JP3633704B2 - Membrane separation biological treatment method of wastewater - Google Patents

Membrane separation biological treatment method of wastewater Download PDF

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Publication number
JP3633704B2
JP3633704B2 JP02544796A JP2544796A JP3633704B2 JP 3633704 B2 JP3633704 B2 JP 3633704B2 JP 02544796 A JP02544796 A JP 02544796A JP 2544796 A JP2544796 A JP 2544796A JP 3633704 B2 JP3633704 B2 JP 3633704B2
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Prior art keywords
membrane
hollow fiber
biological treatment
treatment method
arranged
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Expired - Fee Related
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JP02544796A
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JPH09215980A (en
Inventor
裕 大貫
正 松田
Original Assignee
セイリュウ株式会社
三菱レイヨン・エンジニアリング株式会社
三菱レイヨン株式会社
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Priority to JP02544796A priority Critical patent/JP3633704B2/en
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D63/00Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/02Hollow fibre modules
    • B01D63/04Hollow fibre modules comprising multiple hollow fibre assemblies
    • B01D63/043Hollow fibre modules comprising multiple hollow fibre assemblies with separate tube sheets
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D63/00Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/02Hollow fibre modules
    • B01D63/026Wafer type modules or flat-surface type modules
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D63/00Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/08Flat membrane modules
    • B01D63/082Flat membrane modules comprising a stack of flat membranes, e.g. plate-and-frame devices
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00Biological treatment of water, waste water, or sewage
    • C02F3/02Aerobic processes
    • C02F3/12Activated sludge processes
    • C02F3/1236Particular type of activated sludge installations
    • C02F3/1268Membrane bioreactor systems
    • C02F3/1273Submerged membrane bioreactors
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2313/00Details relating to membrane modules or apparatus
    • B01D2313/08Flow guidance means within the module or the apparatus
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2315/00Details relating to the membrane module operation
    • B01D2315/06Submerged-type; Immersion type
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2319/00Membrane assemblies within one housing
    • B01D2319/02Elements in series
    • B01D2319/022Reject series
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2321/00Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/18Use of gases
    • 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
    • Y02W10/15Aerobic processes

