
2), rate of descent is 76.5%, the average film flux is 5.12L/ (hm
2), as can be known, operating scheme of the present invention has very significantly effect to the recovery and the alleviating of film pollution of membrane flux.
Claims (5)
1. the treatment process of a membrane bioreactor in trade effluent is characterized in that comprising following two stages:
One, be back to back water and aeration phase:
In membrane bioreactor, intake continuously and continuous pumpage, carry out aeration simultaneously, enter next stage after operation for some time;
Two, sky exposes to the sun the stage:
Close Inlet and outlet water, continue aeration, aeration forms tiny air-flow the diaphragm of membrane module in the membrane bioreactor is washed away, and this stage repeats the fs after moving for some time.
2. according to the treatment process of the described membrane bioreactor of claim 1 in trade effluent, it is characterized in that: also increase between described fs and the subordinate phase have two, the anoxic stage, close Inlet and outlet water and aeration, make active sludge be in anoxic condition, enter sky after operation for some time and expose to the sun the stage.
3. the treatment process in trade effluent according to claim 1 or 2 described membrane bioreactors is characterized in that: the described sky stage of exposing to the sun is carried out the sky aeration that exposes to the sun by the original aeration tube of membrane bioreactor.
4. according to the treatment process of the described membrane bioreactor of claim 2 in trade effluent, it is characterized in that: the optimum operation duration of described three phases is: be back to back water and aeration phase 120-180 minute, in 60-120 minute anoxic stage, sky exposed to the sun stage 10-30 minute.
5. a new membrane bio-reactor is provided with membrane module within tank, and membrane module comprises the dialyzate passage that forms in diaphragm and the diaphragm; Be provided with the water inlet pipe that communicates with tank below tank, the top is provided with the water pipe that gives that communicates with the dialyzate passage; The bottom of tank also is provided with aeration tube, and this aeration tube is provided with some solarization air caps; It is characterized in that: increasing in the described tank has gas distribution pipe, has some qi-emitting holes on this gas distribution pipe, and this qi-emitting hole is positioned at diaphragm-operated below or side.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102786188A (en) * | 2012-08-29 | 2012-11-21 | 哈尔滨工业大学 | Forward osmosis membrane bioreactor with magnetic nanoparticles serving as driving liquid |
| US9333464B1 (en) | 2014-10-22 | 2016-05-10 | Koch Membrane Systems, Inc. | Membrane module system with bundle enclosures and pulsed aeration and method of operation |
| USD779632S1 (en) | 2015-08-10 | 2017-02-21 | Koch Membrane Systems, Inc. | Bundle body |
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| CN101549907A (en) * | 2008-04-02 | 2009-10-07 | 天津膜天膜工程技术有限公司 | Membrane biologic reaction equipment and processing method for processing industrial waste water with high ammoniac nitrogen |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102786188A (en) * | 2012-08-29 | 2012-11-21 | 哈尔滨工业大学 | Forward osmosis membrane bioreactor with magnetic nanoparticles serving as driving liquid |
| CN102786188B (en) * | 2012-08-29 | 2013-10-30 | 哈尔滨工业大学 | Forward osmosis membrane bioreactor with magnetic nanoparticles serving as driving liquid |
| US9333464B1 (en) | 2014-10-22 | 2016-05-10 | Koch Membrane Systems, Inc. | Membrane module system with bundle enclosures and pulsed aeration and method of operation |
| US9956530B2 (en) | 2014-10-22 | 2018-05-01 | Koch Membrane Systems, Inc. | Membrane module system with bundle enclosures and pulsed aeration and method of operation |
| US10702831B2 (en) | 2014-10-22 | 2020-07-07 | Koch Separation Solutions, Inc. | Membrane module system with bundle enclosures and pulsed aeration and method of operation |
| USD779632S1 (en) | 2015-08-10 | 2017-02-21 | Koch Membrane Systems, Inc. | Bundle body |
| USD779631S1 (en) | 2015-08-10 | 2017-02-21 | Koch Membrane Systems, Inc. | Gasification device |
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Application publication date: 20110406 |