CN103570129B - A kind of circulation flow ring-shaped membrane bioreactor effluent treatment process - Google Patents
A kind of circulation flow ring-shaped membrane bioreactor effluent treatment process Download PDFInfo
- Publication number
- CN103570129B CN103570129B CN201310531125.2A CN201310531125A CN103570129B CN 103570129 B CN103570129 B CN 103570129B CN 201310531125 A CN201310531125 A CN 201310531125A CN 103570129 B CN103570129 B CN 103570129B
- Authority
- CN
- China
- Prior art keywords
- oxygen
- aerobic zone
- zone
- starved area
- circulation flow
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Abstract
The present invention relates to a kind of circulation flow ring-shaped membrane bioreactor effluent treatment process, carry out sewage disposal by circulation flow ring-shaped membrane bioreactor, described circulation flow ring-shaped membrane bioreactor comprise set up successively anaerobic zone, oxygen-starved area, aerobic zone and the membrane biological reaction district that is arranged in aerobic zone; Sewage successively through described anaerobic zone, oxygen-starved area, aerobic zone and membrane biological reaction district carrying out process, and make to maintain higher sludge concentration in whole reactor by the backflow of membrane biological reaction district to aerobic zone, aerobic zone to oxygen-starved area and oxygen-starved area to anaerobic zone; Utilize described circulation flow ring-shaped membrane bioreactor effluent treatment process by the optimum combination of reactor, greatly improve the flexible adaptability to changes of system, significantly reduce construction investment, energy efficient simultaneously.
Description
Technical field
The present invention relates to a kind of circulation flow ring-shaped membrane bioreactor effluent treatment process, belong to organic sewage processing technology field.
Background technology
In Continuous Flow denitrification dephosphorization technique, current membrane bioreactor (MBR, biological respinse is referred to combine with membrane sepn, be that separating medium substitutes conventional articulated gravity precipitation solid-liquid separation acquisition water outlet with film, and the sewage water treatment method of reaction process and raising reaction efficiency can be changed) because its flow process is simple and direct, processing efficiency is high, occupation of land is saved, effluent quality is superior and have vast potential for future development.
By technique pattern, MBR technique can be divided into submerged membrane biological treatment system (Immersed membrane biologicaltreatment system, be called for short S-MBR) and external membrane biological treatment system (Side stream membrane biologicaltreatment system is called for short R-MBR).S-MBR refers to that membrane module is immersed in biological reaction tank, and pollutent carries out biochemical reaction at biological reaction tank, utilizes film to carry out equipment or the system of solid-liquid separation, and negative pressure can be adopted to produce water, and hydrostaticpressure also can be utilized from miscarrying water.R-MBR refer to membrane module and biological reaction tank arranged apart, active sludge intermixture in biological reaction tank pumps into equipment or the system that film group device carries out solid-liquid separation, produce water discharge or advanced treatment, concentrated mud mixture is back to circulation concentration basin or biological reaction tank, forms circulation.Limitting by operational conditions, from safety performance angularly, R-MBR is the main way of current application.
S-MBR replaces traditional biological treatment technology end second pond with membrane module, high reactivity sludge concentration is kept in bio-reactor, improve biological treatment organic loading, thus reduce sewage treatment facility floor space, and by keeping low sludge loading to reduce surplus sludge volume.The active sludge in the membrane separation plant entrapping tank be immersed in aerobe pond and larger molecular organics can be utilized.In membrane bioreactor system, active sludge (MLSS) concentration can be promoted to 8000 ~ 10,000mg/L, even higher; Sludge age (SRT) can extend to more than 30 days.
But in actual application, MBR energy consumption is higher, for the sewage disposal of Typical Towns, even more traditional A/O technique is high more than 1 times, defines huge obstacle thus for promoting the use of of this technology.
Summary of the invention
The object of the invention is to the shortcoming overcoming prior art, provide a kind of circulation flow ring-shaped membrane bioreactor effluent treatment process, this technique has the sewage disposal feature of high-efficiency low energy consumption.
The present invention is achieved by the following technical solutions:
A kind of circulation flow ring-shaped membrane bioreactor effluent treatment process, for carrying out sewage disposal by circulation flow ring-shaped membrane bioreactor (CCFP-MBR), described circulation flow ring-shaped membrane bioreactor comprise set up successively anaerobic zone, oxygen-starved area, aerobic zone and the membrane biological reaction district that is arranged in aerobic zone; Described sewage treatment process comprises the following steps:
(A) first sewage enter the anaerobic zone of circulation flow ring-shaped membrane bioreactor, mixes with the phegma from oxygen-starved area, and in anaerobic zone, polyP bacteria releases phosphorus under anaerobic environment, and part itrogenous organic substance is carried out ammonification;
(B) then enter oxygen-starved area, mix with the phegma from aerobic zone, carry out denitrification process and carry out denitrogenation in oxygen-starved area, partial organic substances is degraded removal under the effect of denitrifying bacteria;
(C) then enter aerobic zone, carry out the absorption of the nitrated and phosphorus of organic further degraded and ammonia;
(D) then enter membrane biological reaction district and carry out solid-liquid separation, purify waste water and to be discharged by pump, concentrated sludge part is circulated to aerobic zone, and along with the reflux cycle of the mixed solution of aerobic zone to oxygen-starved area and oxygen-starved area to anaerobic zone is to whole reaction zone, maintain sludge concentration higher in reactor, outside excess sludge, drain into sludge thickener.
Preferably, described anaerobic zone comprises anaerobic zone A and anaerobic zone B; First sewage enter anaerobic zone A, the descending flowing of stirring pushing effect of the push flowing diving mixer arranged in the A of anaerobic zone, then enter in the B of anaerobic zone, the up flowing of stirring pushing effect of the push flowing diving mixer arranged in the B of anaerobic zone, then a part is circulated in the A of anaerobic zone, and a part enters oxygen-starved area.
