CN201305510Y - Lateral flow type membrane bioreactor device - Google Patents
Lateral flow type membrane bioreactor device Download PDFInfo
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- CN201305510Y CN201305510Y CNU2008201237584U CN200820123758U CN201305510Y CN 201305510 Y CN201305510 Y CN 201305510Y CN U2008201237584 U CNU2008201237584 U CN U2008201237584U CN 200820123758 U CN200820123758 U CN 200820123758U CN 201305510 Y CN201305510 Y CN 201305510Y
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Abstract
The utility model provides a lateral flow type membrane bioreactor device. The device orderly comprises an adjusting tank (10-2), at least one first bioreactor (20-0) and an ultrafiltration system (40-0), wherein the first bioreactor (20-0) comprises a first aerobic tank (20-2), a first anoxic tank (20-4) and a first anaerobic tank (20-6), and the ultrafiltration system (40-0) further comprises an ultrafiltration device (40-0-0) and an ultrafiltration backwash water tank (40-10-4); a gas recoil pipe (40-8-30) is arranged in the center of a membrane tube (40-8-64), and a nontransparent baffle is arranged between the membrane tube (40-8-64) and a filtered water collecting bin (40-8-48); a plurality of U-shaped hollow fiber membranes (40-8-10) are tightly arranged between the inner wall of the hollow membrane tube (40-8-64) and the outer wall of the gas recoil pipe (40-8-30) and encapsulated in membrane tube (40-8-64) in a mode that the openings faces downwards, and forms a dirt storing bin (40-8-40) with the hollow fiber membrane. The utility mode utilizes at least one lateral flow type membrane bioreactor device and a lateral flow type membrane ultrafiltration device which comprises a gas recoil system, a gas and water joint recoil system and a chemical membrane scavenger system so as to achieve combined sewage disposal.
Description
Technical field
The utility model relates to a kind of waste disposal plant, more particularly, relates to a kind of lateral flow type membrane bioreactor (MBR) device that utilizes.
Background technology
China is a lack of water country, and sewage disposal and reuse thereof are the effective measure of development and use water resources." middle water " reuse is with after the processing of municipal effluent by equipment such as membrane bioreactors, uses it for greening, flushing, replenishes the non-purposes of drinking such as make up water of viewing and admiring water body, industrial circulating water; And the purposes that the cleaning water of further advanced treatment be can be used for drinking contour water quality requirement.Municipal effluent can get nearby, has removed long distance water transfer from, and it is removed significantly at processed pollutent afterwards, has so not only saved water resources, has also reduced environmental pollution." middle water " reuse is extensively employing of the area of many lacks of water in the world, is considered to have significant social, environment and economic benefit.
Membrane technology is based on the water treatment new technology of separation membrane.The engineering of membrane separation technique is used the sea water desaltination that starts from the sixties in 20th century.After, along with the continuous appearance of various new membrane, membrane technique also progressively expands to urban life drink water purifying and municipal sewage treatment, and field such as medicine, food, biotechnology.In water globe resource scarcity, contaminated serious day by day today, membrane technique obtains application more and more widely as a kind of novel reclaimed water reuse technology.
The initial application of membrane technique in municipal sewage treatment is to utilize ultra-filtration membrane to replace the second pond that traditional wastewater is handled, and obtained fabulous water quality effect.But membrane technique was at an early stage of development at that time, and film costs an arm and a leg, and the life-span is short, and the energy consumption height is difficult to be applied widely.
The eighties in 20th century, along with the development of membrane technique and perfect, membrane bioreactor (MBR) begins to introduce the processing of municipal effluent and garbage loading embeading percolation liquid.This integrated form new technology of combined is that the high efficient separation technology of the biological degradation of active sludge biological reactor and film is melted into a whole, and has characteristics such as effluent quality is good and stable, the processing load is high, the plant area area is little, sludge output is little, operational administrative is simple.
Membrane technique in the development of the later stage nineties rapidly; after particularly entering 21 century; the equipmentization of mass-producing, membrane module and the treating product thereof of producing along with mould material and integrated; the universalness and the price of film device production technology are popular, and the development of membrane technique has been developed rapidly from breadboard potential technology becomes the engineering practical technique.In many heavy constructions are used, use, and can compete mutually with conventional art.
From late 1990s till now, MBR develops towards the direction of more combining closely with various new mud technologies from simple aerobic type.The novel process that has occurred comprises: AO type MBR, A
2O type MBR, sequence batch (MBR etc.The appearance of these new membrane bio-reactors makes ammonia nitrogen, total phosphorus, the total nitrogen in degrading high concentration sewage and the draining of control big yield become possibility.
Along with the fast development of industry and the continuous expansion of city size, to there be increasing municipal effluent to handle, municipal effluent is the major reason of present rivers and lakes water pollution, be the major cause of the many urban sustainable developments of restriction, thereby the effective treating method of sewage has become the difficult problem that people need to be resolved hurrily.
Film-bioreactor (Membrane-Bioreactor, abbreviation MBR) technology is a kind of new and effective sewage disposal and advanced treatment recycling technique with membrane separation technique and the combination of traditional wastewater biological treatment, its origin is to carry out solid-liquid separation with the second pond that membrane separation technique replaces in the activated sludge process, obtain extensive concern day by day at international water-treatment technology field in recent years, in the domestic reused water processing engineering of China, also obtained bigger promotion and application.By with the integration of biological treatment, make MBR technology have good denitrogenation and phosphorus removal functional:
1.MBR technology has good denitrification functions: the effect of efficiently damming of film, making microorganism dam fully and be all-trans is fed in the reactor, realized separating fully of the reactor waterpower residence time (HRT) and sludge age (SRT), help breeding damming, grow and breeding of nitrobacteria slowly, system's nitrification efficiency height, simultaneously because the effect of efficiently damming of film can be kept higher sludge concentration in the reactor, make the carbonization efficient of system, denitrification efficient very high.
2.MBR technology has good phosphorus removal functional: because film is to the holding back of suspended solids (SS) nearly 100%, the water outlet of film system contains SS hardly, and this just is trapped in the phosphorus in the particle in the system well.In addition, because the complete crown_interception of MBR and replacing by anaerobism, aerobic environment, polyP bacteria will obtain enrichment easilier, polyP bacteria discharges the decomposition of the phosphorus in the poly-phosphate (Poly-p) in anaerobic environment, essential energy is provided, and the organism that absorbs easily degraded also will be stored in the cell with poly-beta-hydroxy-butanoic acid (pHB); In aerobic processes, polyP bacteria utilizes intravital poly-beta-hydroxy-butanoic acid (pHB), excessively be absorbed in quantitatively considerably beyond the synthetic required phosphorus amount of its cell, phosphorus is housed in the thalline with the form of poly-phosphate and forms high phosphorus sludge, usually the excess sludge phosphorus content of MBR system is higher 1.2～1.5 times than traditional dephosphorization process, like this, even MBR has longer SRT, also can obtain goodish phosphor-removing effect.
From late 1990s till now, MBR develops towards the direction of more combining closely with various new mud technologies from simple aerobic type.The appearance of these new membrane bio-reactors makes ammonia nitrogen, total phosphorus, the total nitrogen in degrading high concentration sewage and the draining of control big yield become possibility.
On its mode of operation, also develop towards the lateral flow type direction of more can the reasonable use active sludge and being more suitable for engineered reconstruction from finishing immersion that mud holds back merely.Because film device is the important component part of MBR, and the development of a lot of novel MBR is closely related with the development of so-called dead end membrane module technology.
Before this, usually use and utilize the downflow system biofilm filtering device of proportion greater than the single filter material of water (proportion of water is 1.0), thereby the removal of solid matter can only occur in the filtering basin surface, loss of head takes place and causes filtering the time length and shorten in solid matter on the surface rapidly because dam, and for the solid matter of removing overflow need frequently carry out back flushing, so cause operation often to be interrupted, occur the problem that the back flushing water yield increases simultaneously.
In order to address the above problem, people develop a kind of downflow system multi-layer biological membrane filter appts.This downflow system multi-layer biological membrane filter appts has the filtering layer elevated thickness, filters the advantage of the time lengthening that continues.
In recent years, begin the device of biofilm filtering device as denitrogenation used.Because the denitrogenation speed of downflow system denitrogenation filtration unit is fast and removal effect solid matter is good, so obtained being extensive use of.Yet, this downflow system denitrification biomembrane filtration unit, the discharge direction of the nitrogen that produces during denitrogenation (reacting according to following chemical equation) is opposite with the direction of current, nitrogen is dammed in filter material layer, the effect identical with solid matter appears, make loss of head sharply increase (referring to Fig. 2, Fig. 2 is the current floe condition synoptic diagram of nitrogen in the downflow system denitrogenation is filtered).Therefore, under downflow system biofilm filtering device condition, in order to remove the nitrogen that dams in filtrate, the operation that need often outgas, thus can't finish continuous operation, and have the air capacity of back flushing and the shortcoming that the water yield increases.
1/5NO
3 -+ 6/5H
++ e
-→ 1/10N
2+ 3/5H
2O (chemical equation)
In order to address the above problem, United States Patent (USP) the 6th, 605, also disclosed a kind of upper-flowing multi-layer biofilm filtration unit 216 B1 numbers, but owing to used the proportion filtrate bigger, therefore be provided with and be used to prevent because of adopting the filtrate expansible device that upflowing causes and be used to the filtrate expansible mechanism that prevents that back flushing from causing, thereby make the running technology complexity that becomes than water, and this device can only can't realize removing by nitrated and denitrogenation the effect of nitrogen as simple filtration unit.
For this reason, the open CN 1834033A of Chinese patent application discloses and has a kind ofly utilized upper-flowing multi-layer biofilm to filter and the formula growth combination process that swims, and is used for removing the organism of denitrification, phosphorus, difficult degradation and reduces colourity.This combination process is applicable to the advanced treatment of sewage, particularly can filter purifying waste water, thereby guarantee the quality of water outlet.
Fig. 1 is the sewerage advanced treatment process schema of CN 1834033A;
This sewage water advanced treatment apparatus comprises: anaerobic pond 201, first anoxic pond 202, second anoxic pond 203, Aerobic Pond 204, settling tank 205, contact tank 206 and biofilm filtering device 207, fixed filtrate 204a wherein is set with the reinforcement nitrification in Aerobic Pond 204, and biofilm filtering device 207 is the upflowing biofilm filtering device.
