CN101830607B - Alternate two-stage aerobic membrane bioreactor - Google Patents
Alternate two-stage aerobic membrane bioreactor Download PDFInfo
- Publication number
- CN101830607B CN101830607B CN2010101799051A CN201010179905A CN101830607B CN 101830607 B CN101830607 B CN 101830607B CN 2010101799051 A CN2010101799051 A CN 2010101799051A CN 201010179905 A CN201010179905 A CN 201010179905A CN 101830607 B CN101830607 B CN 101830607B
- Authority
- CN
- China
- Prior art keywords
- reactor drum
- valve
- reactor
- water
- impeller pump
- 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.)
- Expired - Fee Related
Links
Images
Abstract
The invention provides an alternate two-stage aerobic membrane bioreactor. The alternate two-stage aerobic membrane bioreactor comprises a first reactor MRR1, a second reactor MBR2, a regulating tank I, a flow meter, a valve, a centrifugal pump, an automatic-control motor case II, a water storage tank IV, an alkali liquor box III, an acid liquor box V, a first air blower GFJ1, a second air blowerGFJ2, a perforated pipe aerating apparatus and an inka aeration apparatus. The invention can realize that after high concentrated organic waste water is hydrolyzed and acidized, the effluent is not subjected to methanogenic-phase reaction but directly enters into the aerobic membrane bioreactor for treatment, so that the effluent has qualified quality; and in the process, the effluent is ensured to be continuous, membrane fouling is retarded, membrane flux is recovered to the maximum limit, and full-automatic control, safety, stability and high efficiency are achieved.
Description
Technical field
What the present invention relates to is a kind of waste disposal plant.
Background technology
The development of membrane bioreactor is decades only, but development rapidly, and this mainly is because membrane bioreactor (MBR) combines biological processing unit and membrane technology, effluent quality even reach the standard of middle water reuse.But it is further applied owing to problems affect such as membrane pollution problem are serious, the organic loading rate is limited, the automatic control level is not high, water outlet is discontinuous.One Chinese patent application number is a disclosed membrane biological reaction apparatus in 02104266.7 the patent document; Be made up of membrane module, clear water tanks, water lines, air pipe and water pump, membrane module is made up of hollow fiber bundle, aeration tube, aeration mouth, header, is characterized in: adopt online monitoring measure effectively to detect the film pollution condition; Adopt the pulsation aeration during back flushing; Increase the shake of hollow-fibre membrane, reduced the face obstruction and polluted the prolongation membrane lifetime.But have following problem: 1, common membrane bioreactor bears the limited in one's ability of sludge loading, unsuitable direct treatment of high concentration organic waste water; 2, automatic control weak effect; 3, the mode of back flushing is that water conservancy is washed away and added the pulsation aeration and can not eliminate the deep layer film and pollute, and the membrane flux recovery situation is not as medicine liquid washing.Number of patent application be 200610023281.8 patent document in disclosed integral membrane biological reaction device for water treatment, thereby be that membrane module is positioned in the CASS reaction tank integral membrane biological reaction device for water treatment that forms.Circulating type active sludge technology (cyclic activated sludge system) is that reaction tank is divided into three districts: biological selecting area, oxygen-starved area, aerobic zone, different subregion mikrobes be degradation of organic substances under top condition separately respectively, so effluent quality is good.But the hydrophone of straining of its outlet system often is difficult to reach design requirements, and the water outlet concentration of suspension is high, and turbidity is high.Adopt the water-out manners of MBR to combine promptly to become the biological water treatment device of integral type film with cyclic activated sludge system.But there is following problem in this invention: 1, the cycle of operation is long; 2, water outlet is discontinuous.Alternate two-stage aerobic membrane bioreactor is decelerating membrane pollution, continuous effluent effectively, realizes the heavy-duty service of full automatic control.
Summary of the invention
The object of the present invention is to provide a kind of alternate two-stage aerobic membrane bioreactor that can realize full automatic control, continuous effluent, treatment of high concentration organic waste water.
