CN202089817U - Purifying device of air lifted type external tubular membrane bioreactor - Google Patents

Purifying device of air lifted type external tubular membrane bioreactor Download PDF

Info

Publication number
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
Authority
CN
China
Prior art keywords
water
tubular membrane
pneumatic valve
air
pump
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Fee Related
Application number
CN2011201030580U
Other languages
Chinese (zh)
Inventor
金振忠
万荣群
金洪义
金丽
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Priority to CN2011201030580U priority Critical patent/CN202089817U/en
Application granted granted Critical
Publication of CN202089817U publication Critical patent/CN202089817U/en
Anticipated expiration legal-status Critical
Expired - Fee Related legal-status Critical Current

Links

Images

Classifications

    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02WCLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00Technologies for wastewater treatment
    • Y02W10/10Biological treatment of water, waste water, or sewage

Landscapes

  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

本实用新型气提式外置管式膜生物反应器净化装置,涉及有机废水处理回用管式膜生物反应装置;它包括生物反应器(P1)、给水泵(P2)、循环泵(P3)、管式膜组件(P4)、布气器(P5)、空气压缩机(P6)、反洗泵(P7)、加药泵(P8)和多组气动阀门(V1、V2……V8);管式膜组件(P4)是一个竖直的圆桶形外壳(5)加上、下封头(6、7)用上、下密封(8、9)密闭的整体;本实用新型是利用压缩空气气体将进入膜组件内的混合液在膜管(10)的膜面流速达到1-3米/秒,其电耗可降至0.2-0.3度电/吨水,电耗仅相当于一般大错流的十分之一,而产水量可达90-110L/m2h,是浸没式中空纤维膜的10倍。

Figure 201120103058

The utility model relates to an air-lift type external tubular membrane bioreactor purification device, which relates to a tubular membrane bioreactor for organic wastewater treatment and reuse; it includes a bioreactor (P1), a water supply pump (P2), and a circulation pump (P3) , Tubular membrane module (P4), air distributor (P5), air compressor (P6), backwash pump (P7), dosing pump (P8) and multiple sets of pneumatic valves (V1, V2...V8); Tubular membrane assembly (P4) is a vertical cylinder-shaped shell (5) plus, the lower head (6, 7) is sealed with the upper and lower seals (8, 9) as a whole; the utility model utilizes compression The air gas will enter the mixed liquid in the membrane module, and the membrane surface flow velocity of the membrane tube (10) reaches 1-3 m/s, and its power consumption can be reduced to 0.2-0.3 kWh/ton of water, which is only equivalent to that of a general large One-tenth of the cross-flow, and the water production rate can reach 90-110L/m 2 h, which is 10 times that of the submerged hollow fiber membrane.

Figure 201120103058

Description

气提式外置管式膜生物反应器净化装置Air lift type external tubular membrane bioreactor purification device

技术领域: Technical field:

本实用新型涉及有机废水处理回用管式膜生物反应装置。  The utility model relates to a tubular membrane biological reaction device for organic waste water treatment and reuse. the

背景技术: Background technique:

目前的膜生物反应器绝大多采用“浸没式中空纤维膜组件”膜组件安放在生化池内,采取抽吸式过滤,通过自吸泵或真空抽吸,源水透过中空纤维膜而实现固液分离净化,由于抽吸式工作变量控制小,只有8-12L/m2·h,流量相对较低,且由于膜组件长时间浸泡在拥有大量微生物的污水中,具有生成生物污染的风险,化学清洗时,只能离线进行,这不利于大规模连续稳定运行,膜组件寿命短,一般只有1-2年。  Most of the current membrane bioreactors use "submerged hollow fiber membrane module" membrane module placed in the biochemical pool, adopt suction filtration, through self-priming pump or vacuum suction, the source water passes through the hollow fiber membrane to achieve solid-liquid Separation and purification, due to the small control of the suction working variable, only 8-12L/m2·h, the flow rate is relatively low, and because the membrane module is immersed in the sewage with a large number of microorganisms for a long time, there is a risk of biological pollution, chemical cleaning It can only be done offline, which is not conducive to large-scale continuous and stable operation, and the life of the membrane module is short, generally only 1-2 years. the