Wherein, fixed filtrate 204a is made by polyethylene, is arranged on the bottom of Aerobic Pond 204, and loadings is 30% of Aerobic Pond 204 cumulative volumes, and wherein fixed filtrate 204a is the cilium shape, and specification is that the wide 200mm of being, length are 750mm, and proportion is 1.2g/cm
3, tensile strength is 700kg/20cm.
But above-mentioned utilize upper-flowing multi-layer biofilm to filter and the sewage water advanced treatment apparatus of the formula growth combination process that swims is a fixed configurations, can't arrange in pairs or groups flexibly, therefore have certain defective according to water quality needs and site requirements.
In general, existing MBR is immersion MBR basically, though with most of traditional activated sludge processes mutually specific energy consumption decrease, its energy consumption is still very high; The present built-in film immersion MBR that generally adopts, its film system only plays isolating against the current effect, and can not play the regulating and controlling effect to active sludge; The pollution problem of film is an insoluble problem all the time, though employing cross-flow technology can reduce the pollution of film, required technical equipment complexity, energy consumption height to a certain extent; Film maintenance process complexity is had relatively high expectations to equipment, Personnel Skill Levels, generally needs to stop work to safeguard; Unnecessary sludge discharge is bigger; And cost and running cost are also higher.
For solving the defective that existing waste disposal plant exists, the utility model provides a kind of method of utilizing lateral flow type membrane bioreactor (MBR) to install and utilize this device to dispose of sewage.
The utility model content
At the defective that prior art exists, the purpose of this utility model is to provide a kind of organism and reduction colourity of utilizing lateral flow type membrane bioreactor device to be used to remove COD, BOD, SS and nitrogen, phosphorus, difficult degradation.This combination process is applicable to the advanced treatment of sewage, thereby has guaranteed the quality of water outlet.
An aspect of the present utility model provides a kind of lateral flow type membrane bioreactor device, comprise successively: equalizing tank, at least one first bio-reactor, ultrafiltration system, wherein, described first bio-reactor comprises first Aerobic Pond, first anoxic pond, first anaerobic pond, it is characterized in that: described ultrafiltration system further comprises the membrane ultrafiltration device, ultrafiltration recoil water pot, described membrane ultrafiltration device has the film tube of hollow, be provided with the gas backwash pipe at described film tube center, below described film tube, be provided with the percolation water collecting bin, has the opacity dividing plate between described film tube and the described percolation water collecting bin, a plurality of U type hollow-fibre membranes closely are arranged between the outer wall of the inwall of film tube of described hollow and described gas backwash pipe and Open Side Down is packaged in the described film tube, the U type opening of described a plurality of U type hollow-fibre membranes is enclosed in the described percolation water collecting bin by the opacity dividing plate, space between the film tube of described a plurality of U type hollow-fibre membrane U type upper end that Open Side Down and described hollow forms dust storage cabin, above described film tube, be provided with water-in and/or recoil mixture export, below described film tube, be provided with water outlet and/or the import of recoil mixed solution; Also have in described first bio-reactor by described first Aerobic Pond and in the described first anoxic pond flow process, form the device that the part water body refluxes, in described first Aerobic Pond and described first anoxic pond, and the top of the dividing plate between described first anoxic pond and described first anaerobic pond forms overflow, flow into the membrane ultrafiltration device of described ultrafiltration system through the ultrafiltration service pump by the effusive liquid of described first anaerobic pond, backflow through the effusive recoil mixed solution of described recoil mixture export and to get back to described first Aerobic Pond of described first bio-reactor, described first Aerobic Pond further comprises first inlet pipe that has first gas distributor.
Preferably, described device further comprises second bio-reactor, optional second Aerobic Pond that comprises of described second bio-reactor, second anoxic pond, second anaerobic pond, also have in wherein said second bio-reactor by described second Aerobic Pond and in described second anoxic pond or the described second anaerobic pond flow process, form the device that the part water body refluxes, the described recoil mixed solution import of described membrane ultrafiltration device links to each other with ultrafiltration recoil water pot, wherein said gas backwash pipe coupling has gas blower, described equalizing tank is an anaerobic pond, described second Aerobic Pond further comprises second inlet pipe that has second gas distributor, described first gas distributor and second gas distributor enter first and second Aerobic Ponds with pressurized air in the exit of described first inlet pipe and optional described second inlet pipe and carry out aeration, the sewage that flows into the described membrane ultrafiltration device of described ultrafiltration system through the ultrafiltration service pump comes the effusive liquid of free described second anaerobic pond, backflow through the effusive recoil mixed solution of described recoil mixture export and to get back to described first Aerobic Pond or optional described second Aerobic Pond, described first gas distributor away from described first anoxic pond optional second gas distributor away from optional described second anoxic pond.
More preferably, described first gas distributor and second gas distributor with pressurized air described first inlet pipe and optionally the exit of described second inlet pipe throw away along the tangential direction of the described first and second inlet pipe internal diameter each points.
Preferably, described device further comprises the 3rd biological reactor, optional the 3rd Aerobic Pond, the 3rd anoxic pond, the 3rd anaerobic pond of comprising of the described the 3rd biological reactor also has the device that is formed the backflow of part water body by described the 3rd Aerobic Pond in described the 3rd anoxic pond or the 3rd anaerobic pond flow process in the wherein said the 3rd biological reactor; And optional the 4th bio-reactor that comprises, optional the 4th Aerobic Pond, the 4th anoxic pond, the 4th anaerobic pond of comprising of described the 4th bio-reactor, also have the device that is formed the backflow of part water body by described the 4th Aerobic Pond in described the 4th anoxic pond or the 4th anaerobic pond flow process in wherein said the 4th bio-reactor, the sewage that flows into the described membrane ultrafiltration device of described ultrafiltration system through described ultrafiltration service pump comes free described the 3rd anaerobic pond or the effusive liquid of the 4th anaerobic pond.
Preferably, the device that is formed the backflow of part water body by described first Aerobic Pond in the described first anoxic pond flow process is the slit that the dividing plate below between described first Aerobic Pond and described first anoxic pond has, being used for forming between described first Aerobic Pond and described first anoxic pond part water body refluxes, the device that is formed the backflow of part water body by described second Aerobic Pond in described second anoxic pond or the described second anaerobic pond flow process is the slit that the dividing plate below between optional described second Aerobic Pond that comprises of described second bio-reactor and described second anoxic pond or described second anaerobic pond has, and is used for forming the part water body at flow process and refluxes.
Preferably, described first bio-reactor, described second bio-reactor, the described the 3rd biological reactor, the reaction conditions of each Aerobic Pond in described the 4th bio-reactor, each anoxic pond, each anaerobic pond can be identical, also can be different, the sewage situation that described reaction conditions is handled according to desire be decided.
Preferably, further comprise the device that makes mixed-liquor return that recoil produces behind the described membrane ultrafiltration device described first Aerobic Pond to described first bio-reactor.
Preferably, described first bio-reactor, described second bio-reactor, optionally the described the 3rd biological reactor, optional described the 4th bio-reactor bio-reactor assembly that is an integral body.
Preferably, described first bio-reactor, described second bio-reactor, optional the described the 3rd biological reactor, optional described the 4th bio-reactor are to be connected together by independent component string.
Preferably, the described water outlet that is provided with of the below by the described film tube water displacement after treatment of discharging equates with the water yield of the sewage that enters described the first bio-reactor at least.
Preferably, this lateral flow type membrane bioreactor device, further comprise Controlling System, be used for controlling treatment time, the liquid backwash time of described membrane ultrafiltration device and the gas backwash time of described film tube of raw waste water in the treatment time of described first Aerobic Pond of described at least the first bio-reactor, first anoxic pond, first anaerobic pond, membrane ultrafiltration device at described ultrafiltration system, and above-mentioned each switching between handling.
Preferably, the switching between wherein said each treatment time and each processing presets according to raw water quality with to handling the back requirements in water quality.
Preferably, the switching between wherein said each treatment time and each processing is manually to control according to actual needs.
Preferably, treatment time and the treatment time in the membrane ultrafiltration device of described ultrafiltration system of wherein said raw waste water in described at least the first bio-reactor, follow the gas backwash time of described film tube, then described membrane ultrafiltration device the combined water and air backwash equal time and above-mentioned each switching between handling all is according to raw water quality and the needs of the water quality that requires after handling preset.
More preferably, treatment time and the treatment time in the membrane ultrafiltration device of described ultrafiltration system of wherein said raw waste water in described at least the first bio-reactor, follow the gas backwash time of described film tube, then described membrane ultrafiltration device the combined water and air backwash equal time and above-mentioned each switching between handling all is according to raw water quality and the needs of the water quality that requires after handling preset.
Preferably, the aperture of described a plurality of U type hollow-fibre membranes is 0.01-1 μ m.
Preferably, described a plurality of U type hollow-fibre membranes are that internal diameter is that 1mm, external diameter are the hollow tubular tunica fibrosa of 2mm, and the aperture of described tunica fibrosa is 0.01～0.1 μ m.
Preferably, described slit is that 200～300mm is wide.
Preferably, described ultrafiltration service pump is a water transfer pump.
Preferably, comprise a pump, be used for the mud from least the first bio-reactor backflowed and get back to the Aerobic Pond of at least the first bio-reactor in the outlet of at least the first bio-reactor of this lateral flow type membrane bioreactor device.More preferably, this pump is a water transfer pump.
According to lateral flow type membrane bioreactor device of the present utility model and utilize the lateral flow type sewage water treatment method of the lateral flow type membrane bioreactor device of utility model to have following advantage: lateral flow type membrane bioreactor device of the present utility model (MBR) and to utilize its lateral flow type sewage water treatment method be a kind of novel sewage disposal technology that the high performance membrane isolation technique is combined with activated sludge process, it is the technology that sewage " second-stage treatment technology " and " tertiary treatment technology " are united two into one, system advantage with " 1+1〉2 ", can be used for the higher city of the organic content Industrial Wastewater Treatment of having stable political situation, is typical case's representative of present water treatment high-end technology.