Preferably, described oxygen-starved area comprises oxygen-starved area A and oxygen-starved area B; First sewage from anaerobic zone enter in the A of oxygen-starved area, the descending flowing of stirring pushing effect of the push flowing diving mixer arranged in the A of oxygen-starved area, then enter in the B of oxygen-starved area, the up flowing of stirring pushing effect of the push flowing diving mixer arranged in the B of oxygen-starved area, then a part is circulated in the A of oxygen-starved area, and a part enters aerobic zone.
Preferably, described aerobic zone comprises aerobic zone A and aerobic zone B; Described membrane biological reaction district is positioned at aerobic zone B; First sewage from oxygen-starved area enter aerobic zone A, right lateral flowing under the stirring pushing effect of the push flowing diving mixer arranged in the A of aerobic zone, then aerobic zone B is entered, after mixing from the partial concentration mud in membrane biological reaction district, left lateral flowing under the stirring pushing effect of the push flowing diving mixer arranged in the B of aerobic zone, then a part is circulated in the A of aerobic zone, a part is circulated in the A of aerobic zone by the recycle ratio adjustable checkgate arranged between aerobic zone A and aerobic zone B, and residue enters membrane biological reaction district and carries out solid-liquid separation.
Preferably, sewage in described aerobic zone B enters membrane biological reaction district by the film district water distribution weir gate of side, membrane biological reaction district and carries out solid-liquid separation, local high microorganism concentration range is formed in membrane biological reaction district, purifying waste water of being separated is expelled to outside battery limit (BL) by pump, be separated the thickened sludge part formed and be expelled to aerobic zone B by the film district effluent weir gate being positioned at membrane biological reaction district opposite side, residue thickened sludge is expelled to sludge thickener by mud overboard pump.
Preferably, described membrane biological reaction district is arranged in parallel multiple separate membrane biological reaction subregion; Each membrane biological reaction is distinguished in district and is provided with film district water distribution weir gate and film district effluent weir gate; Be convenient to replace cleaning and be unlikely to be stopped work in whole membrane biological reaction district.
Preferably, the air lift unit I of the mixed solution of oxygen-starved area A by arranged transversely is back in the A of anaerobic zone in the mode of air-lift unit.
Preferably, the air lift unit II of the mixed solution of aerobic zone B by arranged transversely is back in the A of oxygen-starved area in the mode of air-lift unit.
Preferably, the reflux ratio of described oxygen-starved area A mixed solution is 50%-200%; The reflux ratio of the mixed solution of described aerobic zone B is 100%-400%.
Preferably, when designing sludge concentration and being lower, in described aerobic zone, arrange sludge condensation district, thickened sludge, after described sludge condensation district makes preliminary sedimentation, is directly back to anaerobic zone by aerobic zone mixed solution; Construction can be separated in aerobic zone by described sludge condensation district.Design sludge concentration mainly refers to microorganism concn i.e. MLSS value, if MLSS value is lower, then processing power is more weak, and the object of sludge reflux is about to the sludge reflux after concentrating to anaerobic zone, makes the sludge concentration that whole reactor remains higher.
Preferably, described aerobic zone is provided with blast aerator; Described blast aerator comprises the micro-pore aeration system be located in aerobic zone and the gas blower be located at outside aerobic zone.
Preferably, in described oxygen-starved area, be provided with micro-pore aeration system, make described oxygen-starved area leave the air consumption of 15-20% by described micro-pore aeration system; Realize synchronous nitration and denitrification process simultaneously; Extend anoxic section simultaneously, shorten aerobic section, can be effectively energy-conservation.
Preferably, by described push flowing diving mixer, the mean velocity in section of described circulation flow ring-shaped membrane bioreactor internal recycle current for 0.3-0.5m/s, is being controlled as 0.1-0.15m/s under having aeration condition without controlling under aeration condition.Described mean velocity in section realizes by the watt level configuring stirrer; Although section width is inconsistent, as long as just can realize the comparatively ideal cross-sectional flow in this region at the stirrer that this regional choice is suitable.
Preferably, in described anaerobic zone, hydraulic detention time is 1-2 hour.
Preferably, the denitrification load values scope of described oxygen-starved area is 0.03 ~ 0.06kgNO
3 --N/kgMLSSd(20 DEG C).
Preferably, the general value of the sludge loading of described aerobic zone is 0.1 ~ 0.2kgBOD
5/ (kgMLSSd).
Preferably, the energy density of described anaerobic zone is 4 ~ 5W/m
3; The energy density of oxygen-starved area is 1 ~ 2W/m
3; The energy density of aerobic zone is 0.5 ~ 1.5W/m
3.
Preferably, the sludge concentration of described anaerobic zone is 1500-3000mg/L, and the sludge concentration of described oxygen-starved area is 3000-6000mg/L, and the sludge concentration of described aerobic zone is 6000-12000mg/L.
Technique effect of the present invention and advantage are:
1.CCFP-MBR has abandoned the single current pattern of general membrane bioreactor, adopts polytype combination of reactors, facilitates operational management, optimize reaction technology.
2., in operation scheme, adopt the fluidised form of cycling stream, have the ability of the anti-shock loading of complete and the better treatment effect of plug-flow reactor concurrently, both can process city domestic sewage, the composite waste containing part trade effluent can be processed again;
3. use for reference about the near influence principle about shock resistance in the characteristics of motion theory of Solution of Flow in Curved Channel and hydromechanics in river dynamics, the velocity flow profile of ring-type circulatory pool type rationally, not easily produces deposition phenomenon, head loss is less;
4. the current in each section all present fairly obvious limit wall turbulent diffusion phenomenon and secondary flow phenomenon, on mix and blend the impact that rises very positive;
5. current effect of mass transmitting is strengthened, short stream can be eliminated, backflow and dead band possibility occurrence low, reduce current dead angle, the allocation of space of uniform stirring power, the mixed effect of realizing ideal;
6. operation scheme is more flexible, comprise expand mixed-liquor return mode can the aspect such as choice;
7. eliminate into water, the distribution system entering mud and reflux line, the pipeline simplifying reactive system distributes;
8. utilize cycling stream waterpower form, instead of the vast scale sludge reflux in general MBR technique, more effectively recycled film district dissolved oxygen, energy conservation and consumption reduction effects is obvious simultaneously;
9. utilize lower impellent, for the biofloculation in reactor provides favourable condition, energy efficient simultaneously;
10. various hybrid mode is combined, improve the suitability of system process different quality;
11. adopt micro-pore aeration equipment, and power consumption is far below oxidation ditch process; In conjunction with plug-flow, thoroughly solve the contradiction between oxygenation and stirring.
