CN202089817U - Purifying device of air lifted type external tubular membrane bioreactor - Google Patents
Purifying device of air lifted type external tubular membrane bioreactor Download PDFInfo
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- CN202089817U CN202089817U CN2011201030580U CN201120103058U CN202089817U CN 202089817 U CN202089817 U CN 202089817U CN 2011201030580 U CN2011201030580 U CN 2011201030580U CN 201120103058 U CN201120103058 U CN 201120103058U CN 202089817 U CN202089817 U CN 202089817U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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Abstract
The utility model relates to a purifying device of an air lifted type external tubular membrane bioreactor, which relates to a tubular membrane bioreactor for treating and recycling organic wastewater. The purifying device of the air lifted type external tubular membrane bioreactor comprises a bioreactor (P1), a water feeding pump (P2), a circulating pump (P3), a tubular membrane component (P4), an air distributor (P5), an air compressor (P6), a backwashing pump (P7), an additive feeding pump (P8) and multiple sets of pneumatic valves (V1, V2, V3, V4, V5, V6, V7 and V8). A vertical barrel-shaped shell (5) is provided with upper and lower seal heads (6 and 7) and closed by upper and lower seals (8 and 9) so as to form the total tubular membrane component (P4). Flowing speed of mixed fluid, which enters the membrane component, on a membrane surface of a membrane tube (10) achieves 1-3meters per second by the aid of compressed air and gas , electric consumption of the purifying device can be reduced to 0.2-0.3 kilowatt per ton of water and is only one-tenth of that of general large cross flow, but water yield can achieve 90-110L/m2h, and the water yield of the purifying device is ten times higher than that of an existing purifying device comprising an immersed type hollow fiber membrane.
Description
Technical field:
The utility model relates to treatment of Organic Wastewater reuse tubular membrane biological reaction apparatus.
Background technology:
Present membrane bioreactor adopts " immersion hollow fiber film assembly " membrane module to be placed in the biochemistry pool extremely mostly, take suction type filtering, by vacuum primingpump or vacuum take-off, source water sees through hollow-fibre membrane and realizes that solid-liquid separation purifies, because the control of suction type operating variable is little, has only 8-12L/m2h, flow is relatively low, and, has the risk that generates biological pollution, during matting because membrane module is immersed in the sewage that has a large amount of microorganisms for a long time, can only carry out by off-line, this is unfavorable for extensive continous-stable operation, and the membrane module life-span is short, generally has only 1-2.
General external membrane bioreactor is that film device is placed outside biochemistry pool.The former water of biochemistry pool is in the same place film device and biochemistry pool by service pump and recycle pump continuously.See through liquid to clean water basin, dense water returns biochemistry pool, because the mixed liquor suspended solid, MLSS in the biochemistry pool is dense.Dirty stifled for preventing membrane module, this external membrane bioreactor must adopt the streamed solid-liquid separation of carrying out of serious mistake, for reaching the filtration velocity of per second 1-3 rice, usually the ratio of quantity of circulating water and water production rate reaches 10: 1, promptly produce 1 ton and see through liquid, need 10 tons the former water cycle water yield, the power consumption of this big cross-flow will reach 3-5 degree electricity/ton water usually, is apparent that high energy consumption.
Summary of the invention:
The purpose of this utility model is to provide the external tubular membrane bio-reactor of a kind of gas stripping type refining plant.
It comprises bio-reactor (P1), service pump (P2), recycle pump (P3), tubular membrane component (P4), gas pipe (P5), air compressor (P6), backwashing pump (P7), dosing pump (P8) and many group operated pneumatic valve (V1, V2 ... V8); Water in the bio-reactor (P1) after biological treatment enters recycle pump (P3) successively through service pump (P2), operated pneumatic valve (V1), and water-in (1), water distributing pore (13), film pipe (10) produces the mouth of a river (4), and operated pneumatic valve (V8) is to clean water basin; Water outlet/air outlet (3) connects operated pneumatic valve (V6) successively, and bio-reactor (P1) is to emptier; Water-in (1) connects operated pneumatic valve (V5) successively, backwash blow-off pipe, bio-reactor (P1); Air arrives operated pneumatic valve (V2) through air compressor (P6) compression one tunnel, the inlet mouth (2) of tubular membrane component (P4), and one the road to operated pneumatic valve (V4), and operated pneumatic valve (V3, V7, V8) is to producing water out (4); Clean water basin connect backwashing pump (P7) successively, operated pneumatic valve (V3); Dosing tank connects dosing pump (P8) successively to operated pneumatic valve (V7).