Description of drawings
Above-mentioned purpose of the present utility model and advantage will become more apparent by the reference accompanying drawing to its detailed description of preferred embodiment, wherein:
Fig. 1 is the sewerage advanced treatment process schema of CN 1834033A;
Fig. 2 is the current floe condition synoptic diagram of nitrogen in the downflow system denitrogenation is filtered;
Fig. 3 is the structural principle synoptic diagram of lateral flow type membrane bioreactor device of the present utility model;
Fig. 4 is the sectional side elevation of the membrane ultrafiltration device in the lateral flow type membrane bioreactor device shown in Figure 3;
Fig. 5 is the enlarged view of the single U type hollow-fibre membrane (40-8-10) in the membrane ultrafiltration device shown in Figure 4.
Embodiment
The compound membrane bioreactor of effluent (MBR) technology and explanation of nouns
Effluent---distinguish mutually with activity sludge reflux, in the utility model, be meant: in the water body operational process, have the branch with water body overall operation direction different (or opposite), and this branch implements unity feedback or total reflux (perhaps or scarce backflow) process.In sewage water treatment method operational process of the present utility model, there are two kinds of effluents: 1. separating of hyperfiltration membrane assembly and muddy water, realize the unity feedback of muddy water mixed solution of high density or total reflux (perhaps or lack reflux) by recoil to ultra-filtration membrane; 2. in bio-reactor part, " circulation " of the part water body feedback that water body is formed in the flow process of oxygen-starved area by aerobic zone, i.e. partial reflux.
Compound---in the utility model, be meant: in two or more bio-reactors, select as required the whole of aerobic, anoxic, anaerobic reaction or (promptly part repeats, and the order of each several part can be adjusted) multistage reruning, to reach better biochemical degradation and the row's of denitrogenating phosphorus effect.
Lateral flow type membrane bioreactor device---in the utility model, may be interpreted as: lateral flow type membrane bioreactor device (MBR)=bio-reactor+membrane filter plant (or membrane ultrafiltration device)+recoil program and the mixed solution feedback that is produced and the effluent of unity feedback (effluent)+biochemical reaction process.
Membrane ultrafiltration device in the lateral flow type membrane bioreactor device---in the utility model, be meant by the fixed sealing dress to be placed on the device (referring to Fig. 4) that the hollow fiber ultrafiltration membrane in the plastic tube tube (being the film tube) constitutes.
Dust storage cabin (storage hopper dredger or sludge bin)---be meant that in the utility model U type hollow fiber ultrafiltration membrane (being also referred to as the film silk) is placed in the film tube with inverted U type encapsulation, the cavity that reserves between its U type top and the film tube is used for the usefulness (referring to Fig. 4) of buffer storage mud.
Term " alternatively (or optionally) "---be meant that in this application thereafter process or key element or parts can take place or not take place or can exist or not exist.
Term " treating pond " is meant " Aerobic Pond ", the general name of " anoxic pond " or " anaerobic pond " in arbitrary bio-reactor, can represent as required above-mentioned any one.
Term " or lacking backflow " is relative with " total reflux ", is meant partial reflux but not total reflux.
The principle of work of lateral flow type MBR device
1. in the utility model, former water (being the water that comes of sewage) is squeezed into by water transfer pump under certain pressure after at least the first bio-reactor and biological group contacts (promptly by aeration tank, anoxic pond or anaerobic pond) and is passed through ultrafiltration membrance filter in the filtering system (or ultrafiltration system), has realized mud-water separation.Water after the filtration is by reuse or discharging, and active sludge is trapped within the storage hopper dredger that U type hollow fiber ultrafiltration membrane and the space between the film tube by back-off constitute or attached to the outside surface of filtering membrane.
2. in the utility model,, make sedimentary active sludge in backwashing water and the membrane ultrafiltration device (comprising in the dust storage cabin and the active sludge of film surface adhesion) form spissated mixed solution effluent by recoil.And realize the circulation of mud by the effluent unity feedback.The effect of efficiently damming of film, make microorganism dam fully and feed back in first bio-reactor, realized that separating fully of interior hydraulic detention time (HRT) of bio-reactor and sludge age (SRT) is also adjustable, that is to say, the incubation time of the mushroom in the active sludge is the summation of the residence time in each bio-reactor, has shortened the incubation time of the mushroom in the active sludge indirectly.
3. in the utility model, enter the sewage quantity of bio-reactor and water displacement after treatment can equate.And the active sludge that filtering separation is come out before the water outlet can satisfy replenishing of the required active sludge of degraded water inlet by the effluent total reflux.Therefore, lateral flow type membrane bioreactor device has been realized mud quantitatively control or total reflux substantially.And in the prior art, be to reach required flora concentration by constantly replenishing active sludge again, because active sludge is the carrier of required flora.
4. the mixed-liquor return effect in the oxidation ditch of the effect of effluent of the present utility model and general waste disposal plant has some similarity, but the active sludge that the effluent in the utility model can allow the planner to come the reuse effluent to be brought as required more neatly.As: can be used for whole bioprocesses as required, or certain or some link in the process, thereby can be as required and AO of the prior art, A
2The new biological reactor process of O, AOA etc. and multistage degraded is combined into required MBR.
5. lateral flow type MBR of the present utility model can strengthen whole bioprocesses by synchronous nitration-denitrification, does not need to pursue very high sludge concentration (MLSS), but can remove COD, BOD, ammonia nitrogen, phosphorus etc. effectively.
Below, utilize lateral flow type membrane bioreactor device and utilize the sewage water treatment method of this device to be described in detail of the present utility model with reference to the accompanying drawings.
Fig. 3 is the structural principle synoptic diagram of lateral flow type membrane bioreactor device of the present utility model; Fig. 4 is the sectional side elevation of the membrane ultrafiltration device in the lateral flow type membrane bioreactor device shown in Figure 3.
As shown in Figure 3 and Figure 4, in an embodiment, lateral flow type membrane bioreactor device of the present utility model, comprise successively: equalizing tank 10-2, at least one first bio-reactor 20-0, ultrafiltration system 40-0, wherein, the first bio-reactor 20-0 comprises the first Aerobic Pond 20-2, the first anoxic pond 20-4, the first anaerobic pond 20-6, wherein ultrafiltration system 40-0 further comprises membrane ultrafiltration device 40-0-0, ultrafiltration recoil water pot 40-10-4, described membrane ultrafiltration device 40-0-0 has the film tube 40-8-64 of hollow, be provided with gas backwash pipe 40-8-30 at film tube 40-8-64 center, below film tube 40-8-64, be provided with percolation water collecting bin 40-8-48, has the opacity dividing plate between film tube 40-8-64 and the percolation water collecting bin 40-8-48, a plurality of U type hollow-fibre membrane 40-8-10 closely are arranged between the outer wall of the inwall of film tube 40-8-64 of hollow and gas backwash pipe 40-8-30 and Open Side Down is packaged among the film tube 40-8-64, the U type opening of a plurality of U type hollow-fibre membrane 40-8-10 is enclosed in the described percolation water collecting bin 40-8-48 by the opacity dividing plate, space between the film tube 40-8-64 of a plurality of U type hollow-fibre membrane 40-8-10 U type tops that Open Side Down and hollow forms dust storage cabin 40-8-40, above film tube 40-8-64, be provided with water-in 40-8-80 and/or recoil mixture export 40-8-90, below film tube 40-8-64, be provided with water outlet 40-8-50 and/or recoil mixed solution import 40-8-60; Also has the device that in the described first anoxic pond 20-4 flow process, forms part water body backflow 20-14 by the described first Aerobic Pond 20-2 among the first bio-reactor 20-0, at the first Aerobic Pond 20-2 and the first anoxic pond 20-4, and first dividing plate top between anoxic pond 20-4 and the first anaerobic pond 20-6 form overflow, flow into the membrane ultrafiltration device 40-0-0 of ultrafiltration system 40-0 through ultrafiltration service pump 40-2 by the effusive liquid of the first anaerobic pond 20-6, backflow through recoil mixture export 40-8-90 effusive recoil mixed solution and to get back to the first Aerobic Pond 20-2 of the first bio-reactor 20-0, the first Aerobic Pond 20-2 further comprises the first inlet pipe 20-8 that has the first gas distributor 20-20.
In a preferred embodiment, lateral flow type membrane bioreactor device of the present utility model, further comprise the second bio-reactor 30-0, the second bio-reactor 30-0 comprises the second Aerobic Pond 30-2, the second anoxic pond 30-4, the second anaerobic pond 30-6, wherein also has the device that in the second anoxic pond 30-4 or the second anaerobic pond 30-6 flow process, forms part water body backflow 30-14 by the second Aerobic Pond 30-2 among the second bio-reactor 30-0, the recoil mixed solution import 40-8-60 of membrane ultrafiltration device 40-0 links to each other with ultrafiltration recoil water pot 40-10, wherein gas backwash pipe 40-8-30 is connected with gas blower 40-24, equalizing tank 10-2 is with the function of anaerobic pond, the second Aerobic Pond 20-2 further comprises the second inlet pipe 30-8 that has the second gas distributor 30-20, the first gas distributor 20-20 and the second gas distributor 30-20 enter first and second Aerobic Ponds with pressurized air in the exit of described first inlet pipe 20-8 and the described second inlet pipe 30-8 and carry out aeration, tangential direction along the first and second inlet pipe internal diameter each points throws away, the sewage that flows into the membrane ultrafiltration device 40-0-0 of ultrafiltration system 40-0 through ultrafiltration service pump 40-2 comes the effusive liquid of the free second anaerobic pond 30-6, backflow through recoil mixture export 40-8-90 effusive recoil mixed solution and to get back to the first Aerobic Pond 20-2 or the second Aerobic Pond 30-2, the first gas distributor 20-20 away from the first anoxic pond 20-4 the second gas distributor 30-20 away from the second anoxic pond 30-4.In a more preferred embodiment, the first gas distributor 20-20 and the second gas distributor 30-20 throw away in the exit of the first inlet pipe 20-8 and the second inlet pipe 30-8 pressurized air and enter first and second Aerobic Ponds and carry out aeration along the tangential direction of the first and second inlet pipe internal diameter each points.