Description

[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a biological treatment method for organic wastewater by a membrane separation activated sludge method.
[0002]
[Prior art]
Conventionally, biological treatment has been used for the treatment of municipal wastewater and organic wastewater, and precipitation separation has been used for final solid-liquid separation. However, in the precipitation separation, SS spilled out easily when the load fluctuated.
[0003]
When membrane separation is used for solid-liquid separation, a sedimentation tank is not required, SS can be completely prevented from flowing out, and the activated sludge concentration in the aeration tank can be increased, resulting in less generation of excess sludge. In recent years, the membrane separation activated sludge method has attracted attention because it can be made compact.
[0004]
A microfiltration membrane and an ultrafiltration membrane are mainly used for solid-liquid separation in organic wastewater treatment by biological treatment. These separation membranes are used in the form of flat membranes, tubular membranes or hollow fiber membranes. In particular, recently, many methods for solid-liquid separation of activated sludge by suction filtration using a hollow fiber membrane module have been proposed.
[0005]
On the other hand, when activated sludge containing organic gel-like substances is solid-liquid separated with these separation membranes, it is due to clogging of the membrane, adhesion of dirt on the surface of the membrane, retention of dirt between the membranes, etc. Performance degradation is likely to occur, and it is necessary to wash the membrane surface by sending air to vibrate the membrane, and to repeat the membrane surface cleaning.Furthermore, the liquid to be treated is due to the air lift effect of the air sent from the air diffuser It has been proposed to receive more efficient microbial treatment by receiving agitation (JP-A-61-129094, JP-A-3-98697, etc.).
[0006]
However, even with these methods, when the aerobic microorganism concentration is increased, the oxygen demand increases, which tends to be rate-limiting and the processing capacity tends to reach its peak. Moreover, when the sludge concentration is increased, the viscosity of the liquid increases, which causes a decrease in dissolution efficiency. As countermeasures, it is possible to increase the number of diffusers or to use mechanical agitation in combination, but there is a drawback that the equipment and running costs are increased.
[0007]
For example, recently, a hollow fiber membrane is attached to a frame member for the purpose of preventing obstruction of a substance to be filtered between the hollow fiber membranes while securing a membrane area of the hollow fiber membrane. The hollow fiber membranes are arranged in a row, and both ends are supported and fixed by upper and lower molds, and a hollow fiber membrane filtration member having a filtrate passage communicating with a large number of hollow fiber membranes is continuously provided at a predetermined interval. A hollow fiber membrane filter (Japanese Utility Model Laid-Open No. 5-63632 and Japanese Patent Laid-Open No. 5-220357) in which the filtrate passages are connected has been proposed.
[0008]
Furthermore, the hollow fiber membrane is a hollow fiber membrane module in which a hollow fiber membrane is developed and arranged in a sheet shape, and an end of the hollow fiber membrane is fixed while being kept open by a fixing member in the housing, There has been proposed a hollow fiber membrane module (Japanese Patent Laid-Open No. 5-220356) having a substantially rectangular shape with a cross section perpendicular to the hollow fiber membrane.
[0009]
When a flat hollow fiber membrane module in which such hollow fiber membranes are arranged and expanded in a sheet shape is used, a large number of hollow fiber membranes can be evenly arranged at intervals. Since it becomes extremely easy to evenly clean the surface of the thread membrane, it is possible to suppress a decrease in filtration efficiency.
[0010]
However, even with these hollow fiber membrane modules, the suction filtration of highly polluted water tends to increase the differential pressure in a relatively short period of time, so the number of backwashes and pauses increases, so the efficiency of the device is high. It was difficult to perform good filtration.
[0011]
[Problems to be solved by the invention]
An object of the present invention is to provide a membrane separation biological treatment method that increases the amount of dissolved oxygen and suppresses the increase in the differential pressure of suction filtration to increase the efficiency of the apparatus in the treatment of wastewater by the membrane separation activated sludge method. is there.
[0012]
[Means for Solving the Problems]
That is, the present invention relates to a wastewater membrane separation biological treatment method comprising a step of disposing a membrane module in an aeration tank and suction-filtering wastewater through the membrane to obtain membrane permeated water. Membrane modules arranged so as to be approximately parallel are stacked and arranged in multiple stages, and the fiber axes of the hollow fiber membranes in adjacent membrane modules are arranged in a positional relationship of about 90 ° twist angle. And a membrane separation biological treatment method.
[0013]
Another aspect of the present invention relates to a wastewater membrane separation biological treatment method comprising a step of disposing a membrane module in an aeration tank and suction-filtering wastewater through the membrane to obtain membrane permeate. The membrane modules arranged so as to be substantially parallel to each other are stacked in multiple stages, and the plane of the flat membrane in the adjacent membrane modules is perpendicular to the horizontal plane and intersects at about 90 ° The membrane separation biological treatment method is characterized in that the membrane module is housed and arranged inside a mantle having a lower portion that is wider than the upper portion .
[0014]
DETAILED DESCRIPTION OF THE INVENTION
Hereinafter, the membrane separation biological treatment method of wastewater of the present invention will be described in more detail with reference to the drawings, taking the case of using a hollow fiber membrane module as an example.