Tubular membrane component (P4) is that a vertical drum shape shell (5) adds, lower cover (6,7) is used, lower seal (8,9) sealed whole; Upper cover (6) is provided with and produces water out (4) and water outlet/air outlet (3); Lower cover (7) is provided with water-in (1) and inlet mouth (2); Air distribution plate (15), qi-emitting hole (14) and film pipe (10) vertically are set in the shell (5), some water distribution/qi-emitting holes of arranged transversely (12) and water distributing pore (13), the centre is provided with plug (11).
Film pipe (10) is made up of basement membrane and pellicle; Basement membrane is formed by the ultrahigh molecular weight polyethylene(UHMWPE) sintering of sintering process preparation, and pellicle is a polyvinylidene difluoride (PVDF).
A gas pipe with the superhigh molecular weight polyethylene material sinter molding (P5) is equipped with in tubular membrane component (P4) bottom.
The utility model is that the mixed solution that utilizes pressurized air gas will enter in the membrane module reaches the 1-3 meter per second at the crossflow velocity of film pipe (10), its power consumption can be reduced to 0.2-0.3 degree electricity/ton water, power consumption only is equivalent to 1/10th of general big cross-flow, and water production rate can reach 90-110L/m2h, is 10 times of immersion hollow-fibre membrane.
Description of drawings:
Accompanying drawing 1 is the main pseudosection of the utility model tubular membrane component;
Accompanying drawing 2 be the A-A of the utility model Fig. 1 to sectional view:
Accompanying drawing 3 is system construction drawings of the present utility model;
Accompanying drawing 4 is tubular membrane component parameter lists of the present utility model.
Embodiment:
The utility model comprises bio-reactor (P1), service pump (P2), recycle pump (P3), tubular membrane component (P4), gas pipe (P5), air compressor (P6), backwashing pump (P7), dosing pump (P8) and many group operated pneumatic valve (V1, V2 ... V8); Water in the bio-reactor (P1) after biological treatment is through service pump (P2) → recycle pump (P3) → operated pneumatic valve (V1) → water-in (1) → water distributing pore (13) → film pipe (10) → product mouth of a river (4) → operated pneumatic valve (V8) → clean water basin; Water outlet/air outlet (3) → operated pneumatic valve (V6) → bio-reactor (P1), emptier; Water-in (1) → operated pneumatic valve (V5) → backwash blow-off pipe → bio-reactor (P1); Air is through the inlet mouth (2) of air compressor (P6) compression one tunnel → operated pneumatic valve (V2) → tubular membrane component (P4), one tunnel → operated pneumatic valve (V4) → operated pneumatic valve (V3, V7, V8) → product water out (4); Clean water basin → backwashing pump (P7) → operated pneumatic valve (V3); Dosing tank → dosing pump (P8) → operated pneumatic valve (V7); Tubular membrane component (P4) is that a vertical drum shape shell (5) adds, lower cover (6,7) is used, lower seal (8,9) sealed whole; Upper cover (6) is provided with and produces water out (4) and water outlet/air outlet (3); Lower cover (7) is provided with water-in (1) and inlet mouth (2); Air distribution plate (15), qi-emitting hole (14) and film pipe (10) vertically are set in the shell (5), some water distribution/qi-emitting holes of arranged transversely (12) and water distributing pore (13), the centre is provided with plug (11).Film pipe (10) is made up of basement membrane and pellicle; Basement membrane is formed by the ultrahigh molecular weight polyethylene(UHMWPE) sintering of sintering process preparation, and pellicle is a polyvinylidene difluoride (PVDF).A gas pipe with the superhigh molecular weight polyethylene material sinter molding (P5) is equipped with in tubular membrane component (P4) bottom.
Basement membrane forms firm combining with pellicle, makes film pipe (10) can tolerate higher backwashing pressure (0.5MPa), and simultaneously, above-mentioned two kinds of materials all have powerful oxidation corrosion resistance, strong acid, alkaline ability.Comprehensive above-mentioned advantage, film pipe (1) helps quick on-line cleaning, thereby in high density, full-bodied water body filter, remains the continous-stable operation.