In another preferred embodiment, device of the present utility model further comprises the 3rd biological reactor, the 3rd biological reactor comprises the one or more treating ponds that are selected from the group that is made of the 3rd Aerobic Pond, the 3rd anoxic pond, the 3rd anaerobic pond, also has in the wherein said the 3rd biological reactor by described the 3rd Aerobic Pond to form the device that the part water body refluxes in described the 3rd anoxic pond or the 3rd anaerobic pond flow process.
In another preferred embodiment, device of the present utility model further comprises the 4th bio-reactor, described the 4th bio-reactor is selected from by the one or more treating ponds that comprise in the group that the 4th Aerobic Pond, the 4th anoxic pond, the 4th anaerobic pond constitute, and also has in wherein said the 4th bio-reactor by described the 4th Aerobic Pond to form the device that the part water body refluxes in described the 4th anoxic pond or the 4th anaerobic pond flow process.
In a preferred embodiment, the device that is formed part water body backflow 20-14 by the first Aerobic Pond 20-2 in the first anoxic pond 20-4 flow process is the slit that the dividing plate below between the first Aerobic Pond 20-2 and the first anoxic pond 20-4 has, be used between the first Aerobic Pond 20-2 and the first anoxic pond 20-4, forming part water body backflow 20-14, the device that is formed part water body backflow 30-14 by the second Aerobic Pond 30-2 in the second anoxic pond 30-4 or the second anaerobic pond 30-6 flow process is the slit that the dividing plate below between the optional second Aerobic Pond 30-2 that comprises of the second bio-reactor 30-0 and the second anoxic pond 30-4 or the second anaerobic pond 30-6 has, be used for forming part water body backflow 30-14 at flow process, wherein the tangential direction along the first and second inlet pipe internal diameter each points throws away in the exit of the first inlet pipe 20-8 and the optional second inlet pipe 30-8 with pressurized air for the first gas distributor 20-20 and the second gas distributor 30-20.
Those skilled in the art should understand that, at least one first bio-reactor 20-0, the second bio-reactor 30-0, the 3rd biological reactor, the 4th bio-reactor, and more bio-reactor can be provided with as required, and the situation of the sewage that Aerobic Pond wherein, anoxic pond, anaerobic pond also can be handled as required comprises whole Aerobic Ponds, anoxic pond, anaerobic pond or partially disposed pond wherein, and wherein the order of each treating pond can be exchanged.
In another preferred embodiment, device of the present utility model, the first bio-reactor 20-0 wherein, the second bio-reactor 30-0, the 3rd biological reactor, the reaction conditions of each Aerobic Pond in the 4th bio-reactor, each anoxic pond, each anaerobic pond can be identical, also can be different, and the sewage situation that described reaction conditions is handled according to desire is decided.
In another preferred embodiment, lateral flow type membrane bioreactor device of the present utility model further comprises the device that makes mixed-liquor return that recoil produces behind the described membrane ultrafiltration device 40-0-0 described first Aerobic Pond 20-2 to the described first bio-reactor 20-0.
In a preferred embodiment, lateral flow type membrane bioreactor device of the present utility model, the bio-reactor assembly that the wherein said first bio-reactor 20-0, the described second bio-reactor 30-0, optional the described the 3rd biological reactor, optional described the 4th bio-reactor are an integral body.
In another preferred embodiment, lateral flow type membrane bioreactor device of the present utility model, the wherein said first bio-reactor 20-0, the described second bio-reactor 30-0, optional the described the 3rd biological reactor, optional described the 4th bio-reactor are to be connected together by independent component string.
In another preferred embodiment, lateral flow type membrane bioreactor device of the present utility model, wherein the described water outlet 40-8-50 that is provided with of the below by the described film tube 40-8-64 water displacement after treatment of discharging equates with the water yield of the sewage 10-6 that enters the described the first bio-reactor 20-0 at least.
In another preferred embodiment, lateral flow type membrane bioreactor device of the present utility model, further comprise Controlling System, be used for controlling treatment time, the liquid backwash time of membrane ultrafiltration device 40-0-0 and the gas backwash time of film tube 40-8-64 of raw waste water 10-4 in the treatment time of the first Aerobic Pond 20-2 of at least the first bio-reactor 20-0, the first anoxic pond 20-4, the first anaerobic pond 20-6, membrane ultrafiltration device 40-0-0 at ultrafiltration system 40-0, and above-mentioned each switching between handling.
In a preferred embodiment, the switching between wherein said each treatment time and each processing presets according to raw waste water water quality with to handling the back requirements in water quality.
In another preferred embodiment, the switching between wherein said each treatment time and each are handled is according to manually control of actual needs.
In a preferred embodiment, lateral flow type membrane bioreactor device of the present utility model, wherein the treatment time of raw waste water 10-4 in the described at least the first bio-reactor 20-0 set according to water quality requirement with the treatment time in the membrane ultrafiltration device 40-0-0 of described ultrafiltration system 40-0, for example the treatment time in the described at least the first bio-reactor 20-0 can be 10～20 hours, following the gas backwash time of described film tube 40-8-64 sets according to water quality requirement, it for example is 0.5～2 minute, preferred 30 seconds, the time of the dynamic hydraulic combined back flushing that the liquid backwash of described then membrane ultrafiltration device 40-0-0 and described film tube 40-8-64 carry out is simultaneously also set according to water quality requirement, it for example is 0.5～2 minute, preferred 30 seconds, and the switching between above-mentioned each processing presets.
In a preferred embodiment, the aperture of a plurality of U type hollow-fibre membrane 40-8-10 is 0.01-1 μ m, and it is commercially available any hollow tubular fiber, is that 1～10mm, external diameter are the hollow tubular tunica fibrosa of 2～20mm for internal diameter for example.
In a preferred embodiment, the aperture of a plurality of U type hollow-fibre membrane 40-8-10 is 0.01-0.1 μ m, and it is that the internal diameter that is purchased is that 1mm, external diameter are the hollow tubular tunica fibrosa of 2mm.
In a preferred embodiment, the slit between each treating pond in each bio-reactor is that 200-300mm is wide.
In a preferred embodiment, wherein said ultrafiltration service pump 40-2 is a water transfer pump.
In another specific embodiment of the present utility model, a kind of lateral flow type sewage water treatment method also is provided, utilize above-mentioned lateral flow type membrane bioreactor device, described sewage water treatment method may further comprise the steps:
The raw waste water 10-4 that desire the is handled equalizing tank 10-2 that flows through regulates suitable pH value in described equalizing tank 10-2, have concurrently simultaneously under anaerobic to make mud carry out the effect of just sinking;
Make the first Aerobic Pond 20-2, the first anoxic pond 20-4, the first anaerobic pond 20-6 that flow at least the first bio-reactor 20-0 through the sewage of pH regulator in turn then, wherein at the backflow 20-14 that in the described first anoxic pond 20-4 flow process, forms the part water body by the described first Aerobic Pond 20-2;
The sewage of the first anaerobic pond 20-6 that makes the described at least the first bio-reactor 20-0 that flows through is pumped among the membrane ultrafiltration device 40-0 of ultrafiltration system 40-0 by ultrafiltration service pump 40-2 under certain pressure and carries out ultrafiltration, among the percolation water collecting bin 40-8-48 that is provided with below the film tube 40-8-64 that wherein treated sewage enters at described membrane ultrafiltration device 40-0-0, partly discharged behind the ultrafiltration of the flowing through recoil water pot 40-10, among a plurality of U type hollow-fibre membrane 40-8-10 U type tops that Open Side Down that active sludge is trapped within described membrane ultrafiltration device 40-0 and the dust storage cabin 40-8-40 of the formation of the space between the hollow membrane tube 40-8-64 or adhere to the tubular fibre film outer surface.
In a preferred embodiment, the lateral flow type sewage water treatment method further comprises:
Utilize the recoil mixed solution import 40-8-60 that below described film tube 40-8-64, is provided with to pump in the described membrane ultrafiltration device 40-0-0 the treated sewage 40-10-4 that is stranded in described ultrafiltration recoil water pot 40-10, described treated sewage 40-10-4 washes sedimentary active sludge and described a plurality of U type hollow-fibre membrane 40-8-10 outside surface adherent active sludge among the described dust storage cabin 40-8-40 as backwashing water, and forming spissated recoil mixed solution 40-8-90, described recoil mixed solution 40-8-90 effluent is fed back in the first Aerobic Pond 20-2 any treating pond interior or specified above-mentioned biochemical reactor according to need of the described the first bio-reactor 20-0 at least.
In another preferred embodiment, utilize the lateral flow type sewage water treatment method of lateral flow type membrane bioreactor device of the present utility model, further comprise:
When the treated sewage 40-10-4 that will be stranded in described ultrafiltration recoil water pot 40-10 utilizes the recoil mixed solution import 40-8-60 that is provided with below described film tube 40-8-64 to pump among the described membrane ultrafiltration device 40-0-0, blast air by the gas backwash pipe 40-8-84 that is provided with at described film tube 40-8-64 center, further remove sedimentary active sludge and described hollow-fibre membrane 40-8-10 outside surface adherent active sludge among the described dust storage cabin 40-8-40, wherein the described air that blasts by described gas backwash pipe 40-8-84 is only at the inwall by described film tube 40-8-64, the outer wall of a plurality of U type hollow-fibre membrane 40-8-10 and the inside that vibration between the opacity dividing plate of U type closure of openings in percolation water collecting bin 40-8-48 of described a plurality of U type hollow-fibre membrane 40-8-10 is not entered a plurality of U type hollow-fibre membrane 40-8-10.
In another preferred embodiment, utilize the lateral flow type sewage water treatment method of lateral flow type membrane bioreactor device of the present utility model, the air that wherein said gas backwash pipe 40-8-84 blasts is blasted by the gas blower 40-24 that is connected in described gas backwash pipe 40-8-84.