The objective of the invention is to realize like this:
Alternate two-stage aerobic membrane bioreactor of the present invention comprises first reactor drum, second reactor drum, equalizing tank, under meter, SV, suction pump, water tank, lye tank, acid solution case, first gas blower, second gas blower, perforated pipe aerating regulation device, Inka aeration device; Equalizing tank water outlet place is connected with first SV and first flow meter; Equalizing tank is connected by suction culvert with first reactor drum, and second SV and a COD on-line measurement appearance are connected between the first flow meter and first reactor drum; Equalizing tank also is connected by suction culvert with second reactor drum, is connected with SV and COD on-line measurement appearance on the suction culvert, and the 3rd SV and the 2nd COD on-line measurement appearance are connected between the first flow meter and second reactor drum; First reactor drum water outlet place connects the 3rd COD on-line measurement appearance; Take-off pipe of the outlet pipeline of first reactor drum connects and gets into second reactor drum, and the water outlet of first reactor drum is as the water inlet of second reactor drum, and is connected to the 4th SV and first impeller pump on this branch line; Second reactor drum water outlet place connects the 4th COD on-line measurement appearance; Branch line of the outlet pipeline of second reactor drum connects and gets into first reactor drum, and the water outlet of second reactor drum is as the water inlet of first reactor drum, and is connected to the 5th SV and second impeller pump on this branch line; Another branch line of the first reactor drum outlet pipeline links to each other with water tank, is provided with second under meter before the water tank, is connected with the 4th impeller pump, the 7th SV on this branch line successively; Another branch line of second reactor drum links to each other with water tank, and be connected with the 3rd impeller pump successively on this branch line, the 6th SV; With water tank is set up in parallel Youxiaolin lye tank and sulfuric acid acid solution case arranged; Water outlet place of water tank, lye tank, acid solution case is connected with the tenth SV, the 4th under meter, the 11 SV, the 5th under meter, the 12 SV, the 6th under meter respectively; After converging, the outlet pipeline of water tank, lye tank, acid solution case is connected to the 5th impeller pump; By being connected to first reactor drum and second reactor drum respectively by two counter-flushing pipelines respectively again after the lifting of the 5th impeller pump; The counter-flushing pipeline that connects first reactor drum is provided with the 13 SV; Connect second reactor drum counter-flushing pipeline be provided with the 14 SV, the soup of carrying in the counter-flushing pipeline directly gets into reactor drum; First reactor drum and first reactor drum are provided with film and purge and supply the dissolved oxygen aerating system.
Establish four membrane modules in each reactor drum, said film is the polyethylene hollow fiber film.
Film purges and supplies the dissolved oxygen aerating system to comprise perforated pipe that is positioned at reactor bottom and the Inka aeration pipe of highly locating apart from reactor drum top 1/3rd; First gas blower is connected to the 15 SV successively, the 7th under meter constitutes first airline, and first airline links to each other with Inka aeration pipeline air inlet place of first reactor drum; First gas blower also is connected with the 16 SV simultaneously, the 8th under meter constitutes second airline, and second airline links to each other with the bottom aerating apparatus admission passage of first reactor drum; Second gas blower is connected to the 17 SV successively, the 9th under meter constitutes the 3rd airline, and the 3rd airline links to each other with Inka aeration pipeline air inlet place of second reactor drum; Second gas blower also is connected with the 18 SV simultaneously, the tenth under meter constitutes the 4th airline, and the 4th airline links to each other with the bottom aerating apparatus admission passage of second reactor drum.
The invention provides the aerobic membrane bioreactor of a kind of full automatic control, continuous effluent, treatment of high concentration organic waste water.High concentrated organic wastewater produces methane phase and reduces organic concentration and can directly get into membrane bioreactor and (behind acidication, can collect lactic acid through passing through behind the acidication; Do not produce methane; Reduce greenhouse gases); And because high, the hollow-fibre membrane crown_interception of sludge concentration in the membrane bioreactor, effluent quality still can reach higher standard.Simultaneously, because alternate run produces the replacement of mikrobe phase,, slowed down the film pollution because the food chain effect is washed+backwash mode of air purge, alkali cleaning, pickling in addition.
The present invention is by two placed in-line membrane bioreactor alternate runs; Aspirate water outlet to water tank with impeller pump; (through the on-line monitoring reactor drum Inlet and outlet water COD of place, when the COD clearance is 40%, being replaced by automatic controlling system) secondary membrane bioreactor alternately after operation for some time.Because the series connection alternate run of reactor drum; After the reactor drum that be in underload early stage is transformed into the high loading reactor drum; Be in the organism of digesting and assimilating that the mikrobe of endogenous respiration can be excessive; Therefore can bear higher sludge loading, high concentrated organic wastewater need not methane-producing reactor, and water outlet can directly get into this reactor drum after the acidication reaction.Organic loading during alternate run in the reactor drum changes, and the aerobic microbiological bacterium colony changes a lot, and the change of flora occurs, because the effect of food chain can reduce the mud of film surface alluvial and loose sludge blanket, decelerating membrane pollution.Unique simultaneously online backflushing is washed mode: washing+air purge, alkali cleaning, pickling can be removed film more efficiently and pollute, and recover membrane flux to greatest extent.During back flushing, reactor drum normally moves another reactor drum to carry out online backflushing and washes, continual mode of operation guaranteed water outlet continuously.Valve 1, valve 4, valve 5 are manually-operated gate among the present invention, and after impeller pump breaks down, but the manual-lock valve overhauls; Other valves are SV, the water level of Inlet and outlet water, normal reactor drum in service alternately, the back flushing when film is seriously polluted is by full-automatic control system control (II among the figure one is the automatic control motor case), and is safe and reliable, stable.
Technical characterstic of the present invention is mainly reflected in:
1, general high concentrated organic wastewater needs to reach standard by membrane bioreactor aerobic treatment to water outlet again through after the anaerobic treatment earlier.Among the present invention; The series operation of two-stage membrane bioreactor can make high concentrated organic wastewater behind acidication, directly get into membrane bioreactor; The operation for some time after (through the on-line monitoring reactor drum Inlet and outlet water COD of place; When the COD clearance was 40%, automatically control was alternately by robot control system(RCS)) two-stage reactor alternately, underload reactor drum originally is as new high loading reactor drum; Single reaction vessel is born processing power decline, the frequent problem of back flushing that higher load causes when having avoided not alternate run, therefore can bear higher organic loading.