Accompanying drawing explanation
A kind of circulation flow ring-shaped membrane bioreactor plan structure schematic diagram of Fig. 1
Reference numeral:
1, anaerobic zone; 1a, anaerobic zone A; 1b, anaerobic zone B;
2, oxygen-starved area; 2a, oxygen-starved area A; 2b, oxygen-starved area B;
3, aerobic zone; 3a, aerobic zone A; 3b, aerobic zone B;
4, membrane biological reaction district; 5, the first training wall; 6, the first partition wall; 7, the second training wall; 8, the second partition wall; 9, the 3rd training wall; 10, the 3rd partition wall; 11, film district water distribution weir gate; 12, film district effluent weir gate; 13, canal for water distribution; 14, water outlet channel; 15, push flowing diving mixer; 16, the 3rd water hole; 17, the 4th water hole; 18, the first water hole; 19, the 5th water hole; 20, the 6th water hole; 21, the second water hole; 22, the 7th water hole; 23, recycle ratio adjustable checkgate; 24, air lift unit II; 25, air lift unit I, the 26, the 8th water hole.
Embodiment
Below by way of specific specific examples, technical scheme of the present invention is described.Should be understood that these embodiments are only not used in for illustration of the present invention to limit the scope of the invention.And except as otherwise noted, the change of relativeness or adjustment, when changing technology contents without essence, when being also considered as the enforceable category of the present invention.
A kind of circulation flow ring-shaped membrane bioreactor (CCFP-MBR), as shown in Figure 1, comprise set up successively anaerobic zone 1, oxygen-starved area 2, aerobic zone 3 and the membrane biological reaction district 4 that is arranged in aerobic zone 3; Be provided with the first longitudinal partition wall 6 between described anaerobic zone 1 and oxygen-starved area 2, one end of described first partition wall 6 is provided with the first water hole 18; Be provided with the second longitudinal partition wall 8 between described oxygen-starved area 2 and aerobic zone 3, one end of described second partition wall 8 is provided with the second water hole 21;
Described anaerobic zone 1 is provided with the first longitudinal training wall 5, by described first training wall 5, anaerobic zone 1 is divided into the anaerobic zone A1a in left side and the anaerobic zone B1b on right side; One end of described first training wall 5 arranges the 3rd water hole 16, and the other end arranges the 4th water hole 17;
Be provided with the second longitudinal training wall 7 in described oxygen-starved area 2, by described second training wall 7, oxygen-starved area 2 be divided into the oxygen-starved area A2a in left side and the oxygen-starved area B2b on right side; One end of described second training wall 7 arranges the 5th water hole 19, and the other end arranges the 6th water hole 20;
Described aerobic zone 3 is provided with the 3rd horizontal training wall 9, by described 3rd training wall 9, aerobic zone 3 is divided into the aerobic zone A3a of upside and the aerobic zone B3b of downside;
One end near described second partition wall 8 on described 3rd training wall 9 is provided with recycle ratio adjustable checkgate 23, and the other end arranges the 7th water hole 22;
Described membrane biological reaction district 4 is positioned at described aerobic zone B3b;
Described membrane biological reaction district 4 is set to rectangle, and side is connected with longitudinal exterior wall of described aerobic zone B3b, and other three side is adjacent and parallel with the horizontal exterior wall of described 3rd training wall 9, second partition wall 8 and described aerobic zone B3b respectively;
Also be provided with the 3rd horizontal partition wall 10 between described membrane biological reaction district 4 and described 3rd training wall 9, the one end near described 7th water hole 22 on described 3rd partition wall 10 is provided with the 8th water hole 26;
Described membrane biological reaction district 4 is provided with film district water distribution weir gate 11 near the side of the horizontal exterior wall of described aerobic zone B3b, and described membrane biological reaction district 4 is provided with film district effluent weir gate 12 near the side of described 3rd partition wall 10;
Gap between described membrane biological reaction district 4 Shang Mo district water distribution weir gate 11 side and the horizontal exterior wall of described aerobic zone B3b forms canal for water distribution 13, and the gap between the side at effluent weir gate 12 place, Shang Mo district of described membrane biological reaction district 4 and described 3rd partition wall 10 forms water outlet channel 14;
Push flowing diving mixer 15 is equipped with in described anaerobic zone A1a, anaerobic zone B1b, oxygen-starved area A2a, oxygen-starved area B2b, aerobic zone A3a and aerobic zone B3b;
The air lift unit I 25 laterally placed is provided with between described anaerobic zone 1 and oxygen-starved area 2; The fluid inlet of described air lift unit I 25 is positioned at oxygen-starved area A2a, and the liquid outlet of described air lift unit I 25 is positioned at anaerobic zone A1a;
Be provided with the air lift unit II 24 laterally placed between described oxygen-starved area 2 and aerobic zone 3, the fluid inlet of described air lift unit II 24 is positioned at aerobic zone B3b, and the liquid outlet of described air lift unit II 24 is positioned at oxygen-starved area A2a;
The longitudinal parallel connection in described membrane biological reaction district 4 is provided with multiple separate membrane biological reaction subregion; Each membrane biological reaction subregion is provided with film district water distribution weir gate 11 near the side of the horizontal exterior wall of described aerobic zone B3b, and each membrane biological reaction subregion is provided with film district effluent weir gate 12 near the side of described 3rd partition wall 10;
Described aerobic zone 3 is provided with blast aerator; Described blast aerator comprises the micro-pore aeration system be located in aerobic zone 3 and the gas blower be located at outside aerobic zone 3;
Micro-pore aeration system is provided with in described oxygen-starved area 2; Described oxygen-starved area is made to leave the air consumption of 15-20% by described micro-pore aeration system; Realize synchronous nitration and denitrification process simultaneously; Extend anoxic section simultaneously, shorten aerobic section, can be effectively energy-conservation.