The gentle tolerance that provides of formation that tubular membrane component (P4) gas is carried: the design of gas pipe (P5) must be decided according to the packing density of tubular membrane inner membrance pipe.Formed bubble is not the smaller the better, and bubble must suitably can play scrubbing action between film pipe (10) space.The air demand of each tubular membrane component (P4) is at 0-20Nm3/h; Gas pressure-raising power＜0.05MPa is advisable.
Tubular membrane component (P4) working order:
1, filter:
When filtering, service pump (2) is sent the mixed solution in the biochemical reactor (1) into tubular membrane component (P4), and service pump (P2) is used to keep the constant flooding velocity, improves flow velocity through recycle pump (P3) and flows to the top from tubular membrane component (P4) bottom; Pressurized air compresses after the gas pipe of bottom (P5) is sent into even air in the cavity of tubular membrane component (P4) through air compressor (P6).Because the rising of air drives, driving mixed solution and suspended solids rises, keep certain flow velocity (1-3m/s) on film pipe (10) surface, air agitation is cleaned the film surface, take away the suspended particle and the colloid that cause film to pollute easily and stop up, mixed solution flows with the cross-flow form, is trapped within the film surface greater than the particle and the solute of fenestra, and make water be purified less than the seeing through membranous wall of fenestra, realize solid-liquid separation.Product water multiparity water out (4) after the purification, operated pneumatic valve (V8) enters clean water basin.Owing to be cross flow filter, dense water is got back to biochemical reactor (P1) through operated pneumatic valve (V6), makes that sludge concentration constantly increases in the biochemical reactor (P1), helps the organic matter degradation that further difficulty decomposed, thereby improves biochemical effect; Air is through the emptying of emptying pipeline.
2, backwash:
In equipment running process, mud accumulates in the surface and fenestra of inner chamber, film pipe (10) of tubular membrane component (P4), is the normal operation that keeps system.These pollutents must regularly be discharged by back flushing.
In the backwash process, open air compressor (P6), oil-free compressed air is through operated pneumatic valve (V4), product water out (4) enters in the chamber of tubular membrane component (P4) from the opposite direction of membrane filtration, its recoil pressure 0.5MPa, successive pulse formula back flushing 2-3 time, each time is 2-3 second.After the gas recoil, open the product water backwash 1-2min in backwashing pump (P7) the usefulness clean water basin again, process is: backwashing pump (P7) draws water from clean water basin and enters in the chamber of tubular membrane component (P4) from producing water out (4), flows out from water-in (1), gets back to biochemical reactor (P1) through the backwash blow-off pipe.At normal gas recoil, water backwash 15-20 all after dates, need strengthen backwash, promptly in the water backwash, add chemical agent carries out 10-15min to tubular membrane component (P4) immersion and cleaning by volume pump (8).Generally during 30-45 days, also need tubular membrane component (P4) is carried out matting completely, to recover the original flux of tubular membrane component (P4).
Claims (4)
1. the external tubular membrane bio-reactor of gas stripping type refining plant, it comprises bio-reactor (P1), service pump (P2), recycle pump (P3), tubular membrane component (P4), gas pipe (P5), air compressor (P6), backwashing pump (P7), dosing pump (P8) and many group operated pneumatic valve (V1, V2 ... V8), it is characterized in that: the water in the bio-reactor (P1) after biological treatment enters recycle pump (P3) successively through service pump (P2), operated pneumatic valve (V1), water-in (1), water distributing pore (13), film pipe (10), produce the mouth of a river (4), operated pneumatic valve (V8) is to clean water basin; Water outlet/air outlet (3) connects operated pneumatic valve (V6) successively, and bio-reactor (P1) is to emptier; Water-in (1) connects operated pneumatic valve (V5) successively, backwash blow-off pipe, bio-reactor (P1); Air arrives operated pneumatic valve (V2) through air compressor (P6) compression one tunnel, the inlet mouth (2) of tubular membrane component (P4), and one the road to operated pneumatic valve (V4), and operated pneumatic valve (V3, V7, V8) is to producing water out (4); Clean water basin connect backwashing pump (P7) successively, operated pneumatic valve (V3); Dosing tank connects dosing pump (P8) successively to operated pneumatic valve (V7).
2. the external tubular membrane bio-reactor of gas stripping type as claimed in claim 1 refining plant is characterized in that: tubular membrane component (P4) is that a vertical drum shape shell (5) adds, lower cover (6,7) is used, lower seal (8,9) sealed whole; Upper cover (6) is provided with and produces water out (4) and water outlet/air outlet (3); Lower cover (7) is provided with water-in (1) and inlet mouth (2); Air distribution plate (15), qi-emitting hole (14) and film pipe (10) vertically are set in the shell (5), some water distribution/qi-emitting holes of arranged transversely (12) and water distributing pore (13), the centre is provided with plug (11).