一般的外置式膜生物反应器是将膜装置于生化池外放置。生化池的原水通过给水泵和循环泵使膜装置与生化池连续在一起。透过液至清水池,浓水返回生化池,由于生化池中的混合液悬浮固体浓度很高。为防止膜组件污堵,这种外置式膜生物反应器必须采用大错流形式进行固液分离,为达到每秒1-3米的过滤速度,通常循环水量和产水量的比例达到10∶1,即生产1吨透过液,需要10吨的原水循环水量,这种大错流的电耗通常要达到3-5度电/吨水,明显的是高能耗。  The general external membrane bioreactor is to place the membrane device outside the biochemical pool. The raw water in the biochemical pool is connected to the membrane device and the biochemical pool through the feed water pump and the circulation pump. The permeate is sent to the clear water tank, and the concentrated water is returned to the biochemical tank, because the mixed liquid in the biochemical tank has a high concentration of suspended solids. In order to prevent fouling of membrane modules, this external membrane bioreactor must adopt a large cross-flow form for solid-liquid separation. In order to achieve a filtration speed of 1-3 meters per second, the ratio of circulating water to produced water is usually 10:1. , that is, to produce 1 ton of permeate, 10 tons of raw water circulation is required. The power consumption of this large cross-flow usually reaches 3-5 kWh/ton of water, which is obviously high energy consumption. the

发明内容: Invention content:

本实用新型的目的在于提供一种气提式外置管式膜生物反应器净化装置。  The purpose of the utility model is to provide an air lift type external tubular membrane bioreactor purification device. the

它包括生物反应器(P1)、给水泵(P2)、循环泵(P3)、管式膜组件(P4)、布气器(P5)、空气压缩机(P6)、反洗泵(P7)、加药泵(P8)和多组气动阀门(V1、V2……V8);生物反应器(P1)中经生物处理后的水经给水泵(P2)依次进入循环泵(P3),气动阀门(V1),进水口(1),布水孔(13),膜管(10),产水口(4),气动阀门(V8)到清水池;出水/出气口(3)依次连接气动阀门(V6),生物反应器(P1)到排空装置;进水口(1)依次连接气动阀门(V5),反洗排污管,生物反应器(P1);空气经空气压缩机(P6)压缩一路到气动阀门(V2),管式膜组件(P4)的进气口(2),一路到气动阀门(V4),气动阀门(V3、V7、V8)到产水出口(4);清水池依次连接反洗泵(P7),气动阀门(V3);加药箱依次连接加药泵(P8)到气动阀门(V7)。  It includes bioreactor (P1), feed water pump (P2), circulation pump (P3), tubular membrane module (P4), air distributor (P5), air compressor (P6), backwash pump (P7), The dosing pump (P8) and multiple sets of pneumatic valves (V1, V2...V8); the biologically treated water in the bioreactor (P1) enters the circulation pump (P3) sequentially through the feed water pump (P2), and the pneumatic valves ( V1), water inlet (1), water distribution hole (13), membrane tube (10), water production port (4), pneumatic valve (V8) to the clean water pool; water/air outlet (3) is connected to the pneumatic valve (V6) in sequence ), the bioreactor (P1) to the emptying device; the water inlet (1) is sequentially connected to the pneumatic valve (V5), the backwash sewage pipe, and the bioreactor (P1); the air is compressed by the air compressor (P6) all the way to the pneumatic The valve (V2), the air inlet (2) of the tubular membrane module (P4), all the way to the pneumatic valve (V4), the pneumatic valves (V3, V7, V8) to the water outlet (4); Washing pump (P7), pneumatic valve (V3); dosing box connects dosing pump (P8) to pneumatic valve (V7) in turn. the