As one preferred embodiment, when designing sludge concentration and being lower, be provided with sludge condensation district in described aerobic zone 3, establish sludge refluxing apparatus in described sludge condensation district, the mud discharging mouth of described sludge refluxing apparatus is positioned at described anaerobic zone 1; Thickened sludge, after described sludge condensation district makes preliminary sedimentation, is directly back to anaerobic zone 1 by aerobic zone 3 mixed solution; Construction can be separated in aerobic zone 3 by described sludge condensation district.
Utilize the CCFP-MBR shown in Fig. 1 to carry out a technique for sewage disposal, comprise the following steps:
(1) first sewage enter anaerobic zone A1a, mix with the phegma from oxygen-starved area A2a, by the stirring pushing effect of push flowing diving mixer 15 arranged in the A1a of anaerobic zone, along the descending flowing of described first training wall 5, anaerobic zone B1b is entered afterwards by described 3rd water hole 16, by the stirring pushing effect of push flowing diving mixer 15 arranged in the B1b of anaerobic zone, along the up flowing of described first training wall 5; In the B1b of anaerobic zone, a sewage part is circulated in the A1a of anaerobic zone by described 4th water hole 17, and a part enters oxygen-starved area 2 by described first water hole 18;
(2) first the sewage from anaerobic zone B1b enter oxygen-starved area A2a, mix with the phegma from aerobic zone B3b, by the stirring pushing effect of push flowing diving mixer 15 arranged in the A2a of oxygen-starved area, along the descending flowing of described second training wall 7, oxygen-starved area B2b is entered afterwards by described 5th water hole 19, by the stirring pushing effect of push flowing diving mixer 15 arranged in the B2b of oxygen-starved area, along the up flowing of described second training wall 7; In the B2b of oxygen-starved area, a sewage part is circulated in the A2a of oxygen-starved area by described 6th water hole 20, and a part enters aerobic zone 3 by described second water hole 21;
(3) first the sewage from oxygen-starved area B2b enter aerobic zone A3a, by the stirring pushing effect of push flowing diving mixer 15 arranged in the A3a of aerobic zone, along described 3rd training wall 9 right lateral flowing, aerobic zone B3b is entered afterwards by described 7th water hole 22, after mixing with the partial concentration mud from membrane biological reaction district 4, by the stirring pushing effect of push flowing diving mixer 15 arranged in the B3b of aerobic zone, along described 3rd training wall 9 left lateral flowing, then a part is circulated in the A3a of aerobic zone through described recycle ratio adjustable checkgate 23, a part is along the descending flowing of described second partition wall 8, then along described canal for water distribution 13 right lateral flowing, entered in membrane biological reaction district 4 by described film district water distribution weir gate 11 in flow process and carry out solid-liquid separation, form local high microorganism concentration range, purifying waste water of being separated is expelled to outside battery limit (BL) by pump, be separated the thickened sludge part formed flow along described water outlet channel 14 right lateral after the discharge of film district effluent weir gate 12 and be expelled to aerobic zone B3b from described 8th water hole 26, flow along described 3rd training wall 9 left lateral after mixing with next aforementioned sewage in the A3a of aerobic zone, residue thickened sludge is expelled to sludge thickener by mud overboard pump.
Embodiment 1
Adopt the circulation flow ring-shaped membrane bioreactor of one (CCFP-MBR) as shown in Figure 1 and sewage treatment process process 10000m
3the sanitary sewage of/d.
Design influent quality:
COD
cr400mg/L；NH
3-N40mg/L；TP3mg/L；SS180mg/L
Effluent quality requires: reach the one-level A standard in " urban wastewater treatment firm pollutant emission standard " (GB18918-2002).
Relevant design parameter is as follows: water inlet average discharge 416.67m
3/ h; Peak flow 658.33m
3/ h; Design anaerobic zone 1 mixed solution concentration of suspension MLSS is that 2600mg/L(actual motion can by 2000 ~ 3000mg/L), oxygen-starved area 2 mixed solution concentration of suspension MLSS is that 5650mg/L(actual motion can by 4800 ~ 6000mg/L), aerobic zone 3 mixed solution concentration of suspension MLSS is that 7000mg/L(actual motion can by 7000 ~ 9000mg/L); The maximum sludge loading 0.13kgBOD in aerobic zone 3
5/ kgMLSSd; Anaerobic zone 1 hydraulic detention time 1.5h, basin's effective volume 625.00m
3; Oxygen-starved area 2 hydraulic detention time 3.23h, basin's effective volume 1345m
3; The hydraulic detention time 7.57h of aerobic zone 3, basin's effective volume 3153m
3; Design available depth 5.0m; The denitrification load values scope of oxygen-starved area 2 is 0.03 ~ 0.04kgNO
3 --N/kgMLSSd(20 DEG C); Membrane biological reaction district 4 is provided with 4 Ge Mo districts, parallel running, design membrane flux 10 ~ 15L/m
2h; Oxygen-starved area 2 return current ratio of the mixed liquid 100%(actual motion can by 50% ~ 150%); Aerobic zone 3 return current ratio of the mixed liquid 150%(actual motion can by 100% ~ 200%).
