CN101830607A - Alternate two-stage aerobic membrane bioreactor - Google Patents

Alternate two-stage aerobic membrane bioreactor Download PDF

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Publication number
CN101830607A
CN101830607A CN 201010179905 CN201010179905A CN101830607A CN 101830607 A CN101830607 A CN 101830607A CN 201010179905 CN201010179905 CN 201010179905 CN 201010179905 A CN201010179905 A CN 201010179905A CN 101830607 A CN101830607 A CN 101830607A
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reactor
valve
magnetic valve
water
impeller pump
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CN101830607B (en
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陈兆波
刘静
王鸿程
崔敏华
呼冬雪
王世伟
贾建辉
多平平
王晓雨
周伟肖
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Harbin Engineering University
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Harbin Engineering University
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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 blower GFJ2, 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

Alternate two-stage aerobic membrane bioreactor
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 is rapidly, and this mainly is because membrane bioreactor (MBR) combines biological processing unit and membrane technology, effluent quality in addition reach in the standard of 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.Chinese patent application number is a disclosed membrane biological reaction apparatus in 02104266.7 the patent document, constitute by 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, be characterized in: adopt the on-line 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, is not suitable for directly handling high concentrated organic wastewater; 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 microorganisms 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, water outlet concentration of suspension height, turbidity height.The water-out manners of employing MBR combines with cyclic activated sludge system promptly becomes the biological water treatment device of integral type film.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, processing high concentrated organic wastewater.
The object of the present invention is achieved like this:
Alternate two-stage aerobic membrane bioreactor of the present invention comprises first reactor, second reactor, equalizing tank, under meter, magnetic valve, 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 magnetic valve and first flow meter; Equalizing tank is connected by suction culvert with first reactor, and second magnetic valve and a COD on-line measurement instrument are connected between the first flow meter and first reactor; Equalizing tank also is connected by suction culvert with second reactor, is connected with magnetic valve and COD on-line measurement instrument on the suction culvert, and the 3rd magnetic valve and the 2nd COD on-line measurement instrument are connected between the first flow meter and second reactor; First reactor water outlet place connects the 3rd COD on-line measurement instrument; Take-off pipe of the outlet pipeline of first reactor connects and enters second reactor, and the water outlet of first reactor is as the water inlet of second reactor, and is connected to the 4th magnetic valve and first impeller pump on this branch line; Second reactor water outlet place connects the 4th COD on-line measurement instrument; Branch line of the outlet pipeline of second reactor connects and enters first reactor, and the water outlet of second reactor is as the water inlet of first reactor, and is connected to the 5th magnetic valve and second impeller pump on this branch line; Another branch line of the first reactor 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 magnetic valve on this branch line successively; Another branch line of second reactor links to each other with water tank, and be connected with the 3rd impeller pump successively on this branch line, the 6th magnetic valve; With water tank is set up in parallel clorox 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 magnetic valve, the 4th under meter, the 11 magnetic valve, the 5th under meter, the 12 magnetic valve, 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 and second reactor respectively by two counter-flushing pipelines respectively again after the lifting of the 5th impeller pump, the counter-flushing pipeline that connects first reactor is provided with the 13 magnetic valve, connect second reactor counter-flushing pipeline be provided with the 14 magnetic valve, the soup of carrying in the counter-flushing pipeline directly enters reactor; First reactor and first reactor are provided with film and purge and supply the dissolved oxygen aerating system.
Establish four membrane modules in each reactor, described film is the polyethylene hollow fiber film.
Film purges and comprises perforated pipe that is positioned at reactor bottom and the Inka aeration pipe of highly locating apart from reactor top 1/3rd for the dissolved oxygen aerating system; First gas blower is connected to the 15 magnetic valve 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; First gas blower also is connected with the 16 magnetic valve 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; Second gas blower is connected to the 17 magnetic valve 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; Second gas blower also is connected with the 18 magnetic valve 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.
The invention provides the aerobic membrane bioreactor of a kind of full automatic control, continuous effluent, processing high concentrated organic wastewater.High concentrated organic wastewater (can be collected lactic acid through needn't can directly entering membrane bioreactor through product methane phase reduction organic concentration behind the acidication behind acidication, do not produce methane, reduce greenhouse gases), and owing to sludge concentration height, hollow-fibre membrane crown_interception in the membrane bioreactor, effluent quality still can reach higher standard.Simultaneously, because alternate run produces the replacement of microorganism 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, (by the on-line monitoring reactor 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, after the reactor that be in underload early stage is transformed into the high loading reactor, be in the organism of digesting and assimilating that the microorganism 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 enter this reactor after the acidication reaction.Organic loading during alternate run in the reactor 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 normally moves another reactor 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 magnetic valve, the water level of Inlet and outlet water, normal reactor 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 directly enter membrane bioreactor behind acidication, the operation for some time after (by the on-line monitoring reactor Inlet and outlet water COD of place, when the COD clearance is 40%, automatically control alternately by robot control system(RCS)) two-stage reactor is alternately, underload reactor originally is as new high loading reactor, 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 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 clorox+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 microorganism 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 clorox alkali lye can not cause the microorganism in the reactor and murder, and the alternate run of alkali cleaning and pickling has guaranteed that the pH value in the reactor is relative constant.