管式膜组件(P4)是一个竖直的圆桶形外壳(5)加上、下封头(6、7)用上、下密封(8、9)密闭的整体;上封头(6)设置产水出口(4)和出水/出气口(3);下封头(7)设置进水口(1)和进气口(2);外壳(5)内纵向设置布气板(15)、布气孔(14)和膜管(10),横向设置若干布水/布气孔(12)和布水孔(13),中间设置堵头(11)。  The tubular membrane module (P4) is a vertical cylindrical shell (5) plus the lower head (6, 7) sealed with the upper and lower seals (8, 9) as a whole; the upper head (6) Water production outlet (4) and water outlet/air outlet (3) are set; water inlet (1) and air inlet (2) are set on the lower head (7); air distribution plate (15), Air distribution holes (14) and membrane tubes (10), several water distribution/air distribution holes (12) and water distribution holes (13) are arranged horizontally, and plugs (11) are arranged in the middle. the

膜管(10)由基膜和表膜组成;基膜由烧结法制备的超高分子量聚乙烯烧结而成,表膜为聚偏氟乙烯。  The membrane tube (10) is composed of a base film and a surface film; the base film is sintered from ultra-high molecular weight polyethylene prepared by a sintering method, and the surface film is polyvinylidene fluoride. the

管式膜组件(P4)底部装有一个用超高分子量聚乙烯材料烧结成型的布气器(P5)。  The bottom of the tubular membrane module (P4) is equipped with an air distributor (P5) sintered with ultra-high molecular weight polyethylene material. the

本实用新型是利用压缩空气气体将进入膜组件内的混合液在膜管(10)的膜面流速达到1-3米/秒,其电耗可降至0.2-0.3度电/吨水,电耗仅相当于一般大错流的十分之一,而产水量可达 90-110L/m2h,是浸没式中空纤维膜的10倍。  The utility model utilizes compressed air gas to make the mixed solution entering the membrane module reach a flow rate of 1-3 m/s on the membrane surface of the membrane tube (10), and its power consumption can be reduced to 0.2-0.3 kWh/ton of water. The consumption is only equivalent to one tenth of the general large cross flow, and the water production can reach 90-110L/m2h, which is 10 times that of the submerged hollow fiber membrane. the

附图说明: Description of drawings:

附图1是本实用新型管式膜组件的主视剖面图;  Accompanying drawing 1 is the front sectional view of tubular membrane assembly of the present utility model;

附图2是本实用新型图1的A-A向剖面图:  Accompanying drawing 2 is the A-A to sectional view of Fig. 1 of the present utility model:

附图3是本实用新型的系统结构图;  Accompanying drawing 3 is the system structural diagram of the present utility model;

附图4是本实用新型的管式膜组件参数表。  Accompanying drawing 4 is the parameter list of tubular membrane module of the present utility model. the

具体实施方式: Detailed ways:

本实用新型包括生物反应器(P1)、给水泵(P2)、循环泵(P3)、管式膜组件(P4)、布气器(P5)、空气压缩机(P6)、反洗泵(P7)、加药泵(P8)和多组气动阀门(V1、V2……V8);生物反应器(P1)中经生物处理后的水经给水泵(P2)→循环泵(P3)→气动阀门(V1)→进水口(1)→布水孔(13)→膜管(10)→产水口(4)→气动阀门(V8)→清水池;出水/出气口(3)→气动阀门(V6)→生物反应器(P1),排空装置;进水口(1)→气动阀门(V5)→反洗排污管→生物反应器(P1);空气经空气压缩机(P6)压缩一路→气动阀门(V2)→管式膜组件(P4)的进气口(2),一路→气动阀门(V4)→气动阀门(V3、V7、V8)→产水出口(4);清水池→反洗泵(P7)→气动阀门(V3);加药箱→加药泵(P8)→气动阀门(V7);管式膜组件(P4)是一个竖直的圆桶形外壳(5)加上、下封头(6、7)用上、下密封(8、9)密闭的整体;上封头(6)设置产水出口(4)和出水/出气口(3);下封头(7)设置进水口(1)和进气口(2);外壳(5)内纵向设置布气板(15)、布气孔(14)和膜管(10),横向设置若干布水/布气孔(12)和布水孔(13), 中间设置堵头(11)。膜管(10)由基膜和表膜组成;基膜由烧结法制备的超高分子量聚乙烯烧结而成,表膜为聚偏氟乙烯。管式膜组件(P4)底部装有一个用超高分子量聚乙烯材料烧结成型的布气器(P5)。  The utility model includes a bioreactor (P1), a feed water pump (P2), a circulation pump (P3), a tubular membrane module (P4), an air distributor (P5), an air compressor (P6), a backwash pump (P7 ), dosing pump (P8) and multiple sets of pneumatic valves (V1, V2...V8); the biologically treated water in the bioreactor (P1) passes through the feed water pump (P2)→circulation pump (P3)→pneumatic valve (V1)→Water inlet (1)→Water distribution hole (13)→Membrane tube (10)→Water production port (4)→Pneumatic valve (V8)→Clear water pool; water/air outlet (3)→Pneumatic valve (V6 )→bioreactor (P1), emptying device; water inlet (1)→pneumatic valve (V5)→backwash sewage pipe→bioreactor (P1); air compressed by air compressor (P6) all the way→pneumatic valve (V2)→air inlet (2) of tubular membrane module (P4), one way→pneumatic valve (V4)→pneumatic valve (V3, V7, V8)→product water outlet (4); clean water tank→backwash pump (P7)→pneumatic valve (V3); dosing box→dosing pump (P8)→pneumatic valve (V7); tubular membrane module (P4) is a vertical drum-shaped shell (5) plus and bottom The sealing heads (6, 7) are sealed as a whole with upper and lower seals (8, 9); the upper sealing head (6) is provided with the water production outlet (4) and the water outlet/air outlet (3); the lower sealing head (7) is provided with Water inlet (1) and air inlet (2); air distribution plate (15), air distribution hole (14) and membrane tube (10) are arranged longitudinally in the casing (5), and several water distribution/air distribution holes (12) are arranged horizontally With water distribution hole (13), plug (11) is set in the middle. The membrane tube (10) is composed of a base film and a surface film; the base film is sintered from ultra-high molecular weight polyethylene prepared by a sintering method, and the surface film is polyvinylidene fluoride. The bottom of the tubular membrane module (P4) is equipped with an air distributor (P5) sintered with ultra-high molecular weight polyethylene material. the

基膜与表膜形成牢固的结合,使膜管(10)能耐受较高的反冲洗压力(0.5MPa),同时,上述两种材料都具有耐强氧化、强酸、强碱的能力。综合上述优点,膜管(1)有利于快速在线清洗,从而在高浓度、高粘度的水体过滤中,始终保持连续稳定运行。  The base film and the surface film form a firm combination, so that the film tube (10) can withstand a relatively high backwash pressure (0.5MPa). At the same time, the above two materials have the ability to resist strong oxidation, strong acid and strong alkali. Combining the above advantages, the membrane tube (1) is conducive to rapid online cleaning, so that it can always maintain continuous and stable operation in the filtration of high-concentration and high-viscosity water bodies. the

管式膜组件(P4)气提的形成和气提供气量:布气器(P5)的设计必须依据管式膜内膜管的装填密度而定。所形成的气泡不是越小越好,气泡必须适当能在膜管(10)空隙之间起到擦洗作用。每个管式膜组件(P4)的供气量在0-20Nm3/h;气提压力<0.05MPa为宜。  Formation of air lift of tubular membrane module (P4) and gas supply volume: The design of the air distributor (P5) must be determined according to the packing density of the inner membrane tube of the tubular membrane. The formed air bubbles are not as small as possible, and the air bubbles must be able to properly scrub between the gaps of the membrane tubes (10). The gas supply rate of each tubular membrane module (P4) is 0-20Nm3/h; the gas stripping pressure is preferably <0.05MPa. the