[0015]
In the method of the present invention, the hollow fiber membrane module is disposed in the aeration tank. FIG. 1 is a diagram showing a mutual positional relationship between a plurality of hollow fiber membrane modules 1 arranged in an aeration tank. In this example, one hollow fiber membrane module is configured by arranging seven hollow fiber membrane elements such that the sheet-like surfaces formed by the hollow fiber membranes 2 are substantially parallel. And such hollow fiber membrane modules are installed so as to be stacked in three stages. Therefore, a total of 21 hollow fiber membrane elements are used in this example. Here, the fiber axis of the hollow fiber membrane included in the middle hollow fiber membrane module is the position of the twist angle of about 90 ° from the fiber axis of the hollow fiber membrane included in each of the upper and lower hollow fiber membrane modules. They are arranged so as to be in a relationship (a state in which they are rotated about 90 ° and moved up and down).
[0016]
The hollow fiber membrane module used in the method of the present invention is not particularly limited in terms of its form as long as a large number of hollow fiber membranes included in the module are arranged and arranged substantially in parallel. Can be used without Therefore, as shown in FIG. 1, one hollow fiber membrane module may be configured as an assembly of a plurality of hollow fiber membrane elements. As such a hollow fiber membrane element, a hollow fiber membrane that is arranged in a sheet shape and disposed so that the fiber axes are substantially parallel to each other, and an end portion of the hollow fiber membrane is fixed in an open state. A fixing member and a structural member that supports and stores the fixing member, and is preferably of the type shown in FIG. 2, in which the shape of the cross-section perpendicular to the hollow fiber membrane of the fixing member is a substantially rectangular shape. It is illustrated as a thing.
[0017]
The hollow fiber membrane element 3 shown in FIG. 2 includes a structural material 4, a fixing member 5, and a hollow fiber membrane 2. The structural member 4 has an elongated rectangular opening and has a filtrate chamber therein. In this hollow fiber membrane element, the hollow fiber membranes are arranged in a straight line, and structural materials are arranged at both ends thereof, but the hollow fiber membranes are arranged in a U-shape and the structural materials are arranged only at one end. The types of hollow fiber membrane elements that are made can also be used.
[0018]
A fixing member 5 is disposed at the opening of the structural material 4 and a large number of hollow fiber membranes 2 are arranged almost in parallel and spread in a sheet shape, and each end is converged and fixed while maintaining the open state. Thus, the hollow fiber membrane functions as a filtration membrane.
[0019]
Various hollow fiber membranes used in the method of the present invention can be used. For example, those made of various materials such as cellulose, polyolefin, polyvinyl alcohol, PMMA, and polysulfone can be used. A material having high strength such as polypropylene is preferred. In addition, as long as it can be used as a filtration membrane, there is no particular limitation on the pore diameter, porosity, film thickness, outer diameter, etc., but the membrane area per removal object and volume and the strength of the hollow fiber membrane In view of the above, preferable examples include a pore diameter of 0.01 to 1 μm, a porosity of 20 to 90%, a film thickness of 5 to 300 μm, and an outer diameter of 20 to 2000 μm.
[0020]
As a surface characteristic of the hollow fiber membrane, a so-called permanent hydrophilic membrane having a hydrophilic group on the surface is desirable. If the surface is a hydrophobic hollow fiber membrane, hydrophobic interaction occurs between the organic matter in the water to be treated and the surface of the hollow fiber membrane, causing organic matter adsorption to the membrane surface, which results in blockage of the membrane surface and filtration. Life is shortened. Moreover, it is generally difficult to recover the filtration performance by cleaning the membrane surface due to clogging due to adsorption. By using a permanent hydrophilized membrane, the hydrophobic interaction between the organic matter and the hollow fiber membrane surface can be reduced, and adsorption of the organic matter can be suppressed. Furthermore, in the hydrophobic membrane, the membrane surface may become dry due to bubbles during scrubbing, which may increase the hydrophobicity and reduce the flux. Does not occur.
[0021]
The hollow fiber membrane module used in the method of the present invention is arranged in such a manner that a plurality of the above-described hollow fiber membrane elements are arranged in parallel at equal intervals, and the hollow fiber membranes arranged in a sheet form are superposed in parallel. It is preferable. In such a hollow fiber membrane module, since many hollow fiber membranes are arrange | positioned equally spaced apart, since the membrane surface can be wash | cleaned equally, the fall of filtration efficiency can be suppressed. Moreover, it is preferable that the sheet | seat surface which a hollow fiber membrane forms is a perpendicular | vertical direction with respect to a horizontal surface.
[0022]
In the membrane separation biological treatment method of the present invention, such hollow fiber membrane modules are stacked and arranged in multiple stages in an aeration tank, and the fiber axes of the hollow fiber membranes included in the hollow fiber membrane modules installed in adjacent stages Are arranged so as to have a positional relationship of about 90 ° with respect to each other. Here, the twist angle of about 90 ° does not mean a state where the twist is strictly 90 °, but a state where the twist angle is in a substantially right angle state, and more precisely, a range of 70 to 110 °. The state of the twist angle. By arranging the hollow fiber membrane module in such a positional relationship, the rising air bubbles are divided and refined by the surface formed by the hollow fiber membrane, and a turbulent flow is generated by a change in the flow direction. It is presumed that the amount of dissolved oxygen increases and the increase in the differential pressure of suction filtration is suppressed. As long as the hollow fiber membrane module has two or more stages, the hollow fiber membrane module may be stacked and arranged, but about 2 to 5 stages are preferable.