When 2, normally moving, water outlet like this can decelerating membrane pollution by the impeller pump intermittent suction.Water outlet is stored in the water tank again by the water outlet of impeller pump F continuously pumping, therefore can guarantee water outlet continuously.The under meter a and the under meter b at Inlet and outlet water place are connected to automatic control system, according to the switching of online detected flow by automatic controlling system Inlet and outlet water place valve, guarantee that the liquid level in the reactor drum maintains certain limit.
3, during back flushing, first membrane bioreactor (MBR1) carries out back flushing earlier, and the second membrane bioreactor works better guarantees that water outlet is constant relatively.Back flushing adopts the associating backwash mode of sluicing (flushing with clean water+air purge) and medicine liquid washing (sulfuric acid of the Youxiaolin+massfraction 0.035% of massfraction 1%) to remove the film pollution.Flushing with clean water+air purge can be eliminated the loose sludge blanket of mud and film surface that deposits between the tunica fibrosa; The chlorine bleach liquor can remove the mikrobe and the organic pollutant on film surface; Sulphuric acid soln can be removed film surface and inner inorganics dirt.The sulfuric acid acid solution of lower concentration and Youxiaolin alkali lye can not cause the mikrobe in the reactor drum and murder, and the alternate run of alkali cleaning and pickling has guaranteed that the pH value in the reactor drum is constant relatively.
4, during back flushing, soup is got into from the water inlet by impeller pump E suction, and then aspirates out soup to equalizing tank by impeller pump D or C, together carries out a biological disposal upon with raw waste water subsequently.Like this, the path of flowing through of soup gets into inside and then is sucked up to equalizing tank from membrane module is outside, is equivalent to be immersed in membrane module in the soup, cleans the surfaces externally and internally of film simultaneously, and it is big that membrane flux recovers.
5, when works better and back flushing the switching of valve by the Data Control of automatic control system according to on-line monitoring.When water flow is back flushing 40% when finishing, begin back flushing, when flow after the back flushing return to last time back flushing when finishing flow 90% the time stop back flushing, works better once more.So not only safe and reliable, can also guarantee that complete assembly in the operation of optimum regime maximum load best efficiency point, improves whole operating performance, cut down the consumption of energy.
6, each reactor drum is provided with film and purges and supply dissolved oxygen two-way aerating system, and the air feed form is respectively Inka aeration device (highly locating apart from reactor drum top 1/3rd)---the perforated pipe aerating regulation device of micro-hole aerator and bottom.Two cover aerating systems can play the effect that sufficient dissolved oxygen and mixing, stirring are provided simultaneously.In the back flushing, while aeration during flushing with clean water can wash away the surperficial particulate fouling of film, helps recovering membrane flux.Simultaneously, the shallow-layer micro-pore aeration system of middle and upper part can cut down the consumption of energy, and more air capacities are provided, and strengthens turbulent extent, accelerates the transfer rate of oxygen.
7, establish four membrane modules in each reactor drum, film is the polyethylene hollow fiber film.Fixedly the tubular fibre of film vertically places the bottom surface of reactor drum, and rising pipe connects the header that is parallel at the bottom of the reactor drum case by the hollow fiber conduit two ends and forms.Membrane module connects two vertical tubes by two rising pipe two ends and forms.
8, the back flushing case comprises water tank IV, Youxiaolin lye tank III and sulfuric acid acid solution case V, is controlled by separately valve and under meter respectively.Aeration in the time of flushing with clean water is closed aerating system and is made the active sludge sedimentation when soup online backflushing is washed, aspirate out soup with impeller pump D or C.
9, be provided with the perforated pipe aerating regulation device in the bottom of reactor drum, perforated pipe evenly is laid on reactor bottom.Highly locate to establish Inka aeration device---microporous diffuser at reactor drum 1/3rd, the Inka aeration device interts between five gaps of membrane module.Be respectively first reactor drum (MBR1) and second reactor drum (MBR2) provides required air capacity by gas blower GFJ1 and gas blower GFJ2; By the automatic control system switching of by-pass valve control 15, valve 16, valve 17, valve 18 respectively, thereby realize control to the perforated pipe aerating regulation device aeration rate of Inka aeration device in first and second reactor drums and bottom.
10, the below of reactor drum membrane module is provided with blow-down pipe and shore pipe; Top is provided with upflow tube, prevents that reactor drum is submerged.
11, water inlet place under meter a data presented is Q
IN, the data presented of water outlet place under meter b is Q
OUT, when both differences are 90% (this value is a higher limit) of reactor volume, cut off water inlet, continuous effluent automatically; When both differences were 50% (this value is a lower value) of reactor volume, water outlet was closed in water inlet continuously.More than operation realizes by automatic controlling system, has guaranteed the safe and reliable operation of reactor drum.
Structure of the present invention is compared with existing membrane bioreactor, and meliority is:
1, the membrane bioreactor alternate run of two-stage series connection, the organic loading rate is high, can bear higher organic loading, and high concentrated organic wastewater can directly get into this aerobic reactor through need not behind the acidication through methanogenic reaction, and water outlet is effective.The one-level membrane bioreactor load of having avoided causing owing to alternate run not is too high to make the problem that processing power descends, the cycle of operation is short, back flushing is frequent.