Main units: 1 group of CCFP-MBR biochemical reaction tank as shown in Figure 1, overall size L × B × H=51.2m × 20m × 5.5m.
Major equipment: push flowing diving mixer 15,2 is established in anaerobic zone 1, separate unit power 1.5kW; Push flowing diving mixer 15,2 is established in oxygen-starved area 2, separate unit power 1.1kW; Push flowing diving mixer 15,2 is established in aerobic zone 3, separate unit power 1.1kW; 25,1 group, stripping reflux device is established in oxygen-starved area 2; 24,1 group, stripping reflux device is established in aerobic zone; Film district water distribution weir gate 11,4, B × H=600mm × 600mm, supporting manual opening-closing machine; Film district effluent weir gate 12,4, B × H=600mm × 600mm, supporting manual opening-closing machine; Recycle ratio adjustable checkgate 23,1, B × H=500mm × 1200mm, supporting manual opening-closing machine; Immersion type membrane component (ultra filtration hollow fiber membrane) some groups, single group filtration area 25m
2; Root's blower 3, air quantity 25.1m
3/ min, blast 6.0m, power 37kW.
Actual motion effect: ton water power consumption 0.2-42kw.h/m
3, the one-level A standard during effluent quality reaches " urban wastewater treatment firm pollutant emission standard " (GB18918-2002).
Embodiment 2
Adopt the circulation flow ring-shaped membrane bioreactor of one (CCFP-MBR) as shown in Figure 1 and sewage treatment process process 5000m
3the sanitary sewage of/d.
Design influent quality:
COD
cr350mg/L；NH
3-N35mg/L；TP4mg/L；SS200mg/L
Effluent quality requires: reach the one-level A standard in " urban wastewater treatment firm pollutant emission standard " (GB18918-2002).
Relevant design parameter is as follows: water inlet average discharge 208.33m
3/ h; Peak flow 362.50m
3/ h; Design anaerobic zone 1 mixed solution concentration of suspension MLSS is that 3000mg/L(actual motion can by 2000 ~ 3000mg/L), design oxygen-starved area 2 mixed solution concentration of suspension MLSS is that 6000mg/L(actual motion can by 4500 ~ 6000mg/L), design aerobic zone 3 mixed solution concentration of suspension MLSS is that 8000mg/L(actual motion can by 7500 ~ 9000mg/L); The maximum sludge loading 0.145kgBOD in aerobic zone 3
5/ kgMLSSd; Anaerobic zone 1 hydraulic detention time 1.5h, basin's effective volume 312.5m
3; Oxygen-starved area 2 hydraulic detention time 2.15h, basin's effective volume 447.77m
3; The hydraulic detention time 4.96h of aerobic zone 3, basin's effective volume 1034.31m
3; Design available depth 5.0m; The denitrification load values scope of oxygen-starved area 2 is 0.03 ~ 0.035kgNO
3 --N/kgMLSSd(20 DEG C); Membrane biological reaction district 4 is provided with 4 lattice membrane biological reaction subregions, parallel running, design membrane flux 10 ~ 15L/m
2h; Oxygen-starved area 2 return current ratio of the mixed liquid 100%(actual motion is according to 50% ~ 100%); Aerobic zone 3 phegma reflux ratio 150%(actual motion is according to 100% ~ 150%).
Main units: 1 group of CCFP-MBR biochemical reaction tank as shown in Figure 1, overall size L × B × H=24m × 15m × 5.5m.
Major equipment: push flowing diving mixer 15,2 is established in anaerobic zone 1, separate unit power 0.75kW; Push flowing diving mixer 15,2 is established in oxygen-starved area 2, separate unit power 0.37kW; Push flowing diving mixer 15,2 is established in aerobic zone 3, separate unit power 0.37kW; 25,1 group, stripping reflux device is established in oxygen-starved area 2; 24,1 group, stripping reflux device is established in aerobic zone 3; Film district water distribution weir gate 11,4, B × H=500mm × 500mm, supporting manual opening-closing machine; Film district effluent weir gate 12,4, B × H=500mm × 500mm, supporting manual opening-closing machine; Recycle ratio adjustable checkgate 23,1, B × H=300mm × 1000mm, supporting manual opening-closing machine; Immersion type membrane component (ultra filtration hollow fiber membrane) some groups, single group filtration area 25m
2; Root's blower 3, air quantity 16.5m
3/ min, blast 6.0m, power 30kW.
Actual motion effect: ton water power consumption 0.30kw.h/m
3, the one-level A standard during effluent quality reaches " urban wastewater treatment firm pollutant emission standard " (GB18918-2002).
Embodiment 3
Adopt the circulation flow ring-shaped membrane bioreactor of one (CCFP-MBR) as shown in Figure 1 and sewage treatment process process 30000m
3the sanitary sewage of/d.
Design influent quality:
COD
cr450mg/L；NH
3-N40mg/L；TP4mg/L；SS200mg/L
Effluent quality requires: reach the one-level A standard in " urban wastewater treatment firm pollutant emission standard " (GB18918-2002).
Relevant design parameter is as follows: water inlet average discharge 1250m
3/ h; Peak flow 1812.50m
3/ h; Design anaerobic zone 1 mixed solution concentration of suspension MLSS is that 2000mg/L(actual motion can by 1800 ~ 3000mg/L), design oxygen-starved area 2 mixed solution concentration of suspension MLSS is that 6000mg/L(actual motion can by 4800 ~ 6000mg/L), design aerobic zone 3 mixed solution concentration of suspension MLSS is that 8000mg/L(actual motion can by 7500 ~ 9000mg/L); The maximum sludge loading 0.139kgBOD in aerobic zone 3
5/ kgMLSSd; Anaerobic zone 1 hydraulic detention time 1.5h, basin's effective volume 1875.00m
3; Oxygen-starved area 2 hydraulic detention time 2.41h, basin's effective volume 3012.68m
3; The hydraulic detention time 6.67h of aerobic zone 3, basin's effective volume 8340.84m
3; Design available depth 5.5m; The denitrification load values scope of oxygen-starved area 2 is 0.035 ~ 0.04kgNO
3 --N/kgMLSSd(20 DEG C); Membrane biological reaction district 4 is provided with 5 lattice membrane biological reaction subregions, parallel running, design membrane flux 10 ~ 15L/m
2h; Oxygen-starved area 2 return current ratio of the mixed liquid 50%(actual motion can by 50% ~ 100%); Aerobic zone 3 return current ratio of the mixed liquid 200%(actual motion can by 100% ~ 200%).