[0023]
In the method of the present invention, a plurality of hollow fiber membrane modules in which the fiber axes of the hollow fiber membranes between the modules satisfy the positional relationship described above are disposed so as to be housed in the outer sheath 6 as shown in FIG. This is a preferred embodiment. In particular, it is preferable that the outer lower portion is formed as an inverted hopper-shaped (skirt-shaped) air collecting portion that spreads from the upper portion, and is configured to collect air bubbles from the air diffuser 8 disposed below. In this case, it can be used not only as a means for dissolving bubbles in wastewater but also as a scrubbing means for shaking the deposits on the hollow fiber membrane, and ascending flow in the mantle with the bubbles as a driving force. It is also possible to exert a cleaning action that sweeps away deposits that are generated and peeled off the surface of the hollow fiber membrane.
[0024]
In the membrane separation biological treatment method of the present invention, the wastewater in the aeration tank is subjected to suction filtration through the separation membrane. Suction filtration can keep the permeation flux high for a long time under filtration conditions with a small differential pressure even if it is continuously performed, but of course it is also possible to adopt a so-called intermittent suction operation method in which suction is temporarily stopped it can. Moreover, the hollow fiber membrane module can be back-washed using membrane permeated water as required.
[0025]
In the above, an example of using a membrane module using a hollow fiber membrane has been described. However, in the present invention, a membrane module including a flat membrane is accommodated and disposed inside a mantle having a shape in which the lower part is wider than the upper part. The case can be similarly implemented. FIG. 4 is a view similar to FIG. 1 showing the mutual positional relationship of a plurality of flat membrane modules arranged in the aeration tank, except for the flat membrane.
[0026]
In the case of flat membranes, the action of the membrane surface to divide and refine bubbles is equal to or greater than that of membrane modules using hollow fiber membranes, so it is possible to greatly increase the amount of dissolved oxygen in wastewater. is there.
[0027]
【Example】
Hereinafter, the present invention will be described specifically by way of examples.
[0028]
Examples and Comparative Examples An example in which the method of the present invention is applied to wastewater in a food processing factory will be described with reference to the flow sheet of FIG.
[0029]
As the hollow fiber membrane module, 28 hollow fiber membrane elements of the form as shown in FIG. 2 are arranged in parallel, and modules having a total membrane area of 112 m 2 are stacked in three stages, and below that Aerated with a diffuser. In the examples, the fiber axes of the hollow fiber membranes of the modules in the respective stages are alternately positioned at a twist angle of 90 ° as shown in FIG. 1, whereas in the comparative example, the fibers of the hollow fiber membranes All the shafts were arranged in the same direction.
[0030]
Treatment facility, adjusting tank 11 is 40 m 3, the aeration tank 12 is 40 m 3, the process water is 30 m 3 / day, the water quality of raw water BOD3000~4000mg / L, CODl500~2000mg / L, at SS200~400mg / L there were.
[0031]
The operation was performed under the following conditions. MLSS was 10,000-15000 mg / L, and it concentrated to 30000 mg / L using the hollow fiber membrane in the sludge concentration storage tank. Sludge withdrawal was 10 kg / day per solid and 50 kg / day per 80% wet cake. In addition, air was aerated from the air diffuser at 200 Nm 3 / hour.
[0032]
As a result, DO of the aeration tank and BOD of the membrane permeated water quality were as shown in Table 1.
[0033]
[Table 1]
As in the comparative example, when the fiber axes were aligned in the same direction, almost no DO was detected. On the other hand, the direction of the fiber axes was changed alternately in three steps as in the method of the present invention. In the stacked ones, an increase in DO was observed due to aeration by the same blower, and the treated water BOD was also low and stable. Moreover, in the method of the present invention, the increase in the differential pressure of suction filtration was smaller than that in the comparative example.
[0034]
【The invention's effect】
According to the present invention, the supply amount of oxygen can be significantly increased without changing the energy cost. In addition, the membrane surface has improved cleaning properties, has a great effect of suppressing clogging, has an advantage that the differential pressure increase in suction filtration is suppressed, and the apparatus efficiency is high.
[Brief description of the drawings]
FIG. 1 is a schematic diagram showing the positional relationship of hollow fiber membrane modules in the method of the present invention.
FIG. 2 is a perspective view showing an example of a hollow fiber membrane element used in the method of the present invention.
FIG. 3 is a schematic view showing a state in which the hollow fiber membrane module is disposed in the mantle in the method of the present invention.
FIG. 4 is a schematic diagram showing a positional relationship of flat membranes of a membrane module in the method of the present invention.
FIG. 5 is a flow sheet showing an example to which the method of the present invention is applied.
[Explanation of symbols]
DESCRIPTION OF SYMBOLS 1 Hollow fiber membrane module 2 Hollow fiber membrane 3 Hollow fiber membrane element 4 Structural material 5 Fixing member 6 Outer jacket 7 Air collecting part 8 Air diffuser 9 Flat membrane 11 Adjustment tank 12 Aeration tank 13 Sludge concentration storage tank 14 Membrane module 15 Aeration pipe 16 Adjustment tank pump 17 Sludge transfer pump 18 Treated water suction pump 19 Sludge concentration suction pump