2, the mode of alternate run and alternately back flushing has guaranteed the continuous of water outlet, and effluent quality is unaffected basically.
3, theoretical Inka aeration device---the two aerating systems of the perforated pipe aerating regulation device of microporous diffuser and bottom of Inka aeration have been adopted; Sufficient dissolved oxygen can not only be provided; Increase turbulent extent, accelerate the transfer rate of oxygen, also because the Inka aeration device has reduced energy consumption; Increase air capacity, promoted washing away of mud of film surface to come off.
4, this covering device adopts full-automatic control system, has kept the constant fluctuation of water level in the reactor drum in certain limit, has kept certain hydraulic detention time.The valve opening and closing of simultaneously normal operation, back flushing, aerating system makes the operation of total system highly effective and safe by automatic controlling system.
5, the backwash mode of washing+air purge, alkali cleaning, pickling has recovered membrane flux to greatest extent, and film cleans thoroughly.
Description of drawings
Fig. 1 is a principle flow chart of the present invention;
Fig. 2-1 is a membrane bioreactor 2-2 sectional view; Fig. 2-2 is a membrane bioreactor 1-1 sectional view;
Fig. 3-1 is the membrane module vertical view, and Fig. 3-2 is the 1-1 sectional view of Fig. 3-1, and Fig. 3-3 is the 2-2 sectional view of Fig. 3-1;
Fig. 4-1 is the structural representation of bottom aerating apparatus, and Fig. 4-2 is the 1-1 sectional view of Fig. 4-1, and Fig. 4-3 is the 2-2 sectional view of Fig. 4-1
Fig. 5-1 is the structural representation of Inka aeration device, and Fig. 5-2 is the 1-1 sectional view of Fig. 5-1, and Fig. 5-3 is the 2-2 sectional view of Fig. 5-1.
Embodiment
For example the present invention is done description in more detail below in conjunction with accompanying drawing:
In conjunction with Fig. 1, this covering device is made up of following: membrane bioreactor MBR1, membrane bioreactor MBR2, equalizing tank I, under meter, valve, impeller pump, water tank IV, lye tank II, acid solution case V, automatic control motor case II, gas blower GFJ1, gas blower GFJ2, perforated pipe aerating regulation device, Inka aeration device.
Equalizing tank water outlet place is connected with valve 1, impeller pump G and under meter a.Equalizing tank is connected by suction culvert with the first reactor drum MBR1, is connected with valve 2 and the 2nd COD on-line measurement appearance on the suction culvert of the equalizing tank and the first reactor drum MBR1, and valve 2 and the 2nd COD on-line measurement appearance are connected between the under meter a and the first reactor drum MBR1.Equalizing tank also is connected by suction culvert with the second reactor drum MBR2, is connected with a valve 3 and a COD on-line measurement appearance on the suction culvert, and a valve 3 and a COD on-line measurement appearance are connected between the under meter a and the second reactor drum MBR2.First reactor drum MBR1 water outlet place connects the 3rd COD on-line measurement appearance.A take-off pipe of the outlet pipeline of the first reactor drum MBR1 connects the entering second reactor drum MBR2, and the water outlet of the first reactor drum MBR1 is connected to valve 4, tensimeter YLB1 and impeller pump A as the water inlet of the second reactor drum MBR2 on this pipeline.Equally, second reactor drum MBR2 water outlet place also connects the 4th COD on-line measurement appearance.A branch line of the outlet pipeline of the second reactor drum MBR2 connects the entering first reactor drum MBR1, and the water outlet of the second reactor drum MBR2 is connected to impeller pump B, tensimeter YLB2 and valve 5 as the water inlet of the first reactor drum MBR1 on this pipeline.Another branch line of the first reactor drum MBR1 outlet pipeline links to each other with water tank, is provided with under meter b before the water tank, is connected with tensimeter YLB4 impeller pump D, valve 7 on this outlet pipeline successively, and valve 7 links to each other with under meter b.Equally, another water outlet branch line of the second reactor drum MBR2 also links to each other with water tank, on this pipeline, is connected with tensimeter YLB3, impeller pump C, valve 6 successively, and valve 6 links to each other with under meter b.With water tank is set up in parallel Youxiaolin lye tank and sulfuric acid acid solution case arranged.Water outlet place of water tank, lye tank, acid solution case is connected with valve 10, under meter d respectively; Valve 11, under meter e; Valve 12, under meter f.After converging, the outlet pipeline of water tank, lye tank, acid solution case is connected to impeller pump E; By being connected to first reactor drum and second reactor drum respectively by two counter-flushing pipelines respectively again after the impeller pump E lifting; The counter-flushing pipeline that connects first reactor drum is provided with valve 13; Connect second reactor drum counter-flushing pipeline be provided with valve 14, the soup of carrying in the counter-flushing pipeline directly gets into reactor drum.Gas blower GFJ1 is connected to valve 15, under meter g successively, and this airline links to each other with Inka aeration pipeline air inlet place of the first reactor drum MBR1; Gas blower GFJ1 also is connected with valve 16, under meter h simultaneously; This airline gas blower GFJ2 that links to each other with the bottom aerating apparatus admission passage of the first reactor drum MBR1 is connected to valve 17, under meter i successively, and this airline links to each other with Inka aeration pipeline air inlet place of the second reactor drum MBR2; Gas blower GFJ2 also is connected with valve 18, under meter j simultaneously, and this airline links to each other with the bottom aerating apparatus admission passage of the second reactor drum MBR2.