In a preferred embodiment, utilize the lateral flow type sewage water treatment method of lateral flow type membrane bioreactor device of the present utility model, wherein described raw waste water 10-4 is supplied with equalizing tank 10-2 and carry out pH regulator, making described raw waste water 10-4 carry out mud simultaneously in described equalizing tank 10-2 just sinks, and the reaction of generation release phosphorus, simultaneously the partial organic substances among the described raw waste water 10-4 is degraded;
To introduce among the first Aerobic Pond 20-2 of the described at least the first bio-reactor 20-0 through the sewage that described equalizing tank 10-2 handles, in the described first Aerobic Pond 20-2, make that remaining organism is continued by the microbial biochemical oxidation to descend in the sewage that described equalizing tank 10-2 handles, and phosphorus also descends with fast speeds along with the excess ingestion of polyP bacteria;
To introduce among the first anoxic pond 20-4 of the described at least the first bio-reactor 20-0 through the sewage that the described first Aerobic Pond 20-2 handles, in the described first anoxic pond 20-4, carry out denitrification denitrogenation, remove remaining most of organism in the sewage that described equalizing tank 10-2 handles simultaneously, wherein in the process of the first anoxic pond 20-4 of the described at least the first bio-reactor 20-0 of introducing, have partial reflux to go into the described first Aerobic Pond 20-2 through the sewage that the described first Aerobic Pond 20-2 handles;
To guide among the first anaerobic pond 20-6 of the described at least the first bio-reactor 20-0 through the sewage that the described first anoxic pond 20-4 handles, in the described first anaerobic pond 20-6, further carry out denitrification denitrogenation, remove remaining organism in the sewage that the described first anoxic pond 20-4 handles simultaneously;
The sewage that to handle through the first anaerobic pond 20-6 of the described at least the first bio-reactor 20-0 further flows among the second Aerobic Pond 30-2 of the described second bio-reactor 30-0, in the described second Aerobic Pond 30-2, make that remaining organism is continued by the microbial biochemical oxidation to descend in the sewage that the described first anoxic pond 20-4 or the first anaerobic pond 20-6 handle, and phosphorus also continues to descend fast with the excess ingestion of polyP bacteria;
To introduce among the second anoxic pond 30-4 or the second anaerobic pond 30-6 of the described second bio-reactor 30-0 through the sewage that the described second Aerobic Pond 30-2 handles, in the described second anoxic pond 30-4 or the second anaerobic pond 30-6, proceed denitrification denitrogenation to remove remaining most of organism in the decontaminated water, wherein in the sewage that the described second Aerobic Pond 30-2 handles is being introduced the process of the second anoxic pond 30-4 of the described second bio-reactor 30-0 or the second anaerobic pond 30-6, have partial reflux to go into the described second Aerobic Pond 30-2;
To guide among the second anaerobic pond 30-6 of the described second bio-reactor 30-0 through the sewage that the described second anoxic pond 30-4 handles, in the described second anaerobic pond 30-6, further carry out denitrification denitrogenation, remove remaining organism in the sewage that the described second anoxic pond 30-4 handles simultaneously;
Pumped into the sewage that the sewage that carries out ultrafiltration among the membrane ultrafiltration device 40-0-0 of described ultrafiltration system 40-0 comes free described first anaerobic pond 20-6 or the described second anaerobic pond 30-6 to discharge by described ultrafiltration service pump 40-2,
Sedimentary active sludge among mud among described first anaerobic pond 20-6 and the described second anaerobic pond 30-6 and the described dust storage cabin 40-8-40 and described a plurality of U type hollow-fibre membrane 40-8-10 outside surface adherent active sludge are passed back among the first Aerobic Pond 20-2 of the described first bio-reactor 20-0 by recoil or according to need in any treating pond of specified above-mentioned arbitrary biochemical reactor.
In a preferred embodiment, utilize the lateral flow type sewage water treatment method of lateral flow type membrane bioreactor device of the present utility model, wherein the described raw waste water 10-4 that supplies with described equalizing tank 10-2 is carried out pH regulator, pH is reached between 6.5～8.
In a preferred embodiment, utilize the lateral flow type sewage water treatment method of lateral flow type membrane bioreactor device of the present utility model, the treatment time of wherein said raw waste water 10-4 in the described at least the first bio-reactor 20-0 look raw water quality with treatment time in the membrane ultrafiltration device 40-0-0 of described ultrafiltration system 40-0 and handle after water quality requirement and different, follow gas backwash time of described film tube 40-8-64, the combined water and air backwash equal time of described then membrane ultrafiltration device 40-0-0, and the switching between above-mentioned each processing all is according to raw water quality and required the presetting of water quality requirement after handling.
One more in the preferred embodiment, utilize the lateral flow type sewage water treatment method of lateral flow type membrane bioreactor device of the present utility model, the treatment time of wherein said raw waste water 10-4 at least the first bio-reactor 20-0 set according to water quality requirement with the treatment time in the membrane ultrafiltration device 40-0-0 of described ultrafiltration system 40-0, for example the treatment time in the first Aerobic Pond 20-2 of the first bio-reactor 20-0 is more than 4 hours, treatment time in the first anaerobic pond 20-4 is more than 10 hours, treatment time in the first anoxic pond 20-4 is more than 4 hours, then the air that blasts by gas backwash pipe 40-8-84 is 0.5～2 minute to the gas backwash time of described film tube 40-8-64,30 seconds for example, utilize the recoil mixed solution import 40-8-60 that below film tube 40-8-64, is provided with treated sewage to be pumped into the liquid backwash time to described membrane ultrafiltration device 40-0-0 is 0.5～2 minute in the membrane ultrafiltration device 40-0-0 then, for example be 30 seconds, and the switching between above-mentioned each processing preset by Controlling System.
Owing to adopt lateral flow type membrane bioreactor device of the present utility model, when sewage enters in the film pipe from water inlet, major parts such as mud rest on dust storage cabin, and seldom a part of bottom that can enter into film and film centre and film pipe is only arranged, and this cleaning for film is highly profitable; Gas blower or air pump inject air by the gas backwash pipe in the film tube (air does not pass through the tubular fibre membranous wall, do not arrive the film inner chamber, and only flow between film tube inner chamber and film outer wall), the oscillating flow impact of air is loosened the mud of film surface adhesion, is come off, and that when helping back flushing mud is cleaned is more thorough.
The advantage of lateral flow type MBR of the present utility model:
By comparing with traditional activated sludge process and biomembrance process, lateral flow type MBR technology of the present utility model has following advantage:
As the characteristics of dead end membrane module (being the U type membrane fiber of hollow), its effluent quality standard height, stay in grade.The film surface apertures has only 1～0.1 micron, can carry out solid-liquid separation efficiently, and suspended substance and turbidity all approach zero, but direct reuse;
Operation control is more stable.The effect of efficiently damming of film makes active sludge and microorganism dam fully and feed back in reactor, has realized separating fully of the reactor waterpower residence time (HRT) and sludge age (SRT); Hydraulic detention time is short, and mud (organic macromolecule sizing material) residence time is long; Microorganism concn, biochemical efficiency increase substantially.
Variation adaptive faculty to water quality and quantity is strong, and anti impulsion load is strong.Solved the restriction of precipitation part that traditional activated sludge process causes, the microorganism concn height in the reactor to maximum biological concentration; Lateral flow type MBR can strengthen whole bioprocesses by synchronous nitration-denitrification simultaneously, do not pursue very high MLSS merely, this is because the active sludge in the lateral flow type membrane bioreactor device of the present utility model backflows in first Aerobic Pond of the first bio-reactor with formed concentrated recoil mixed solution at least, make to remain certain density active sludge in the Aerobic Pond, can also remove COD, BOD, ammonia nitrogen, phosphorus etc. effectively simultaneously.
Dephosphorization and denitrification effect is good.Help breeding damming, grow and breeding of nitrobacteria and other bacterium slowly, every indexs such as system's nitrification efficiency, COD clearance are improved, and the reaction times also shortens greatly; Big organism is trapped within the pond simultaneously, guarantees that it is continued degraded;
The organic removal rate height.Membrane sepn makes the macromole difficult degradation composition in the sewage that enough residence time be arranged in the bio-reactor of finite volume, help the cultivation of obligate bacterium, for example utilize the active sludge that is purchased in the sewage that needs are handled, to tame, thereby make the flora after the domestication be suitable for handling this sewage, improved the degradation efficiency of hardly degraded organic substance greatly, COD clearance height;
Modular design, adaptability is strong, be easy to dilatation or carry out the technology adjustment, can can adopt single bio-reactor according to the requirement of situation of coming water and externally discharged waste water, twin thing reactor, three biological reactors or four bio-reactors, be preferably twin thing reactor, Aerobic Pond in the wherein follow-up bio-reactor, whether anoxic pond and anaerobic pond exist and put in order is variable, requirement according to situation of coming water and externally discharged waste water decides, but should note, bio-reactor before entering ultrafiltration system is last arrange should be anaerobic pond, for no other reason than that sewage leaves standstill in the anaerobic pond, reduced the sludge quantity that filters in the sewage;
System adopts PLC control, can realize whole-course automation control, and operational management is convenient, comprises Controlling System in lateral flow type membrane bioreactor device of the present utility model, can control automatically the mud recoil;
The material of hollow membrane is a polyacrylonitrile, and the life-span is long, and resistance to crocking is strong, and easy cleaning is cheap, is suitable for sewage disposal.Stable chemical performance, oxidation-resistance is strong, and can adopt oxidisability medicament commonly used to clean when needed;
Realized the total reflux of mud in the lateral flow type membrane bioreactor device of the present utility model, made sludge age long, sludge quantity is few.Reactor moves under high volumetric loading, low sludge loading, long mud condition in age, and the excess sludge discharge amount is extremely low;
Adopt low press filtration, carry out to the timing cycle sequencing gas backwash and combined water and air backwash, wherein gas backwash and combined water and air backwash can carry out in proper order, can recoil 0.1～10 minute by advanced promoting the circulation of qi body, for example 0.3～3 minute, preferred 0.5～1 minute, make the mud of storage in the hopper dredger and loose attached to the mud on hollow-fibre membrane surface, carried out combined water and air backwash then 0.1～10 minute, for example 0.3～3 minute, preferred 0.5～1 minute, can also carry out sequencing according to the surface contamination situation of hollow-fibre membrane and strengthen back flushing (promptly increasing the intensity and the time of gas back-flushing and combined water and air backwash), strengthen chemical back flushing (in the recoil water pot, add common chemical reagent and carry out back flushing), reach minimum level to guarantee that film pollutes.Cut down the consumption of energy significantly simultaneously.
Lateral flow type membrane bioreactor device volumetric loading height of the present utility model takes up an area of few; Start soon, easy and simple to handle, not influenced by the mud expansible; Can save second pond, mud concentrates and sterilization pool.