3. the external tubular membrane bio-reactor of gas stripping type as claimed in claim 1 or 2 refining plant, it is characterized in that: film pipe (10) is made up of basement membrane and pellicle; Basement membrane is formed by the ultrahigh molecular weight polyethylene(UHMWPE) sintering of sintering process preparation, and pellicle is a polyvinylidene difluoride (PVDF).
4. the external tubular membrane bio-reactor of gas stripping type as claimed in claim 1 or 2 refining plant is characterized in that: a gas pipe with the superhigh molecular weight polyethylene material sinter molding (P5) is equipped with in tubular membrane component (P4) bottom.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201030580U CN202089817U (en) | 2011-04-11 | 2011-04-11 | Purifying device of air lifted type external tubular membrane bioreactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201030580U CN202089817U (en) | 2011-04-11 | 2011-04-11 | Purifying device of air lifted type external tubular membrane bioreactor |
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| Publication Number | Publication Date |
|---|---|
| CN202089817U true CN202089817U (en) | 2011-12-28 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011201030580U Expired - Fee Related CN202089817U (en) | 2011-04-11 | 2011-04-11 | Purifying device of air lifted type external tubular membrane bioreactor |
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| CN (1) | CN202089817U (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102730816A (en) * | 2011-04-11 | 2012-10-17 | 金振忠 | Airlift external tubular membrane bioreactor purifier |
| CN103011394A (en) * | 2012-12-21 | 2013-04-03 | 东华大学 | Gravity air lift split type textile membrane bioreactor |
| CN103243024A (en) * | 2013-05-24 | 2013-08-14 | 河南农业大学 | Culture bottle for sulfur hexafluoride permeation tube |
| US9333464B1 (en) | 2014-10-22 | 2016-05-10 | Koch Membrane Systems, Inc. | Membrane module system with bundle enclosures and pulsed aeration and method of operation |
| USD779632S1 (en) | 2015-08-10 | 2017-02-21 | Koch Membrane Systems, Inc. | Bundle body |
| CN110228834A (en) * | 2019-05-31 | 2019-09-13 | 苏州英特工业水处理工程有限公司 | The gravity flow water treatment system that can be backwashed |
-
2011
- 2011-04-11 CN CN2011201030580U patent/CN202089817U/en not_active Expired - Fee Related
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102730816A (en) * | 2011-04-11 | 2012-10-17 | 金振忠 | Airlift external tubular membrane bioreactor purifier |
| CN103011394A (en) * | 2012-12-21 | 2013-04-03 | 东华大学 | Gravity air lift split type textile membrane bioreactor |
| CN103243024A (en) * | 2013-05-24 | 2013-08-14 | 河南农业大学 | Culture bottle for sulfur hexafluoride permeation tube |
| US9333464B1 (en) | 2014-10-22 | 2016-05-10 | Koch Membrane Systems, Inc. | Membrane module system with bundle enclosures and pulsed aeration and method of operation |
| US9956530B2 (en) | 2014-10-22 | 2018-05-01 | Koch Membrane Systems, Inc. | Membrane module system with bundle enclosures and pulsed aeration and method of operation |
| US10702831B2 (en) | 2014-10-22 | 2020-07-07 | Koch Separation Solutions, Inc. | Membrane module system with bundle enclosures and pulsed aeration and method of operation |
| USD779632S1 (en) | 2015-08-10 | 2017-02-21 | Koch Membrane Systems, Inc. | Bundle body |
| USD779631S1 (en) | 2015-08-10 | 2017-02-21 | Koch Membrane Systems, Inc. | Gasification device |
| CN110228834A (en) * | 2019-05-31 | 2019-09-13 | 苏州英特工业水处理工程有限公司 | The gravity flow water treatment system that can be backwashed |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Wuhan micro film science and Technology Industrial Co. Ltd. Assignor: Jin Zhenzhong Contract record no.: 2015420000071 Denomination of utility model: Airlift external tubular membrane bioreactor purifier Granted publication date: 20111228 License type: Common License Record date: 20150508 |
|
| LICC | Enforcement, change and cancellation of record of contracts on the licence for exploitation of a patent or utility model | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20111228 Termination date: 20150411 |
|
| EXPY | Termination of patent right or utility model |