The valve (SV) of a whole set of reaction unit, impeller pump, under meter, COD on-line measurement appearance etc. all are connected with the motor case of automatic control system, realize full automatic control.
In conjunction with Fig. 2-1 and Fig. 2-2, be equipped with four membrane modules in each reactor drum, mould material is the polyethylene hollow fiber film, and hollow fiber conduit is perpendicular to the reactor drum bottom surface, and impeller pump is the suction of the header in reactor drum bottom surface water outlet from lower, parallel.The perforated pipe aerating regulation device is installed in the bottom of each reactor drum, and reactor drum 1/3rd is highly located the Inka aeration device is installed between membrane module, and using gas blower GFJ1 and gas blower GFJ2 respectively is that two reactor drums provide air.Reactor lower part is provided with blow-down pipe and shore pipe, and upflow tube is arranged at top.
In conjunction with Fig. 1, two reactors in series operations during works better.The first reactor drum MBR1 is delivered to the second reactor drum MBR2 through impeller pump A with water, realizes through automatic control decorum control impeller pump A; The second reactor drum MBR2 is delivered to the first reactor drum MBR1 through impeller pump B with water, through the start and stop realization of control impeller pump B.The water outlet of the first reactor drum MBR1 is delivered to water tank by impeller pump D suction, through the switching realization of by-pass valve control 7; The water outlet of the second reactor drum MBR2 is delivered to water tank by impeller pump C suction water outlet and is realized by the switching of by-pass valve control 6.Between the water outlet of reactor drum and water tank, under meter b is installed, measures discharge.Water in the water tank is by the water outlet of impeller pump F continuously pumping.
When online backflushing was washed, shown in long and short dash line among the figure, order was from water tank IV, lye tank III and the suction of acid solution case V respectively with impeller pump E, and by under meter d, under meter e, under meter f difference dominant discharge, valve 10, valve 11, valve 12 controls open and close.Being that massfraction is 1% chlorine bleach liquor in the lye tank III, is that massfraction is 0.035% sulphuric acid soln in the acid solution case V.The back flushing loop that the back flushing loop of the first reactor drum MBR1 is provided with valve 13, the second reactor drum MBR2 is provided with valve 14.The soup that gets in the first reactor drum MBR1 aspirates out reactor drum and is delivered to equalizing tank with impeller pump D, is provided with valve 9 between the first reactor drum MBR1 and the equalizing tank; Get into soup in the second reactor drum MBR2 and aspirate out reactor drum with impeller pump C and be delivered to equalizing tank, be provided with valve 8 therebetween.Under meter c is installed between valve 8 and valve 9 and equalizing tank, is used for the recovery situation that metering film cleans the back flux.
The working process of one-period internal reaction device:
During works better, as the one-level membrane bioreactor, the second reactor drum MBR2 is as the secondary membrane bioreactor with the first reactor drum MBR1 in elder generation.Open valve 2 valve-offs 3, raw waste water gets into the first reactor drum MBR1.In the first reactor drum MBR1, microbiological deterioration organic substance, waste water obtain preliminary purification.The second reactor drum MBR2 is aspirated out and be delivered to the water outlet of the first reactor drum MBR1 by impeller pump A; Organic substance is degraded in the second reactor drum MBR2 once more; Water body is purified; To handle water up to standard by impeller pump C suction water outlet then and be delivered to the water tank IV, keep certain water level in the water tank IV, by the water outlet of impeller pump F continuously pumping.At this moment, valve 2, valve 4, valve 6 are opened, and all the other valves are all closed.The working order of impeller pump is that intermittent suction pollutes to alleviate film, and the work period of impeller pump is suction 12min, and stop pumping 2min, swabbing pressure are 0.25MPa (being shown by tensimeter before the impeller pump).The operation for some time after (through the on-line monitoring reactor drum Inlet and outlet water COD of place; When the COD clearance is 40%; Replace by automatic controlling system); The first reactor drum MBR1 and second reactor drum MBR2 exchange working order, the second reactor drum MBR2 is as the one-level membrane bioreactor, and water inlet directly gets into the second reactor drum MBR2.The water outlet of the second reactor drum MBR2 is pumped to water inlet place of the first reactor drum MBR1 by impeller pump B, water outlet after the processing once more of the first reactor drum MBR1, and water outlet is drawn to the water tank IV by impeller pump D.The working order of impeller pump remains suction 12min, and stop pumping 2min, swabbing pressure are 0.25MPa.At this moment, valve 3, valve 5, valve 7 are opened, and all the other are all closed.During works better, two cover aerating apparatus non-stop runs simultaneously in each reactor drum.The registration of under meter a is flooding velocity Q
IN, the flow of under meter b is water flow Q
OUT, work as Q
OUTBe 40%Q
INThe time, showing that film is seriously polluted, the beginning online backflushing is washed.