4, during back flushing, soup is entered from the water inlet, and then is aspirated out soup to equalizing tank by impeller pump D or C by impeller pump E suction, together carries out a biological disposal upon with raw waste water subsequently.Like this, the path of flowing through of soup enters inside and then is sucked up to equalizing tank from the membrane module outside, is equivalent to membrane module is immersed 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 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 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, aeration simultaneously during flushing with clean water can wash away the particulate fouling on film surface, 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, film is the polyethylene hollow fiber film.Fixedly the tubular fibre of film vertically places the bottom surface of reactor, and rising pipe connects a header that is parallel at the bottom of the reactor 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, clorox 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, perforated pipe evenly is laid on reactor bottom.Highly locate to establish Inka aeration device---microporous diffuser at reactor 1/3rd, the Inka aeration device interts between five gaps of membrane module.Be respectively first reactor (MBR1) and second reactor (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 realization is to the control of the perforated pipe aerating regulation device aeration rate of Inka aeration device in first and second reactors and bottom.
10, the below of reactor membrane module is provided with blow-down pipe and shore pipe; Top is provided with upflow tube, prevents that reactor 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.
Structure of the present invention is compared with existing membrane bioreactor, and superiority is:
1, the membrane bioreactor alternate run of two-stage series connection, organic loading rate height can bear higher organic loading, and high concentrated organic wastewater can directly enter this aerobic reactor through need not behind the acidication through methanogenic reaction, and water outlet is effective.Avoided that the one-level membrane bioreactor load that causes 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 substantially.
3, adopted the Inka aeration device of Inka aeration theory---two aerating systems of the perforated pipe aerating regulation device of microporous diffuser and bottom, 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 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 MBR1, is connected with valve 2 and the 2nd COD on-line measurement instrument on the suction culvert of the equalizing tank and the first reactor MBR1, and valve 2 and the 2nd COD on-line measurement instrument are connected between the under meter a and the first reactor MBR1.Equalizing tank also is connected by suction culvert with the second reactor MBR2, is connected with a valve 3 and a COD on-line measurement instrument on the suction culvert, and a valve 3 and a COD on-line measurement instrument are connected between the under meter a and the second reactor MBR2.First reactor MBR1 water outlet place connects the 3rd COD on-line measurement instrument.A take-off pipe connection of the outlet pipeline of the first reactor MBR1 enters the second reactor MBR2, and the water outlet of the first reactor MBR1 is connected to valve 4, tensimeter YLB1 and impeller pump A as the water inlet of the second reactor MBR2 on this pipeline.Equally, second reactor MBR2 water outlet place also connects the 4th COD on-line measurement instrument.A branch line connection of the outlet pipeline of the second reactor MBR2 enters the first reactor MBR1, and the water outlet of the second reactor MBR2 is connected to impeller pump B, tensimeter YLB2 and valve 5 as the water inlet of the first reactor MBR1 on this pipeline.Another branch line of the first reactor 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 MBR2 also links to each other with water tank, is connected with tensimeter YLB3, impeller pump C, valve 6 on this pipeline successively, and valve 6 links to each other with under meter b.With water tank is set up in parallel clorox 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 and second reactor respectively by two counter-flushing pipelines respectively again after the impeller pump E lifting, the counter-flushing pipeline that connects first reactor is provided with valve 13, connect second reactor counter-flushing pipeline be provided with valve 14, the soup of carrying in the counter-flushing pipeline directly enters reactor.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 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 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 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 MBR2.
The valve (magnetic valve) of a whole set of reaction unit, impeller pump, under meter, COD on-line measurement instrument 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, mould material is the polyethylene hollow fiber film, and hollow fiber conduit is perpendicular to the reactor bottom surface, and impeller pump is the suction of the header in reactor bottom surface water outlet from lower parallel.The perforated pipe aerating regulation device is installed in the bottom of each reactor, and reactor 1/3rd is highly located the Inka aeration device is installed between membrane module, provides air with gas blower GFJ1 and gas blower GFJ2 for two reactors respectively.