Main units: CCFP-MBR biochemical reaction tank as shown in Figure 1,2 sets in parallel operation, single packet size L × B × H=38m × 20m × 6.0m.
Major equipment: push flowing diving mixer 4 (often organizing 2) is established in anaerobic zone 1, separate unit power 2.2kW; Push flowing diving mixer 4 (often organizing 2) is established in oxygen-starved area 2, separate unit power 1.1kW; Push flowing diving mixer 4 (often organizing 2) is established in aerobic zone 3, separate unit power 2.2kW; 25,1 group, stripping reflux device is established in oxygen-starved area 2; 24,1 group, stripping reflux device is established in aerobic zone 3; Film district water distribution weir gate 11,4, B × H=500mm × 500mm, supporting manual opening-closing machine; Film district effluent weir gate 12,4, B × H=500mm × 500mm, supporting manual opening-closing machine; Recycle ratio adjustable checkgate 23,1, B × H=500mm × 1200mm, supporting manual opening-closing machine; Immersion type membrane component (ultra filtration hollow fiber membrane) some groups, single group filtration area 25m
2; Root's blower 6, air quantity 48.9m
3/ min, blast 7.0m, power 90kW.
Actual motion effect: ton water power consumption 0.31kw.h/m
3, the one-level A standard during effluent quality reaches " urban wastewater treatment firm pollutant emission standard " (GB18918-2002).
Claims (10)
1. a circulation flow ring-shaped membrane bioreactor effluent treatment process, for carrying out sewage disposal by circulation flow ring-shaped membrane bioreactor; Described circulation flow ring-shaped membrane bioreactor comprise set up successively anaerobic zone (1), oxygen-starved area (2), aerobic zone (3) and the membrane biological reaction district (4) that is arranged in aerobic zone (3); Described sewage treatment process comprises the following steps:
(A) first sewage enter described anaerobic zone (1), mix with the phegma from oxygen-starved area (2), anaerobic zone (1) interior polyP bacteria releases phosphorus under anaerobic environment, transforms the organic pollutant of easily degraded simultaneously, and part itrogenous organic substance is carried out ammonification;
(B) then enter oxygen-starved area (2), mix with the phegma from aerobic zone (3), carry out denitrification process and carry out denitrogenation in oxygen-starved area (2), partial organic substances is degraded removal under the effect of denitrifying bacteria;
(C) then enter aerobic zone (3), carry out the absorption of the nitrated and phosphorus of organic further degraded and ammonia;
(D) then enter membrane biological reaction district (4) and carry out solid-liquid separation, purify waste water and to be discharged by pump, concentrated sludge part is circulated to aerobic zone (3), and along with aerobic zone (3) to oxygen-starved area (2) and oxygen-starved area (2) are to the reflux cycle of the mixed solution of anaerobic zone (1) in whole reaction zone, maintain sludge concentration higher in reactor, outside excess sludge, drain into sludge thickener;
Described anaerobic zone (1) comprises anaerobic zone A (1a) and anaerobic zone B (1b); First sewage enter anaerobic zone A (1a), descending flowing under the stirring pushing effect of the push flowing diving mixer arranged in anaerobic zone A (1a), then enter in anaerobic zone B (1b), up flowing under the stirring pushing effect of the push flowing diving mixer arranged in anaerobic zone B (1b); Then a part is circulated in anaerobic zone A (1a), and a part enters oxygen-starved area (2);
Described oxygen-starved area (2) comprises oxygen-starved area A (2a) and oxygen-starved area B (2b); First sewage from anaerobic zone (1) enter oxygen-starved area A (2a), descending flowing under the stirring pushing effect of the push flowing diving mixer arranged in oxygen-starved area A (2a), then oxygen-starved area B (2b) is entered, up flowing under the stirring pushing effect of the push flowing diving mixer arranged in oxygen-starved area B (2b), then a part is circulated in oxygen-starved area A (2a), and a part enters aerobic zone (3);
Described aerobic zone (3) comprises aerobic zone A (3a) and aerobic zone B (3b), described membrane biological reaction district (4) is positioned at aerobic zone B (3b), first sewage from oxygen-starved area (2) enter aerobic zone A (3a), right lateral flowing under the stirring pushing effect of the push flowing diving mixer arranged in aerobic zone A (3a), then aerobic zone B (3b) is entered, after mixing with the partial concentration mud from membrane biological reaction district (4), left lateral flowing under the stirring pushing effect of the push flowing diving mixer arranged in aerobic zone B (3b), then a part is circulated in aerobic zone A (3a), a part is circulated in the A of aerobic zone by the recycle ratio adjustable checkgate (23) arranged between aerobic zone A (3a) and aerobic zone B (3b), residue enters in membrane biological reaction district (4) carries out solid-liquid separation,
Sewage in described aerobic zone B (3b) enters membrane biological reaction district (4) by the film district water distribution weir gate (11) of membrane biological reaction district (4) side and carries out solid-liquid separation, local high microorganism concentration range is formed in membrane biological reaction district (4), purifying waste water of being separated is expelled to outside battery limit (BL) by pump, be separated the thickened sludge part formed and be expelled to aerobic zone B (3b) by film district effluent weir gate (12) being positioned at membrane biological reaction district (4) opposite side, residue thickened sludge is expelled to sludge thickener by mud overboard pump.