During back flushing, the first reactor drum MBR1 is carried out back flushing, the second reactor drum MBR2 works better earlier.The switching situation of valve is on the inlet and outlet pipe: valve 1, valve 3, valve 6 are opened, and valve 2, valve 4, valve 5, valve 7 are closed.Former water directly gets into the second reactor drum MBR2, through directly aspirating water outlet to water tank by impeller pump C after the biological degradation of the second reactor drum MBR2.The first reactor drum MBR1 carries out online backflushing and washes.The flow of back flushing is 40%Q
IN, online backflushing is washed the branch three phases: washing+air purge, alkali cleaning, pickling.Carry out online washing+air purge earlier and remove the loose sludge blanket in film surface.At this moment, valve 10, valve 13 are opened, and valve 11, valve 12, valve 14 are closed, and by impeller pump E the water in the water tank IV are pumped to the first reactor drum MBR1, the while aeration, and valve 15, valve 16, valve 17, valve 18 are all opened.The time of online washing+air purge is 2 hours, carries out online alkali cleaning subsequently, and the online alkali cleaning time is 30min, this moment valve-off 10, valve 12, Open valve 11; Valve 15, valve 16 close in the aerating system, and valve 17, valve 18 are opened, and gas blower GFJ1 closes, and gas blower GFJ2 opens, and all the other valve opening and closing situation are constant.Close aerating system when medicine is washed and make sludge settling, by water outlet impeller pump D soup is extracted out simultaneously, like this, whole diaphragm is immersed in the soup, and soup flows through to internal surface from film outer surface and make film clean thoroughly, helps recovering to greatest extent membrane flux.Carry out online pickling at last, the online pickling time is 30min, and valve 10, valve 11 close, and valve 12 is opened.Valve opening and closing situation in the whole backwash process of the first reactor drum MBR1 on the back flushing outlet pipeline is: valve 9 is opened, valve 8 closes.Repeat above-mentioned backwash process after online pickling finishes and reach preassigned until the recovery situation of membrane flux.Be connected with under meter c behind the valve 9, show the recovery situation that cleans the back membrane flux, as the flow Q of under meter c
REReturn to last time back flushing and finish back flow Q
0(automatic control system each back flushing finish more this value of new record) 90% o'clock shows the back flushing end, stops the back flushing to the first reactor drum MBR1.Subsequently, the first reactor drum MBR1 begins works better, begins that the second reactor drum MBR2 is carried out online backflushing and washes.It is the same that the online backflushing of the second reactor drum MBR2 is washed process; Valve opening and closing situation during back flushing is: during (1) washing: valve 1, valve 2, valve 7, valve 8, valve 10, valve 14, valve 15, valve 16, valve 17, valve 18 are opened; Impeller pump C, impeller pump D, impeller pump E, impeller pump F, impeller pump G open, and gas blower GFJ1, gas blower GFJ2 open; Valve 3, valve 4, valve 5, valve 6, valve 9, valve 11, valve 12, valve 13 close, and impeller pump A, impeller pump B close.(2) during alkali cleaning: valve 1, valve 2, valve 7, valve 8, valve 11, valve 14, valve 15, valve 16 are opened, and impeller pump C, impeller pump D, impeller pump E, impeller pump F, impeller pump G open, and gas blower GFJ1 opens; Valve 3, valve 4, valve 5, valve 6, valve 9, valve 10, valve 12, valve 13, valve 17, valve 18 close, and impeller pump A, impeller pump B close, and gas blower GFJ2 closes.(3) during pickling: valve 1, valve 2, valve 7, valve 8, valve 12, valve 14, valve 15, valve 16 are opened, and impeller pump C, impeller pump D, impeller pump E, impeller pump F, impeller pump G open, and gas blower GFJ1 opens; Valve 3, valve 4, valve 5, valve 6, valve 9, valve 10, valve 11, valve 13, valve 17, valve 18 close, and impeller pump A, impeller pump B close, and gas blower GFJ2 closes.
Electromagnetic valve switching situation in working process and the backwash process sees the following form:
| Gas blower GFJ2 | Open | Open | Open | Open | Open | Open | Close | Close | Open |
The design's liquid level control is achieved in that as T* (Q
IN-Q
OUTDuring)=90%V (T is a hydraulic detention time, and V is the volume of reactor drum), stop into water, impeller pump G stops suction; As T* (Q
IN-Q
OUTDuring)=50%V, continue water inlet, stop water outlet, valve-off 6 or valve 7; Work as Q
IN-Q
OUTValue between two ultimate values the time, the situation during with normal operation.
In the above valve; Valve 1, valve 4, valve 5 are manually-operated gate; All the other are electromagnetic valve; The open and-shut mode of valve is realized by automatic control system and data management system, adopts full automatic control aeration, Inlet and outlet water, backwash mode can guarantee reactor drum safety, stablize, work efficiently.
To Fig. 3-3, figure is the three-view diagram of membrane module, the long 1.5m of reactor drum, wide 1.2m, 2.0m in conjunction with Fig. 3-1.Establish four membrane modules in the reactor drum, film is the polyethylene hollow fiber film, and the spacing between diaphragm is 300mm, length direction upper diaphragm and reactor drum be spaced apart 300mm; The wide 700mm of membrane module, membrane module and reactor drum interval 250mm on the width; The high 1200mm of membrane module, the 500mm apart from the reactor drum upper end, membrane module lower central place is provided with header and collects the water outlet after Membrane Bioreactor for Wastewater Treatment.