The suitability of lateral flow type MBR of the present utility model
Efficient low pressure ultrafiltration operation reduces the film surface contamination.
Compact to design, volume is little, and flexibly, can design according to the practical situation of sewage and the requirement of the sewage after the processing, determines the quantity of needed bio-reactor.
Energy consumption low (compare significantly cut down the consumption of energy than the submerged membrane reactor), system compares with conventional process, can save 50% energy consumption.Feedwater water transfer pump of the present utility model is a force (forcing) pump, the energy consumption of force (forcing) pump is far below suction pump, and traditional submerged membrane reactor need use one group of suction pump usually, each suction pump only can be carried out the suction of several hollow-fibre membranes, the utility model is compared than traditional submerged membrane reactor and has been lowered energy consumption significantly, simultaneously, the utility model makes membrane pollution problem alleviate (pollution intensity that low pressure feed water absorbs water and causes to film far below high pressure or suction pump film formed pollution intensity) significantly again, and in the utility model, mud only exists in the storage hopper dredger that is made of the space between the inwall of the top of the U type hollow-fibre membrane that Open Side Down and plastic film tube and sticks on the outside surface of compact arranged U type hollow-fibre membrane.
Low cost and low operating cost clean simply, and working cost is low.Free from extraneous odour.The high loading processing power is strong.
Sludge discharge is very low, even does not almost have sludge discharge under certain conditions, has reduced the expense of handling.Remove suspended substance and bacterium fully.In a MBR, can remove suspended substance, bacterium and degraded COD, BOD, ammonia nitrogen, total nitrogen and total phosphorus simultaneously.No sludge bulking problem.Start-up system is fast.Can under conditions such as aerobic, anoxic, anaerobism, operate as requested.More convenient project reconstruction and Reconstruction design.Membrane ultrafiltration device in the ultrafiltration system (or membrane filtration system) can replace the secondary settling tank in the activated sludge process to remove suspended solids, organism, the preparation sterilized water.Can hold back nitrifier and larger molecular organics, prolong its residence time in reactor, can improve the clearance and the organic matter degradation of nitrogen.
Can long-time running under the condition of sequencing air, filtered water and chemical automatic backwash, membrane filtration water intaking form can adapt to as required from aerobic, anoxic, the water intaking of anaerobism any part.
Even various back flushinges were lost efficacy, also just fenestra diminishes.Can not cause the effluent characteristics problem.
Maintenance to film can not influence the outer biological respinse of membrane filtration system (or membrane ultrafiltration system), thereby can operate under hypoxia condition; The membrane ultrafiltration device is not only finished mud-water separation, and finishes the collection to mud.Thereby can realize the regulation and control rationally according to need that mud uses by the reasonable utilization of recoil mixed solution.
The demand that lateral flow type membrane bioreactor simultaneous adaptation of the present utility model is newly-built and transformation project develops.Adapt to water resources shortage and make the new requirement of society, and sewage drainage standard has been improved the reasonable utilization proposition of water.
Because lateral flow type MBR of the present utility model uses the film device of water delivery (pressurization) formula, reconstruction project does not need to build unnecessary facilities such as membrane filtration pond, does not need former facility to stop production yet.
All need the submerged membrane equipment erection staff of specialty to compare with reconstruction or newly-built each engineering, adopt lateral flow type membrane bioreactor device of the present utility model, Sewage Plant reconstruction contractor only need buy film device and possess simple equipment installable knowledge.Construction is simple, and the duration shortens, and is easy to safeguard.
Compare with the submerged membrane bio-reactor, the cost of lateral flow type membrane bioreactor device of the present utility model will hang down 20% to 30%, but equipment performance is better.
Because lateral flow type membrane bioreactor device of the present utility model can be worked under anaerobism, anoxic or aerobic condition, has given the bio-reactor planner bigger design space.
Gas backwash and carbonated drink associating recoil structure, make when sewage enters in the film tube from water-in, major parts such as mud rest on dust storage cabin, and seldom a part can enter in the middle of film and the film and the bottom of film tube, and film pollutes and the cleaning of film is highly profitable for reducing for this;
Gas blower or air pump inject air by the gas backwash pipe in the film tube (air does not pass through the tubular fibre membranous wall, do not arrive the film inner chamber, only flow between film tube inner chamber and film outer wall), the oscillating flow impact of air is loosened the mud of film surface adhesion, is come off, and that when helping back flushing mud is cleaned is more thorough.
Simultaneously, carry out gas backwash in the air admission film tube and also can play the effect that similar small bubbles are safeguarded the membrane fiber surface.
The effluent of membrane filtration system, not only can play the effect of mud-water separation, mud is thoroughly separated with hydraulic detention time age, uncorrelated mutually, that is to say, sludge age is to add new mud in slave unit driving or the operational process to begin to calculate, and hydraulic detention time is the temporal summation in each sewage disposal cycle then, makes sludge age much larger than hydraulic detention time.And, can also realize high density muddy water mixed solution feedback or unity feedback by the film back flushing, play regulating and controlling effect to active sludge and activated sludge biochemical reaction.
In the bio-reactor part, water body is according to the structure of bio-reactor, and the part water body feedback " circulation " that is formed in the flow process of oxygen-starved area by aerobic zone is an another lateral flow technology.It further makes the biochemical reaction time of water body reach controlled." controlled " of mud age and water body biochemical reaction time makes the controllable degree of MBR water technology reach a new level.Owing to the effect of hydromeehanics rule, fluidic changes also can bring some variations to biochemical reaction simultaneously.
Because the application of lateral flow technology makes the biochemical treatment process there is no need to reach higher biochemical effect to pursue higher MLSS.Therefore, unnecessary sludge discharge is very low, even almost can accomplish not have unnecessary sludge discharge under certain conditions.
Lateral flow type membrane bioreactor device of the present utility model has carried out gas back-flushing, combined water and air backwash and chemical back flushing, and the application that strengthens chemical backwashing technology, and it can be set among the normal working procedure of whole M BR as required, it can remain among the efficient operation operation of MBR so that film is in the high-throughput state for a long time; Make the film maintenance process become extremely simple simultaneously,, generally need not to stop work without any need for the personnel of complex apparatus and hi-tech level.
In the biochemical reactor,, effectively improve processing efficiency because the constructional feature (as the structure principle chart of Fig. 3) and the intermittent aeration The Application of Technology of lateral flow type membrane bioreactor device of the present utility model can be regulated aerobic, anaerobic reaction on the one hand according to need; Make aerobic zone and oxygen-starved area, anaerobic zone can have the drop of short period of time on the other hand, behind aeration, can produce a large amount of bubbles for the more abominable sewage of water quality and float on the surface, bubble can flow and be covered in each region surface, can suppress distributing of gas with foreign flavor to a certain extent, makes peculiar smell little.
Below in conjunction with embodiment, the utility model is further set forth, and can therefore not limit protection domain of the present utility model.
Embodiment
Embodiment of the present utility model is based on the various tests that pilot plant carries out, and as shown in Figure 3, it is installed in wastewater treatment plant.
Embodiment 1
In the present embodiment, lateral flow type membrane bioreactor device of the present utility model as shown in Figure 3, wherein membrane ultrafiltration (or filtration) device 40-0-0 is arranged to assembly as shown in Figure 4, a plurality of U type tubular fibre film closes that wherein Open Side Down are arranged and are encapsulated in the film tube.
As shown in Figure 3 and Figure 4, lateral flow type membrane bioreactor device of the present utility model, comprise successively: equalizing tank 10-2, at least one first bio-reactor 20-0, the second bio-reactor 30-0, the 40-0 of membrane ultrafiltration system, wherein, the 40-0 of membrane ultrafiltration system further comprises membrane ultrafiltration device 40-0-0, ultrafiltration recoil water pot 40-10-4, described membrane ultrafiltration device 40-0-0 has the film tube 40-8-64 of hollow, be provided with gas backwash pipe 40-8-30 at film tube 40-8-64 center, below film tube 40-8-64, be provided with percolation water collecting bin 40-8-48, has the opacity dividing plate between film tube 40-8-64 and the percolation water collecting bin 40-8-48, a plurality of U type hollow-fibre membrane 40-8-10 closely are arranged between the outer wall of the inwall of film tube 40-8-64 of hollow and gas backwash pipe 40-8-30 and Open Side Down is packaged among the film tube 40-8-64, the U type opening of a plurality of U type hollow-fibre membrane 40-8-10 is enclosed in the described percolation water collecting bin 40-8-48 by the opacity dividing plate, and the space between the film tube 40-8-64 of a plurality of U type hollow-fibre membrane 40-8-10 U type tops that Open Side Down and hollow forms dust storage cabin 40-8-40.