管式膜组件(P4)工作状态:  Working status of tubular membrane module (P4):

1、过滤:  1. Filtering:

在过滤时,给水泵(2)将生化反应器(1)中的混合液送入管式膜组件(P4),给水泵(P2)用于保持恒定的进水流量,经循环泵(P3)提高流速从管式膜组件(P4)底部流向顶部;压缩空气经过空气压缩机(P6)压缩后经底部的布气器(P5)将空气均匀送入管式膜组件(P4)的腔体中。由于空气的上升驱动,带动混合液和悬浮固体上升,在膜管(10)表面保持一定的流速(1-3m/s),空气搅动擦洗膜表面,带走容易造成膜污染和堵塞的悬浮颗粒和胶体,混合液以错流形式流动,大于膜孔的颗粒和溶质被截留在膜表面,而小于膜孔的透过膜壁而使得水得到净化,实现固液分离。净化后的产水经产水出口(4), 气动阀门(V8)进入清水池。由于是错流过滤,浓水经气动阀门(V6)回到生化反应器(P1),使得生化反应器(P1)中污泥浓度不断增加,有利于进一步将难分解的有机物降解,从而提高生化效果;空气经排空管路排空。  During filtration, the feed water pump (2) sends the mixed liquid in the biochemical reactor (1) into the tubular membrane module (P4), and the feed water pump (P2) is used to maintain a constant feed water flow rate, which is passed through the circulation pump (P3) Increase the flow rate from the bottom of the tubular membrane module (P4) to the top; the compressed air is compressed by the air compressor (P6) and sent to the cavity of the tubular membrane module (P4) evenly through the air distributor (P5) at the bottom . Driven by the rise of the air, the mixed liquid and suspended solids rise to maintain a certain flow rate (1-3m/s) on the surface of the membrane tube (10), and the air stirs and scrubs the surface of the membrane, taking away the suspended particles that are likely to cause membrane fouling and clogging And colloid, the mixed liquid flows in the form of cross flow, the particles and solutes larger than the membrane pores are trapped on the surface of the membrane, and the particles smaller than the membrane pores pass through the membrane wall to purify the water and realize the solid-liquid separation. The purified product water enters the clear water pool through the product water outlet (4) and the pneumatic valve (V8). Due to the cross-flow filtration, the concentrated water returns to the biochemical reactor (P1) through the pneumatic valve (V6), so that the sludge concentration in the biochemical reactor (P1) increases continuously, which is beneficial to further degrade the refractory organic matter, thereby improving the biochemical Effect; the air is evacuated through the evacuation line. the

2、反洗:  2. Backwashing:

在设备运行过程中,污泥聚积在管式膜组件(P4)的内腔、膜管(10)的表面和膜孔内,为保持系统的正常运行。这些污染物必须定期通过反冲洗排出。  During the operation of the equipment, sludge accumulates in the inner cavity of the tubular membrane module (P4), the surface of the membrane tube (10) and in the membrane holes, in order to maintain the normal operation of the system. These contaminants must be removed periodically by backwashing. the