To Fig. 4-3, figure is the three-view diagram of bottom perforated tube aeration device in conjunction with Fig. 4-1, and gas blower GFJ1 or gas blower GFJ2 connect the aeration house steward, and the aeration house steward directly is deep at the bottom of the pond 100mm at the bottom of the width between centers pond from top, and the aeration house steward is apart from reactor wall 100mm; The total pipe coupling aeration of aeration main, the long 1200mm of main, main is apart from reactor wall 150mm; Do not have at a distance from 400mm on the main to be uniform-distribution with four aeration arms, aeration Zhi Guanchang 800mm, apart from reactor wall 200mm, oblique angle of declination is offered the aperture for 45 ° symmetrically and evenly on the arm, aperture size 5mm, aperture spacing 75mm.
Arrive Fig. 5-3 in conjunction with Fig. 5-1; The microporous diffuser of Inka aeration device is immersed in membrane module 1/3rd and highly locates; The 1100mm apart from the reactor drum lower end, gas blower GFJ1 or gas blower GFJ2 connect the aeration house steward, and the 100mm place is the main of microporous aeration device apart from reactor head 400mm membrane module top; Connecting five arms by main, arm is deeply to membrane module; Spacing between arm is followed successively by 250mm, 300mm, 300mm, 250mm, and the spacing of arm and reactor wall is 250mm.On the aeration arm microporous diffuser is installed, is provided size to be the microbubble of 0.1mm, service area 0.5m
2/ individual about, two of microporous diffusers are installed on the every arm.
The present invention can realize that high concentrated organic wastewater is behind acidication; Water outlet needn't the phase reaction of multiparity methane and directly get into aerobic membrane bioreactor to handle the back effluent quality up to standard; And guarantee that in this process water outlet is continuous; Decelerating membrane pollution, recover membrane flux to greatest extent, full automatic control, safety and stability are efficient.
Claims (3)
1. an alternate two-stage aerobic membrane bioreactor comprises first reactor drum, second reactor drum, equalizing tank, under meter, SV, suction pump, water tank, lye tank, acid solution case, first gas blower, second gas blower, perforated pipe aerating regulation device, Inka aeration device; It is characterized in that: equalizing tank water outlet place is connected with first-hand movable valve and first flow meter; Equalizing tank is connected by suction culvert with first reactor drum, and second SV and the 2nd COD on-line measurement appearance are connected between the first flow meter and first reactor drum; Equalizing tank also is connected by suction culvert with second reactor drum, and the 3rd SV and a COD on-line measurement appearance are connected between the first flow meter and second reactor drum; First reactor drum water outlet place connects the 3rd COD on-line measurement appearance; Take-off pipe of the outlet pipeline of first reactor drum connects and gets into second reactor drum, and the water outlet of first reactor drum is as the water inlet of second reactor drum, and is connected to the 4th manually-operated gate and first impeller pump on this branch line; Second reactor drum water outlet place connects the 4th COD on-line measurement appearance; Branch line of the outlet pipeline of second reactor drum connects and gets into first reactor drum, and the water outlet of second reactor drum is as the water inlet of first reactor drum, and is connected to the 5th manually-operated gate and second impeller pump on this branch line; Another branch line of the first reactor drum outlet pipeline links to each other with water tank, is provided with second under meter before the water tank, is connected with the 4th impeller pump, the 7th SV on this branch line successively; Another branch line of second reactor drum links to each other with water tank, and be connected with the 3rd impeller pump successively on this branch line, the 6th SV; With water tank is set up in parallel Youxiaolin lye tank and sulfuric acid acid solution case arranged; Water outlet place of water tank, Youxiaolin lye tank, sulfuric acid acid solution case is connected with the tenth SV, the 4th under meter, the 11 SV, the 5th under meter, the 12 SV, the 6th under meter respectively; After converging, the outlet pipeline of water tank, Youxiaolin lye tank, sulfuric acid acid solution case is connected to the 5th impeller pump; By being connected to first reactor drum and second reactor drum respectively by two counter-flushing pipelines respectively again after the lifting of the 5th impeller pump; The counter-flushing pipeline that connects first reactor drum is provided with the 13 SV; The counter-flushing pipeline that connects second reactor drum is provided with the 14 SV, and the soup of carrying in the counter-flushing pipeline directly gets into reactor drum; First reactor drum and second reactor drum are provided with film and purge and supply the dissolved oxygen aerating system.
2. alternate two-stage aerobic membrane bioreactor according to claim 1 is characterized in that: establish four membrane modules in each reactor drum, said film is the polyethylene hollow fiber film.