2. a kind of circulation flow ring-shaped membrane bioreactor effluent treatment process as claimed in claim 1, is characterized in that, described membrane biological reaction district (4) is arranged in parallel multiple separate membrane biological reaction subregion; Each described membrane biological reaction subregion is provided with film district water distribution weir gate (11) and film district effluent weir gate (12).
3. a kind of circulation flow ring-shaped membrane bioreactor effluent treatment process as claimed in claim 2, it is characterized in that, the mixed solution of oxygen-starved area A (2a) is back in anaerobic zone A (1a) by the air lift unit I (25) of arranged transversely in the mode of air-lift unit; The air lift unit II (24) of the mixed solution of aerobic zone B (3b) by arranged transversely is back in oxygen-starved area A (2a) in the mode of air-lift unit.
4. a kind of circulation flow ring-shaped membrane bioreactor effluent treatment process as claimed in claim 3, is characterized in that, the reflux ratio of described oxygen-starved area A (2a) mixed solution is 50%-200%; The reflux ratio of the mixed solution of described aerobic zone B (2b) is 100%-400%.
5. a kind of circulation flow ring-shaped membrane bioreactor effluent treatment process as claimed in claim 4, it is characterized in that, when designing sludge concentration and being lower, in described aerobic zone (3), sludge condensation district is set, thickened sludge, after described sludge condensation district makes preliminary sedimentation, is directly back to anaerobic zone (1) by aerobic zone (3) mixed solution.
6. a kind of circulation flow ring-shaped membrane bioreactor effluent treatment process as claimed in claim 5, is characterized in that, described aerobic zone (3) are provided with blast aerator; Described blast aerator comprises to be located at micro-pore aeration system in aerobic zone (3) and to be located at aerobic zone (3) gas blower outward; Described oxygen-starved area is provided with micro-pore aeration system in (2), makes described oxygen-starved area (2) leave the air consumption of 15-20% by described micro-pore aeration system.
7. a kind of circulation flow ring-shaped membrane bioreactor effluent treatment process as claimed in claim 6, it is characterized in that, by described push flowing diving mixer, the mean velocity in section of described circulation flow ring-shaped membrane bioreactor internal recycle current, is being controlled as 0.1-0.15m/s under having aeration condition for 0.3-0.5m/s without controlling under aeration condition.
8. a kind of circulation flow ring-shaped membrane bioreactor effluent treatment process as claimed in claim 7, is characterized in that, described anaerobic zone (1) interior hydraulic detention time is 1-2 hour; 20 DEG C of denitrification load values scopes of described oxygen-starved area (2) are 0.03 ~ 0.06kgNO
3 --N/ (kgMLSSd); The sludge loading value of described aerobic zone (3) is 0.1 ~ 0.2kgBOD
5/ (kgMLSSd).
9. a kind of circulation flow ring-shaped membrane bioreactor effluent treatment process as claimed in claim 8, is characterized in that, the energy density of described anaerobic zone (1) is 4 ~ 5W/m
3; The energy density of oxygen-starved area (2) is 1 ~ 2W/m
3; The energy density of aerobic zone (3) is 0.5 ~ 1.5W/m
3.
10. a kind of circulation flow ring-shaped membrane bioreactor effluent treatment process as claimed in claim 9, it is characterized in that, the sludge concentration of described anaerobic zone (1) is 1500-3000mg/L, the sludge concentration of described oxygen-starved area (2) is 3000-6000mg/L, and the sludge concentration of described aerobic zone (3) is 6000-12000mg/L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310531125.2A CN103570129B (en) | 2013-10-30 | 2013-10-30 | A kind of circulation flow ring-shaped membrane bioreactor effluent treatment process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310531125.2A CN103570129B (en) | 2013-10-30 | 2013-10-30 | A kind of circulation flow ring-shaped membrane bioreactor effluent treatment process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103570129A CN103570129A (en) | 2014-02-12 |
| CN103570129B true CN103570129B (en) | 2015-08-12 |
Family
ID=50042937
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310531125.2A Active CN103570129B (en) | 2013-10-30 | 2013-10-30 | A kind of circulation flow ring-shaped membrane bioreactor effluent treatment process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103570129B (en) |
Families Citing this family (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104118969B (en) * | 2014-07-08 | 2016-02-17 | 广州市市政工程设计研究总院 | A kind of A2O-MBR waste disposal plant and method |
| EP3209411B1 (en) | 2014-10-22 | 2022-05-18 | Koch Separation Solutions, Inc. | Membrane module system with bundle enclosures and pulsed aeration |
| USD779631S1 (en) | 2015-08-10 | 2017-02-21 | Koch Membrane Systems, Inc. | Gasification device |
| CN107777828A (en) * | 2016-08-26 | 2018-03-09 | 广州市环境保护工程设计院有限公司 | A kind of integrated sewage treatment device and its sewage water treatment method |
| CN109748450A (en) * | 2017-11-06 | 2019-05-14 | 天津万品科技有限公司 | A kind of integrated sewage disposal small testing device and process |
| CN108383320B (en) * | 2017-12-25 | 2024-01-05 | 湖南新九方科技有限公司 | Integrated treatment method for livestock and poultry breeding wastewater |
| CN109052647B (en) * | 2018-08-23 | 2021-07-13 | 浙江开创环保科技股份有限公司 | Integrated multi-state nitrogen and phosphorus removal equipment and method |
| CN109534625B (en) * | 2019-01-25 | 2020-12-11 | 清华大学 | Method for enhanced phosphorus removal of membrane bioreactor |
| CN110563283A (en) * | 2019-10-12 | 2019-12-13 | 昆明金泽实业有限公司 | Air stripping formula backward flow integrates MBR sewage treatment device |