反洗过程中,开启空气压缩机(P6),无油压缩空气经气动阀门(V4),产水出口(4)从膜过滤的反方向进入管式膜组件(P4)的腔内,其反冲压力0.5MPa,连续脉冲式反冲洗2-3次,每次时间是2-3秒。气反冲后,再开启反洗泵(P7)用清水池中的产水反洗1-2min,过程是:反洗泵(P7)从清水池抽水从产水出口(4)进入管式膜组件(P4)的腔内,从进水口(1)流出,经反洗排污管回到生化反应器(P1)。在正常气反冲、水反洗15-20个周期后,需进行加强反洗,即在水反洗中,通过计量泵(8)投加化学药剂对管式膜组件(P4)进行10-15min的浸泡和清洗。一般在30-45天期间,还需对管式膜组件(P4)进行彻底的化学清洗,以恢复管式膜组件(P4)的原始通量。  During the backwashing process, the air compressor (P6) is turned on, the oil-free compressed air passes through the pneumatic valve (V4), and the product water outlet (4) enters the cavity of the tubular membrane module (P4) from the opposite direction of the membrane filtration, and the opposite direction The punching force is 0.5MPa, and the continuous pulse backwashing is 2-3 times, each time is 2-3 seconds. After gas recoil, turn on the backwash pump (P7) to backwash with the product water in the clear water tank for 1-2min. The process is: the backwash pump (P7) pumps water from the clear water tank and enters the tubular membrane from the product water outlet (4) The cavity of the component (P4) flows out from the water inlet (1), and returns to the biochemical reactor (P1) through the backwash sewage pipe. After 15-20 cycles of normal air backwashing and water backwashing, enhanced backwashing is required, that is, in water backwashing, the tubular membrane module (P4) is subjected to 10- 15min of soaking and washing. Generally, during 30-45 days, the tubular membrane module (P4) needs to be thoroughly chemically cleaned to restore the original flux of the tubular membrane module (P4). the

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.
CN2011201030580U 2011-04-11 2011-04-11 Purifying device of air lifted type external tubular membrane bioreactor Expired - Fee Related CN202089817U (en)

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

Publications (1)

Publication Number Publication Date
CN202089817U true CN202089817U (en) 2011-12-28

Family

ID=45364898

Family Applications (1)

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

Country Status (1)

Country Link
CN (1) CN202089817U (en)

Cited By (6)

* Cited by examiner, † Cited by third party
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
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

Cited By (9)

* Cited by examiner, † Cited by third party
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
USD779631S1 (en) 2015-08-10 2017-02-21 Koch Membrane Systems, Inc. Gasification device
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

Similar Documents

Publication Publication Date Title
CN102730816A (en) Airlift external tubular membrane bioreactor purifier
CN202089817U (en) Purifying device of air lifted type external tubular membrane bioreactor
CN102580545B (en) Combined ultra-filtration device with membrane pollution control and ultrasonic cleaning functions
CN104108830B (en) Reclaimed water advanced treatment and reuse system
CN100567172C (en) Inclined plate separate film biological reactor
CN204162570U (en) A kind of light electrolysis/aerobic/anaerobic/membrane filtration treatment unit
CN101323484A (en) Nested Multidimensional Membrane Module Dynamic Membrane Bioreactor
CN101028949A (en) Cast-sand membrane biological reactor
CN210150897U (en) Reclaimed water recycling device
CN115818862A (en) A cold water mariculture tail water treatment system
CN104261603B (en) The integrated drinking water advanced treatment device of a kind of electric coagulation-electro-flotation/immersion ultrafiltration
CN103214147A (en) Oil-refining wastewater treatment method and device
CN203890088U (en) Efficient dissolved air flotation system
CN114262052A (en) A kind of anaerobic membrane bioreactor and organic sewage treatment method
CN202671258U (en) Gravity membrane filtering device
CN105439277A (en) Tail water deep treatment system based on micro-bubble ozone heterogeneous catalysis and oxidization
CN201626870U (en) A Submerged Ceramic Membrane Bioreactor
CN205328688U (en) Tail water degree of depth processing system based on heterogeneous catalytic oxidation of microbubble ozone
CN205061690U (en) Anaerobism - good oxygen integrative sewage treatment device
CN206467030U (en) A kind of self-cleaning flexibility MBR flat sheet membrane devices
CN102616991B (en) Method and equipment for sewage treatment by means of biochemical pressurized dissolved air flotation
CN217323758U (en) High-efficient sewage treatment plant of aerodynamic force
CN201200865Y (en) High-recovery rate hyperfiltration device
CN212833252U (en) Self-oxygen-supply circulating industrial aquaculture water purification system
CN204509013U (en) A kind of waste water from dyestuff deep purifying reclaiming system

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