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 MBR1 is delivered to the second reactor MBR2 by impeller pump A with water, realizes by automatic control decorum control impeller pump A; The second reactor MBR2 is delivered to the first reactor MBR1 by impeller pump B with water, by the start and stop realization of control impeller pump B.The water outlet of the first reactor MBR1 is delivered to water tank by impeller pump D suction, by the switching realization of by-pass valve control 7; The water outlet of the second reactor 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 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 MBR1 is provided with valve 13, the second reactor MBR2 is provided with valve 14.The soup that enters in the first reactor MBR1 aspirates out reactor and is delivered to equalizing tank with impeller pump D, is provided with valve 9 between the first reactor MBR1 and the equalizing tank; Enter soup in the second reactor MBR2 and aspirate out reactor 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 MBR2 is as the secondary membrane bioreactor with the first reactor MBR1 in elder generation.Open valve 2 valve-offs 3, raw waste water enters the first reactor MBR1.In the first reactor MBR1, microbiological deterioration organic substance, waste water obtain preliminary purification.The second reactor MBR2 is aspirated out and be delivered to the water outlet of the first reactor MBR1 by impeller pump A, organic substance is degraded in the second reactor 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 (by the on-line monitoring reactor Inlet and outlet water COD of place, when the COD clearance is 40%, replace by automatic controlling system), the first reactor MBR1 and second reactor MBR2 exchange working order, the second reactor MBR2 is as the one-level membrane bioreactor, and water inlet directly enters the second reactor MBR2.The water outlet of the second reactor MBR2 is pumped to water inlet place of the first reactor MBR1 by impeller pump B, water outlet after the processing once more of the first reactor 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.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 MBR1 is carried out back flushing, the second reactor 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 enters the second reactor MBR2, through directly aspirating water outlet to water tank by impeller pump C after the biological degradation of the second reactor MBR2.The first reactor 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 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 situations 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 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 MBR1.Subsequently, the first reactor MBR1 begins works better, begins that the second reactor MBR2 is carried out online backflushing and washes.It is the same that the online backflushing of the second reactor 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:
Figure GSA00000129879200091
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), 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 safety, stablize, work efficiently.
To Fig. 3-3, figure is the three-view diagram of membrane module, the long 1.5m of reactor, wide 1.2m, 2.0m in conjunction with Fig. 3-1.Establish four membrane modules in the reactor, film is the polyethylene hollow fiber film, and the spacing between diaphragm is 300mm, length direction upper diaphragm and reactor be spaced apart 300mm; The wide 700mm of membrane module, membrane module and reactor interval 250mm on the width; The high 1200mm of membrane module, apart from reactor upper end 500mm, membrane module lower central place is provided with the water outlet of header collection 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; Be not uniform-distribution with four aeration arms on the main every 400mm, 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, apart from reactor lower end 1100mm, gas blower GFJ1 or gas blower GFJ2 connect the aeration house steward, 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/ 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 enter 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, second reactor, equalizing tank, under meter, magnetic valve, 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 magnetic valve and first flow meter; Equalizing tank is connected by suction culvert with first reactor, and second magnetic valve and a COD on-line measurement instrument are connected between the first flow meter and first reactor; Equalizing tank also is connected by suction culvert with second reactor, is connected with magnetic valve and COD on-line measurement instrument on the suction culvert, and the 3rd magnetic valve and the 2nd COD on-line measurement instrument are connected between the first flow meter and second reactor; First reactor water outlet place connects the 3rd COD on-line measurement instrument; Take-off pipe of the outlet pipeline of first reactor connects and enters second reactor, and the water outlet of first reactor is as the water inlet of second reactor, and is connected to the 4th magnetic valve and first impeller pump on this branch line; Second reactor water outlet place connects the 4th COD on-line measurement instrument; Branch line of the outlet pipeline of second reactor connects and enters first reactor, and the water outlet of second reactor is as the water inlet of first reactor, and is connected to the 5th magnetic valve and second impeller pump on this branch line; Another branch line of the first reactor 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 magnetic valve on this branch line successively; Another branch line of second reactor links to each other with water tank, and be connected with the 3rd impeller pump successively on this branch line, the 6th magnetic valve; With water tank is set up in parallel clorox 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 magnetic valve, the 4th under meter, the 11 magnetic valve, the 5th under meter, the 12 magnetic valve, 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 and second reactor respectively by two counter-flushing pipelines respectively again after the lifting of the 5th impeller pump, the counter-flushing pipeline that connects first reactor is provided with the 13 magnetic valve, connect second reactor counter-flushing pipeline be provided with the 14 magnetic valve, the soup of carrying in the counter-flushing pipeline directly enters reactor; First reactor and first reactor 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, described 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 comprises perforated pipe that is positioned at reactor bottom and the Inka aeration pipe of highly locating apart from reactor top 1/3rd for the dissolved oxygen aerating system; First gas blower is connected to the 15 magnetic valve 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; First gas blower also is connected with the 16 magnetic valve 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; Second gas blower is connected to the 17 magnetic valve 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; Second gas blower also is connected with the 18 magnetic valve 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.
CN2010101799051A 2010-05-24 2010-05-24 Alternate two-stage aerobic membrane bioreactor Expired - Fee Related CN101830607B (en)

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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

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