The first bio-reactor 20-0 comprises the first Aerobic Pond 20-2, the first anoxic pond 20-4, the first anaerobic pond 20-6, the second bio-reactor 30-0 comprises the second Aerobic Pond 30-2, the second anoxic pond 30-4, the second anaerobic pond 30-6, above film tube 40-8-64, be provided with water-in 40-8-80 and/or recoil mixture export 40-8-90, below film tube 40-8-64, be provided with water outlet 40-8-50 and/or recoil mixed solution import 40-8-60; The bottom of the opacity dividing plate between first Aerobic Pond 20-2 described in the first bio-reactor 20-0 and the described first anoxic pond 20-4 has a slit, the height of this slit is about 200-300mm, thereby forms part water body backflow 20-14 at the described first Aerobic Pond 20-2 in the flow process of the described first anoxic pond 20-4.Also has a slit at the second Aerobic Pond 30-2 of the second bio-reactor 30-0 and the bottom of the opacity dividing plate between the second anoxic pond 30-4 or the second anaerobic pond 30-6, the height of this slit is about 200-300mm, thereby in the flow process of the described second anoxic pond 30-4 or the second anaerobic pond 30-6, form part water body backflow 30-14 at the described second Aerobic Pond 30-2, at the first Aerobic Pond 20-2 and the first anoxic pond 20-4, and first dividing plate top between anoxic pond 20-4 and the first anaerobic pond 20-6 form overflow, at the second Aerobic Pond 30-2 and the second anoxic pond 30-4, and second dividing plate top between anoxic pond 30-4 and the second anaerobic pond 30-6 form overflow, and the recoil mixed solution import 40-8-60 of the membrane ultrafiltration device 40-0-0 in ultrafiltration system 40-0 links to each other with ultrafiltration recoil water pot 40-10, and wherein gas backwash pipe 40-8-30 is connected with gas blower 40-24.Flow into the membrane ultrafiltration device 40-0-0 of ultrafiltration system 40-0 through ultrafiltration service pump 40-2 by the effusive liquid of the first anaerobic pond 20-6, backflow through recoil mixture export 40-8-90 effusive recoil mixed solution and to get back to the first Aerobic Pond 20-2 of the first bio-reactor 20-0, the first Aerobic Pond 20-2 also comprises the first inlet pipe 20-8 that has the first gas distributor 20-20, the second Aerobic Pond 20-2 also comprises the second inlet pipe 30-8 that has the second gas distributor 30-20, the first gas distributor 20-20 and the second gas distributor 30-20 throw away in the exit of the first inlet pipe 20-8 and the second inlet pipe 30-8 pressurized air and enter first and second Aerobic Ponds and carry out aeration along the tangential direction of the first and second inlet pipe internal diameter each points, the sewage that flows into the membrane ultrafiltration device 40-0-0 of ultrafiltration system 40-0 through ultrafiltration service pump 40-2 comes the effusive liquid of the free second anaerobic pond 30-6, backflow through recoil mixture export 40-8-90 effusive recoil mixed solution and to get back to the first Aerobic Pond 20-2 or the second Aerobic Pond 30-2, the first gas distributor 20-20 away from the first anoxic pond 20-4 the second gas distributor 30-20 away from the second anoxic pond 30-4.
In lateral flow type membrane bioreactor device of the present utility model, also comprise accessories such as necessary under meter, necessary valve, backflow or transport pipe, water transfer pump, sludge circulation pump, more than all be well-known to those skilled in the art.
Embodiment 2
In the present embodiment, utilize lateral flow type membrane bioreactor device of the present utility model the lateral flow type sewage water treatment method as shown in Figure 3, wherein membrane ultrafiltration (or filtration) device 40-0-0 is arranged to the assembly as Fig. 4, a plurality of U type tubular fibre film closes that wherein Open Side Down are arranged and are encapsulated in the film tube.
As shown in Figure 3 and Figure 4, utilize the lateral flow type sewage water treatment method of lateral flow type membrane bioreactor device of the present utility model, comprise
Described raw waste water 10-4 is supplied with equalizing tank 10-2, make described raw waste water 10-4 regulate the pH value in described equalizing tank 10-2, make pH reach 6.5～8, the mud that carries out raw waste water simultaneously is just heavy, and the reaction of generation release phosphorus, simultaneously the partial organic substances among the described raw waste water 10-4 is degraded;
To introduce among the first Aerobic Pond 20-2 of the described at least the first bio-reactor 20-0 through the sewage that described equalizing tank 10-2 handles, in the described first Aerobic Pond 20-2, make that remaining organism is continued by the microbial biochemical oxidation to descend in the sewage that described equalizing tank 10-2 handles, and phosphorus also descends with fast speeds along with the excess ingestion of polyP bacteria;
To go among the first anoxic pond 20-4 of the described at least the first bio-reactor 20-0 through the sewage overflow that the described first Aerobic Pond 20-2 handles, tangential direction along the first inlet pipe internal diameter each point throws away in the exit of the first inlet pipe 20-8 with pressurized air by the first gas distributor 20-20, in the described first anoxic pond 20-4, carry out denitrification denitrogenation, remove remaining most of organism in the sewage that described equalizing tank 10-2 handles simultaneously, wherein introducing in the process of the first anoxic pond 20-4 of the described at least the first bio-reactor 20-0 through the sewage that the described first Aerobic Pond 20-2 handles, below the opacity dividing plate of the first Aerobic Pond 20-2 and the first anoxic pond 20-4, be provided with the slit of one 200～300mm, make the sewage backflow of the part first anoxic pond 20-4 go into the described first Aerobic Pond 20-2;
The sewage overflow that to handle through the described first anoxic pond 20-4 is in the first anaerobic pond 20-6 of the described at least the first bio-reactor 20-0, in the described first anaerobic pond 20-6, further carry out denitrification denitrogenation, remove remaining organism in the sewage that the described first anoxic pond 20-4 handles simultaneously;
The further overflow of sewage that to handle through the first anaerobic pond 20-6 of the described at least the first bio-reactor 20-0 is gone among the second Aerobic Pond 30-2 of (or pumping into) described second bio-reactor 30-0, tangential direction along the second inlet pipe internal diameter each point throws away in the exit of the second inlet pipe 30-8 with pressurized air by the second gas distributor 30-20 in the described second Aerobic Pond 30-2, make that remaining organism is continued by the microbial biochemical oxidation to descend in the sewage that the described first anoxic pond 20-4 or the first anaerobic pond 20-6 handle, and phosphorus also continues to descend fast with the excess ingestion of polyP bacteria;
To go among the second anoxic pond 30-4 of the described second bio-reactor 30-0 through the sewage overflow that the described second Aerobic Pond 30-2 handles, in the described second anoxic pond 30-4, proceed denitrification denitrogenation to remove remaining most of organism in the decontaminated water, wherein go in the process of the second anoxic pond 30-4 of the described second bio-reactor 320-0 in overflow through sewage that the described second Aerobic Pond 30-2 handles, below the opacity dividing plate of the second Aerobic Pond 30-2 and the second anoxic pond 30-4, be provided with the slit of a 200-300mm, make the sewage backflow of the part second anoxic pond 30-4 go into the described second Aerobic Pond 30-2;
The sewage overflow that to handle through the described second anoxic pond 30-4 is in the second anaerobic pond 30-6 of the described second bio-reactor 30-0, in the described second anaerobic pond 30-6, further carry out denitrification denitrogenation, remove remaining organism in the sewage that the described second anoxic pond 30-4 handles simultaneously;
Pump into the membrane ultrafiltration device 40-0-0 of described ultrafiltration system 40-0 through ultrafiltration service pump 40-2 by the effusive liquid of the second anaerobic pond 30-6, wherein mud is stored in by the space between the film tube 40-8-64 of a plurality of U type hollow-fibre membrane 40-8-10 U type tops that Open Side Down and hollow and forms dust storage cabin 40-8-40, effusive water purification flows into ultrafiltration recoil water pot 40-10-4 and is discharged, and above-mentioned each process is moved 10 minutes altogether.
Then, by Controlling System with pressurized air by recoil gas inlet 40-8-84 in gas backwash pipe 40-8-30 blasts space between the outer wall of the outer wall of the opacity dividing plate of inwall, sealing percolation water collecting bin 40-8-48 of the film tube 40-8-64 of hollow and a plurality of U type hollow-fibre membrane 40-8-10 and gas backwash pipe 40-8-30, make on the outer wall of sedimentary and a plurality of U type hollow-fibre membrane 40-8-10 among the dust storage cabin 40-8-40 sedimentary mud loose, move 1 minute altogether;
Then, recoil water purification among the water pot 40-10-4 of ultrafiltration is pumped into membrane ultrafiltration device 40-0-0 by ultrafiltration recoil pump 40-2 through recoil mixed solution import 40-8-60 and carries out back flushing, simultaneously pressurized air still blasts in the space between the outer wall of the outer wall of the opacity dividing plate of inwall, sealing percolation water collecting bin 40-8-48 of the film tube 40-8-64 of hollow and a plurality of U type hollow-fibre membrane 40-8-10 and gas backwash pipe 40-8-30 by gas backwash pipe 40-8-30, moves 1 minute altogether.
Then, will backflow through recoil mixture export 40-8-90 effusive recoil mixed solution and get back in the first Aerobic Pond 20-2 of the described first bio-reactor 20-0.
Begin above-mentioned operation cycle then again.
Can also be according to the sludge quantity (being limited not stop up slit between slit, the second Aerobic Pond 30-2 and the second anoxic pond 30-4 between the first anoxic pond 20-4 and the first anaerobic pond 20-6 and the slit between the second anoxic pond 30-4 and the second anaerobic pond 30-6) of accumulative total in the bioreactor, the activated sludge that utilizes sludge circulation pump 40-2 that the activated sludge that deposits among the mud among the first anaerobic pond 20-6 and described the second anaerobic pond 30-6 and the dust storage cabin 40-8-40 and hollow-fibre membrane 40-8-10 outer surface are sticked recoil among the first Aerobic Pond 20-2 that passes back into described the first bioreactor 20-0 or arbitrary treatment pond of above-mentioned arbitrary bioreactor in.
The above-mentioned operating time can coming the regimen condition and water purifying required change according to sewage.Can also carry out processing such as matting according to the pollution condition of hollow membrane, employed medicament and method are well known in the art, do not repeat them here.
Adopt lateral flow type membrane bioreactor device of the present utility model and utilize the advanced treatment method for sewage water of lateral flow type membrane bioreactor device of the present utility model, improve denitrogenation, dephosphorization effectively, removed the effect of insoluble organic, and omitted second pond.Thereby further embodied advance of the present utility model.
The above is a preferred embodiment of the present utility model only, is not limited to the utility model, and for a person skilled in the art, the utility model can have various changes and variation.All spirit of the present utility model and former within, any modification of being done, be equal to replacement, improvement etc., all should be included within the protection domain of the present utility model.
The primary clustering symbol description
10-2 regulating reservoir 10-4 raw sewage 20-0 first bioreactor
The 30-0 second bioreactor 20-2 first Aerobic Pond 20-4 first anoxic pond
The 20-6 first anaerobic pond 30-2 second Aerobic Pond 30-4 second anoxic pond
The 30-6 second anaerobic pond 40-0 ultrafiltration system 40-0-0 film ultrafiltration apparatus
40-10-4 ultrafiltration recoil water pot 40-8-44 dividing plate 40-8-48 filtered water collecting bin
40-8-64 film tube 40-8-10 hollow-fibre membrane 40-8-40 dust storage cabin
The import of 40-8-80 water-in 40-8-50 water outlet 40-8-60 recoil mixed solution
The 20-14 first Aerobic Pond part water body backflow 30-14 second Aerobic Pond part water body refluxes
40-10 ultrafiltration recoil water pot 40-8-30 gas backwash pipe 40-24 gas blower
40-6 under meter 40-4 variable valve 20-8 first inlet pipe
20-20 first gas distributor 10-6 water inlet 20-10 gas bubbling
The 30-8 second inlet pipe 30-20 second gas distributor 20-14 first refluxes
50-10 mud discharge line 30-14 second refluxes
40-2 pump (as ultrafiltration service pump, ultrafiltration recoil pump or sludge circulation pump)
40-8-84 recoil gas inlet 40-50 first sewage backflow
The 40-60 second sewage backflow 40-90 the 3rd sewage backflow.