Claims (4)

  1. In a membrane separation biological treatment method having a step of arranging a membrane module in an aeration tank and sucking and filtering wastewater through the membrane to obtain membrane permeate, so that the fiber axes of the hollow fiber membranes are substantially parallel to each other The arranged membrane modules are stacked in multiple stages, and the fiber axes of the hollow fiber membranes in the adjacent membrane modules are arranged so as to have a twist angle of about 90 °. Membrane separation biological treatment method.
  2. The membrane separation biological treatment method according to claim 1, wherein an aeration device is disposed below the membrane module.
  3. The membrane separation biological treatment method according to claim 1 or 2, wherein the membrane module is housed and disposed in a mantle having a shape in which the lower part extends from the upper part.
  4. In a membrane separation biological treatment method for wastewater having a process of arranging a membrane module in an aeration tank and obtaining a membrane permeated water by suction filtration of the wastewater through the membrane, a plurality of flat membranes are arranged substantially in parallel. The membrane modules are stacked and arranged in multiple stages, and the flat membranes in the adjacent membrane modules are arranged so that the planes of the membranes are perpendicular to the horizontal plane and intersect at about 90 °. A membrane-separated biological treatment method, wherein a membrane module is housed and disposed in a mantle having a shape in which the lower part is wider than the upper part.
JP02544796A 1996-02-13 1996-02-13 Membrane separation biological treatment method of wastewater Expired - Fee Related JP3633704B2 (en)

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Application Number Priority Date Filing Date Title
JP02544796A JP3633704B2 (en) 1996-02-13 1996-02-13 Membrane separation biological treatment method of wastewater

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JP3633704B2 true JP3633704B2 (en) 2005-03-30

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Cited By (1)

* Cited by examiner, † Cited by third party
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EP0931582B1 (en) 1996-08-22 2006-10-11 Mitsubishi Rayon Co., Ltd. Process of manufacturing a hollow fiber membrane module, process of manufacturing a hollow fiber membrane module unit, and septic tank provided with a module unit thus obtained
US6280626B1 (en) 1998-08-12 2001-08-28 Mitsubishi Rayon Co., Ltd. Membrane separator assembly and method of cleaning the assembly utilizing gas diffuser underneath the assembly
DE69942845D1 (en) * 1998-08-12 2010-11-18 Mitsubishi Rayon Co Membrane separator
AT286777T (en) * 1999-11-18 2005-01-15 Zenon Environmental Inc Overflow procedure and pumped membrane filtration system for its implementation
US7037426B2 (en) 2000-05-04 2006-05-02 Zenon Environmental Inc. Immersed membrane apparatus
CA2290053C (en) 1999-11-18 2009-10-20 Zenon Environmental Inc. Immersed membrane module and process
JP2003093828A (en) * 2001-09-27 2003-04-02 Mitsui Eng & Shipbuild Co Ltd Distillation apparatus equipped with separation membrane module and distillation column
JP2007130579A (en) * 2005-11-10 2007-05-31 Mitsubishi Rayon Eng Co Ltd Filtration membrane cleaning apparatus and method for membrane filtration unit in activated sludge treatment
JP5438879B2 (en) * 2005-12-01 2014-03-12 三菱レイヨン株式会社 Membrane filtration unit
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JP4614188B2 (en) * 2007-05-15 2011-01-19 株式会社日立プラントテクノロジー Immersion flat membrane filtration device
JP5425394B2 (en) * 2007-12-27 2014-02-26 月島機械株式会社 Filtration module, filtration module laminate, and filtration device
CN102531153B (en) * 2011-12-21 2014-06-25 大连大学 Integrated bubbleless aeration membrane bioreactor
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CN102596374A (en) * 2009-10-26 2012-07-18 株式会社明电舍 Membrane module, membrane unit, and membrane separation device
CN102596374B (en) * 2009-10-26 2014-09-10 株式会社明电舍 Membrane module, membrane unit, and membrane separation device

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