3. alternate two-stage aerobic membrane bioreactor according to claim 1 and 2 is characterized in that: film purges and supplies the dissolved oxygen aerating system to comprise perforated pipe that is positioned at reactor bottom and the Inka aeration pipe of highly locating apart from reactor drum top 1/3rd; First gas blower is connected to the 15 SV successively, the 7th under meter constitutes first airline, and first airline links to each other with Inka aeration pipe air inlet place of first reactor drum; First gas blower also is connected with the 16 SV simultaneously, the 8th under meter constitutes second airline, and second airline links to each other with the admission passage of the perforated pipe of first reactor bottom; Second gas blower is connected to the 17 SV successively, the 9th under meter constitutes the 3rd airline, and the 3rd airline links to each other with Inka aeration pipe air inlet place of second reactor drum; Second gas blower also is connected with the 18 SV simultaneously, the tenth under meter constitutes the 4th airline, and the 4th airline links to each other with the admission passage of the perforated pipe of second reactor bottom.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010101799051A CN101830607B (en) | 2010-05-24 | 2010-05-24 | Alternate two-stage aerobic membrane bioreactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010101799051A CN101830607B (en) | 2010-05-24 | 2010-05-24 | Alternate two-stage aerobic membrane bioreactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101830607A CN101830607A (en) | 2010-09-15 |
| CN101830607B true CN101830607B (en) | 2012-02-01 |
Family
ID=42714851
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010101799051A Expired - Fee Related CN101830607B (en) | 2010-05-24 | 2010-05-24 | Alternate two-stage aerobic membrane bioreactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101830607B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105366805B (en) * | 2015-11-16 | 2017-10-24 | 东华大学 | A kind of alternative expression hydrolysis pretreatment unit and the method that waste water is handled using the device |
| CN108328869B (en) * | 2018-03-07 | 2023-07-18 | 中科瑞阳膜技术（北京）有限公司 | Anaerobic membrane bioreactor and wastewater treatment system |
| CN110395845A (en) * | 2019-07-17 | 2019-11-01 | 上海世渊环保科技有限公司 | A kind of High-concentration Phenolic Aldehyde production of resins waste water treatment system and processing method |
| CN110921752A (en) * | 2019-10-15 | 2020-03-27 | 邯郸钢铁集团有限责任公司 | Reactor staggered type efficient operation method |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2001008789A2 (en) * | 1999-07-29 | 2001-02-08 | Zenon Environmental Inc. | Maintenance cleaning for membranes |
| US7122121B1 (en) * | 2004-05-28 | 2006-10-17 | Jiang Ji | Advanced submerged membrane modules, systems and processes |
| CN101033107A (en) * | 2007-02-12 | 2007-09-12 | 张民良 | Separator and immersion membrane bioreactor combined water purifying device and system |
| CN101327989A (en) * | 2008-08-01 | 2008-12-24 | 中国海洋石油总公司 | Tandem type two-stage three-segment aerating biological filter |
| CN101402487A (en) * | 2008-11-18 | 2009-04-08 | 北京科技大学 | Water treatment system in two-stage moving bed biomembrane reactor |
| CN101503245A (en) * | 2009-03-27 | 2009-08-12 | 九江学院 | Double-circulating ceramic membrane bioreactor |
| CN101633546B (en) * | 2009-08-13 | 2011-12-07 | 重庆大学 | High-efficiency combined anaerobic biological treatment for treating high-concentration organic waste water |
-
2010
- 2010-05-24 CN CN2010101799051A patent/CN101830607B/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN101830607A (en) | 2010-09-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101215045B (en) | Three-compartment immersion type anaerobic film bioreactor | |
| CN100567172C (en) | Inclined plate separate film biological reactor | |
| CN101830607B (en) | Alternate two-stage aerobic membrane bioreactor | |
| CN105129974B (en) | A kind of progressive rotation type membrane bioreactor | |
| CN100342956C (en) | Membrane filter | |
| CN206396002U (en) | A kind of biological film sewage treatment system | |
| CN104445838B (en) | A kind of small-town sewage treatment system | |
| CN104162367B (en) | The cleaning method of a kind of high-efficiency water-saving, joint medicine film group device and device | |
| CN207511908U (en) | A kind of MBR film process equipment of intelligent movable type | |
| CN101450831A (en) | Gas stripping circulation type membrane biological reaction apparatus and sewage disposal method | |
| CN201770575U (en) | Combined membrane bioreactor | |
| CN107321189A (en) | A kind of outer cleaning device of MBR films line and cleaning method | |
| CN104140172A (en) | Seawater desalination pretreatment method | |
| CN105884131A (en) | Double-membrane integrated intelligent biological sewage treatment system | |
| CN202465450U (en) | Treatment device of electroplating pretreatment waste water | |
| CN215161380U (en) | External anaerobic MBR device | |
| CN213493001U (en) | Full-automatic external-pressure internal-suction type membrane filtration system | |
| CN213171958U (en) | A sewage treatment system that is used for sewage treatment's filter equipment and has it | |
| CN204661466U (en) | Mark sub-prime advanced treatment system is carried by sewage work | |
| CN102659241A (en) | Air-lift circulation type membrane-bioreactor with membrane assembly unit capable of being independently cleaned | |
| CN102949874A (en) | Floccule self-filtering device and using method thereof | |
| CN202808473U (en) | Membrane bioreactor capable of effectively treating sewage | |
| CN202808474U (en) | Membrane bioreactor capable of continuously working | |
| CN207187519U (en) | A kind of outer cleaning device of MBR films line | |
| CN1358675A (en) | Split type film biological reactor and water treatment method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20120201 Termination date: 20170524 |