Claims (13)
1. lateral flow type membrane bioreactor device, comprise successively: equalizing tank (10-2), at least one first bio-reactor (20-0), ultrafiltration system (40-0), wherein, described first bio-reactor (20-0) comprises first Aerobic Pond (20-2), first anoxic pond (20-4), first anaerobic pond (20-6), it is characterized in that: described ultrafiltration system (40-0) further comprises membrane ultrafiltration device (40-0-0), ultrafiltration recoil water pot (40-10-4), described membrane ultrafiltration device (40-0-0) has the film tube (40-8-64) of hollow, be provided with gas backwash pipe (40-8-30) at described film tube (40-8-64) center, be provided with percolation water collecting bin (40-8-48) in the below of described film tube (40-8-64), has the opacity dividing plate between described film tube (40-8-64) and the described percolation water collecting bin (40-8-48), a plurality of U type hollow-fibre membranes (40-8-10) closely are arranged between the outer wall of the inwall of film tube (40-8-64) of described hollow and described gas backwash pipe (40-8-30) and Open Side Down is packaged in the described film tube (40-8-64), the U type opening of described a plurality of U type hollow-fibre membranes (40-8-10) is enclosed in the described percolation water collecting bin (40-8-48) by the opacity dividing plate, space between the film tube (40-8-64) of described a plurality of U type hollow-fibre membranes (40-8-10) U type upper end that Open Side Down and described hollow forms dust storage cabin (40-8-40), be provided with water-in (40-8-80) and/or recoil mixture export (40-8-90) in the top of described film tube (40-8-64), be provided with water outlet (40-8-50) and/or recoil mixed solution import (40-8-60) in the below of described film tube (40-8-64); Also has the device that in described first anoxic pond (20-4) flow process, forms part water body backflow (20-14) by described first Aerobic Pond (20-2) in described first bio-reactor (20-0), in described first Aerobic Pond (20-2) and described first anoxic pond (20-4), and the top of the dividing plate between described first anoxic pond (20-4) and described first anaerobic pond (20-6) forms overflow, flow into the membrane ultrafiltration device (40-0-0) of described ultrafiltration system (40-0) through ultrafiltration service pump (40-2) by the effusive liquid of described first anaerobic pond (20-6), backflow through the effusive recoil mixed solution of described recoil mixture export (40-8-90) and to get back to described first Aerobic Pond (20-2) of described first bio-reactor (20-0), described first Aerobic Pond (20-2) further comprises first inlet pipe (20-8) that has first gas distributor (20-20).
2. lateral flow type membrane bioreactor device according to claim 1, it is characterized in that, described device further comprises second bio-reactor (30-0), optional second Aerobic Pond (30-2) that comprises of described second bio-reactor (30-0), second anoxic pond (30-4), second anaerobic pond (30-6), also has the device that in described second anoxic pond (30-4) or described second anaerobic pond (30-6) flow process, forms part water body backflow (30-14) by described second Aerobic Pond (30-2) in wherein said second bio-reactor (30-0), the described recoil mixed solution import (40-8-60) of described membrane ultrafiltration device (40-0) links to each other with ultrafiltration recoil water pot (40-10), wherein said gas backwash pipe (40-8-30) is connected with gas blower (40-24), described equalizing tank (10-2) is with the function of anaerobic pond, described second Aerobic Pond (20-2) further comprises second inlet pipe (30-8) that has second gas distributor (30-20), described first gas distributor (20-20) and second gas distributor (30-20) enter described first and second Aerobic Ponds with pressurized air in the exit of described first inlet pipe (20-8) and optional described second inlet pipe (30-8) and carry out aeration, the sewage that flows into the described membrane ultrafiltration device (40-0-0) of described ultrafiltration system (40-0) through ultrafiltration service pump (40-2) comes the effusive liquid of free described second anaerobic pond (30-6), backflow through the effusive recoil mixed solution of described recoil mixture export (40-8-90) and to get back to described first Aerobic Pond (20-2) or optional described second Aerobic Pond (30-2), described first gas distributor (20-20) away from described first anoxic pond (20-4) optional second gas distributor (30-20) away from optional described second anoxic pond (30-4).
3. lateral flow type membrane bioreactor device according to claim 2, it is characterized in that, described device further comprises the 3rd biological reactor, optional the 3rd Aerobic Pond, the 3rd anoxic pond, the 3rd anaerobic pond of comprising of the described the 3rd biological reactor also has the device that is formed the backflow of part water body by described the 3rd Aerobic Pond in described the 3rd anoxic pond or the 3rd anaerobic pond flow process in the wherein said the 3rd biological reactor; And optional the 4th bio-reactor that comprises, optional the 4th Aerobic Pond, the 4th anoxic pond, the 4th anaerobic pond of comprising of described the 4th bio-reactor, also have the device that is formed the backflow of part water body by described the 4th Aerobic Pond in described the 4th anoxic pond or the 4th anaerobic pond flow process in wherein said the 4th bio-reactor, the sewage that flows into the described membrane ultrafiltration device (40-0-0) of described ultrafiltration system (40-0) through described ultrafiltration service pump (40-2) comes free described the 3rd anaerobic pond or the effusive liquid of the 4th anaerobic pond.
4. lateral flow type membrane bioreactor device according to claim 2, it is characterized in that, the device that is formed part water body backflow (20-14) by described first Aerobic Pond (20-2) in described first anoxic pond (20-4) flow process is the slit that the dividing plate below between described first Aerobic Pond (20-2) and described first anoxic pond (20-4) has, be used between described first Aerobic Pond (20-2) and described first anoxic pond (20-4), forming part water body backflow (20-14), the device that is formed part water body backflow (30-14) by described second Aerobic Pond (30-2) in described second anoxic pond (30-4) or described second anaerobic pond (30-6) flow process is the slit that the dividing plate below between optional described second Aerobic Pond (30-2) that comprises of described second bio-reactor (30-0) and described second anoxic pond (30-4) or described second anaerobic pond (30-6) has, be used for forming the part water body at flow process and reflux (30-14), the tangential direction along the described first and second inlet pipe internal diameter each points throws away in the exit of described first inlet pipe (20-8) and optional described second inlet pipe (30-8) with pressurized air for wherein said first gas distributor (20-20) and second gas distributor (30-20).
5. lateral flow type membrane bioreactor device according to claim 3, it is characterized in that, described first bio-reactor (20-0), described second bio-reactor (30-0), the described the 3rd biological reactor, the reaction conditions of each Aerobic Pond in described the 4th bio-reactor, each anoxic pond, each anaerobic pond can be identical, also can be different, and the sewage situation that described reaction conditions is handled according to desire is decided.
6. according to each described lateral flow type membrane bioreactor device of claim 1～5, it is characterized in that, further comprise the device that makes mixed-liquor return that the described membrane ultrafiltration device of recoil (40-0-0) back produces described first Aerobic Pond (20-2) to described first bio-reactor (20-0).
7. according to each described lateral flow type membrane bioreactor device of claim 3～5, it is characterized in that described first bio-reactor (20-0), described second bio-reactor (30-0), optionally the described the 3rd biological reactor, optional described the 4th bio-reactor bio-reactor assembly that is an integral body or independent component string is connected together.
8. according to each described lateral flow type membrane bioreactor device of claim 1～5, it is characterized in that the water displacement after treatment that the described water outlet (40-8-50) that the below by described film tube (40-8-64) is provided with is discharged equates with the water yield of the sewage (10-6) that enters described the first bio-reactor (20-0) at least.
9. according to each described lateral flow type membrane bioreactor device of claim 1～5, further comprise Controlling System, be used to control described first Aerobic Pond (20-2) of raw waste water (10-4) at described at least the first bio-reactor (20-0), first anoxic pond (20-4), treatment time in first anaerobic pond (20-6), treatment time in the membrane ultrafiltration device (40-0-0) of described ultrafiltration system (40-0), the gas backwash time of the liquid backwash time of described membrane ultrafiltration device (40-0-0) and described film tube (40-8-64), and the switching between above-mentioned each processing.
10. lateral flow type membrane bioreactor device according to claim 9, the switching between wherein said each treatment time and each are handled or according to raw water quality with to handling the back requirements in water quality presets, perhaps manually control according to actual needs.
11., it is characterized in that the aperture of described a plurality of U type hollow-fibre membranes (40-8-10) is 0.01-1 μ m according to each described lateral flow type membrane bioreactor device of claim 1～5.
12., it is characterized in that described slit is that 200～300mm is wide according to each described lateral flow type membrane bioreactor device of claim 4～5.
13. according to each described lateral flow type membrane bioreactor device of claim 1～5, wherein said ultrafiltration service pump (40-2) is a water transfer pump.
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| Application Number | Priority Date | Filing Date | Title |
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| CNU2008201237584U CN201305510Y (en) | 2008-11-19 | 2008-11-19 | Lateral flow type membrane bioreactor device |
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| Application Number | Priority Date | Filing Date | Title |
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| CNU2008201237584U CN201305510Y (en) | 2008-11-19 | 2008-11-19 | Lateral flow type membrane bioreactor device |
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| CN201305510Y true CN201305510Y (en) | 2009-09-09 |
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| CNU2008201237584U Expired - Fee Related CN201305510Y (en) | 2008-11-19 | 2008-11-19 | Lateral flow type membrane bioreactor device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102351382A (en) * | 2011-09-06 | 2012-02-15 | 北京昊业怡生科技有限公司 | Combined treatment method of leachate and excrement wastewater |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102351382A (en) * | 2011-09-06 | 2012-02-15 | 北京昊业怡生科技有限公司 | Combined treatment method of leachate and excrement wastewater |
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Granted publication date: 20090909 Termination date: 20121119 |