| CN110862142A (en) * | 2019-12-20 | 2020-03-06 | 格蓝特环保工程(北京)有限公司 | High-efficiency membrane bioreactor and sewage treatment method |
| CN111003807A (en) * | 2019-12-25 | 2020-04-14 | 江苏清泉环保集团有限公司 | Labyrinth type integrated MBR (membrane bioreactor) |
| CN115367877B (en) * | 2022-08-24 | 2023-07-14 | 上海禾元环保集团有限公司 | Reactor and method for biological denitrification and dephosphorization by continuous circulation flow |
| CN115353205B (en) * | 2022-10-21 | 2023-02-17 | 北京博汇特环保科技股份有限公司 | Biochemical reaction system and sewage treatment method |
| CN115353206B (en) * | 2022-10-21 | 2023-02-17 | 北京博汇特环保科技股份有限公司 | Biochemical reaction equipment and sewage treatment method |
| CN117209062A (en) * | 2023-09-14 | 2023-12-12 | 上海禾元环保集团有限公司 | Circulation flow biochemical treatment reactor and method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20020044820A (en) * | 2000-12-06 | 2002-06-19 | 방정섭 | Management Unit and Method of Foul and Waste Water |
| JP2007160147A (en) * | 2005-12-09 | 2007-06-28 | Mitsubishi Heavy Ind Ltd | Advanced sewage treatment method and system |
| CN101092270A (en) * | 2007-06-08 | 2007-12-26 | 沈阳建筑大学 | Biological reactor of polygonal line flowing film |
| CN102515431A (en) * | 2011-12-14 | 2012-06-27 | 郑州大学 | Integrated technology for high efficiency nitrogen and phosphorus removal based on sludge emission reduction and device thereof |
-
2013
- 2013-10-30 CN CN201310531125.2A patent/CN103570129B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20020044820A (en) * | 2000-12-06 | 2002-06-19 | 방정섭 | Management Unit and Method of Foul and Waste Water |
| JP2007160147A (en) * | 2005-12-09 | 2007-06-28 | Mitsubishi Heavy Ind Ltd | Advanced sewage treatment method and system |
| CN101092270A (en) * | 2007-06-08 | 2007-12-26 | 沈阳建筑大学 | Biological reactor of polygonal line flowing film |
| CN102515431A (en) * | 2011-12-14 | 2012-06-27 | 郑州大学 | Integrated technology for high efficiency nitrogen and phosphorus removal based on sludge emission reduction and device thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103570129A (en) | 2014-02-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103570129B (en) | A kind of circulation flow ring-shaped membrane bioreactor effluent treatment process | |
| CN105254008B (en) | A kind of circulation flow ring-shaped multistage Activated sludge-biofilm composite type bioreactor and its sewage treatment process | |
| CN104030443B (en) | A kind of intensified denitrification and dephosphorization of urban sewage system and treatment process thereof based on fine-grained management | |
| CN106565017B (en) | A kind of bicirculating denitrogenation dephosphorizing waste water treatment system and its method | |
| CN102180543B (en) | Highly-efficient stable bio-doubling sewage treatment device | |
| CN103373794A (en) | Sewage treatment process and special-purpose one-piece sewage treatment plant | |
| CN205258127U (en) | Circulatory flow loop type multistage sludge -biofilm intergrowth combined type bioreactor | |
| CN103723896A (en) | Integrated sewage disposal system and disposal method | |
| CN207986809U (en) | The AAO biochemical treatment tanks of treated sewage | |
| CN203999260U (en) | A kind of synchronous denitrification dephosphorizing film bioreactor device | |
| CN202881052U (en) | Device for removing phosphorus chemically and forcibly by adopting A2O, membrane separation and cloth filter filtering | |
| CN206970300U (en) | Nitrification liquid reflux and biological reaction pool for biological reaction pool | |
| CN103183454A (en) | Coupling type biological denitrification method and system thereof | |
| CN203768177U (en) | Integrated sewage treatment system | |
| CN201325907Y (en) | Sewage treatment system for oxidation ditch | |
| CN105293701A (en) | Carbon source reserve type immobilized bioreactor (IBR) | |
| CN203558920U (en) | Circulation flow annular type membrane bioreactor | |
| CN209210482U (en) | Integrated rural sewage-treatment plant associated with a kind of AAO and SBR technique | |
| CN209193638U (en) | A kind of Small Towns advanced sewage treatment system of photovoltaic solar driving | |
| CN203159405U (en) | Coupled biological denitrification system | |
| CN201999827U (en) | High-efficiency stable sewage treatment device with bio-doubling process | |
| CN110540348B (en) | High-efficiency sewage nitrogen and phosphorus removal treatment process and equipment | |
| CN113698051A (en) | Sewage treatment station upgrading reconstruction treatment system and sewage treatment method | |
| CN201915003U (en) | Novel side channel-type integrated bioreactor sewage treatment device | |
| CN201971710U (en) | Municipal wastewater treatment biochemical reaction tank |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C53 | Correction of patent for invention or patent application | ||
| CB02 | Change of applicant information |
Address after: 200092, room 1121, No. two, 801 North Road, Zhongshan, Shanghai, Yangpu District Applicant after: SHANGHAI CITIC WATER INDUSTRY CO., LTD. Address before: 200092, room 1121, No. two, 801 North Road, Zhongshan, Shanghai, Yangpu District Applicant before: Shanghai Aton Environmental Limited Liability Company |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: APPLICANT; FROM: SHANGHAI ATON ENVIRONMENTAL LIMITED LIABILITY COMPANY TO: SHANGHAI ZHONGXIN WATER INDUSTRY CO., LTD. |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20181129 Address after: 610101 Chengdu Economic and Technological Development Zone, Sichuan Province, No. 888 Chengdu Chenglong Avenue Section 2 Patentee after: Sichuan Rongxinkai Engineering Design Co., Ltd. Address before: Room 801, 1121 Zhongshan North Second Road, Yangpu District, Shanghai, 200092 Patentee before: SHANGHAI CITIC WATER INDUSTRY CO., LTD. |