WO2012117768A1 - 膜分離装置 - Google Patents
膜分離装置 Download PDFInfo
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- WO2012117768A1 WO2012117768A1 PCT/JP2012/051371 JP2012051371W WO2012117768A1 WO 2012117768 A1 WO2012117768 A1 WO 2012117768A1 JP 2012051371 W JP2012051371 W JP 2012051371W WO 2012117768 A1 WO2012117768 A1 WO 2012117768A1
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- membrane
- air
- diffuser
- bubble group
- holes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/08—Prevention of membrane fouling or of concentration polarisation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/18—Apparatus therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
- B01D63/08—Flat membrane modules
- B01D63/082—Flat membrane modules comprising a stack of flat membranes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
- B01F23/231—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids by bubbling
- B01F23/23105—Arrangement or manipulation of the gas bubbling devices
- B01F23/2312—Diffusers
- B01F23/23121—Diffusers having injection means, e.g. nozzles with circumferential outlet
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
- B01F23/231—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids by bubbling
- B01F23/23105—Arrangement or manipulation of the gas bubbling devices
- B01F23/2312—Diffusers
- B01F23/23126—Diffusers characterised by the shape of the diffuser element
- B01F23/231265—Diffusers characterised by the shape of the diffuser element being tubes, tubular elements, cylindrical elements or set of tubes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
- C02F3/1273—Submerged membrane bioreactors
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/20—Activated sludge processes using diffusers
- C02F3/208—Membrane aeration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/26—Specific gas distributors or gas intakes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2315/00—Details relating to the membrane module operation
- B01D2315/06—Submerged-type; Immersion type
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2317/00—Membrane module arrangements within a plant or an apparatus
- B01D2317/04—Elements in parallel
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/18—Use of gases
- B01D2321/185—Aeration
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
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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
Definitions
- the present invention relates to a membrane separation device, and more particularly to a membrane separation device used in the field of water treatment.
- Membrane separation technology has been used for seawater desalination, water purification, gas separation, blood purification, etc., but recently, from the viewpoint of environmental conservation, research to apply membrane separation technology to wastewater treatment has been promoted. It has been.
- Non-Patent Document 1 As a method for solving this problem, various methods for solid-liquid separation by immersing a membrane module provided with a separation membrane such as a microfiltration membrane and an ultrafiltration membrane in water to be treated have been studied in recent years. When filtration of water to be treated is performed using a separation membrane, high quality treated water can be obtained (for example, Non-Patent Document 1).
- a plurality of diffuser tubes of the membrane separation device described in Patent Document 1 are formed such that slit-like diffuser holes are arranged substantially perpendicular to the axis of the diffuser tube in the lower peripheral wall portion of the cylindrical diffuser tube. .
- a diffuser (aeration tube) is provided for each separation membrane in order to cause bubbles for scrubbing to act uniformly and sufficiently on the entire separation membrane. Further, in order to improve the dissolution efficiency of the scrubbing air for the water to be treated, a grid-like or mesh-like dispersion member is arranged above the air diffuser to generate bubbles having a smaller diameter than the bubbles provided from the device. ing.
- the membrane separation device of Patent Document 1 is effective by maintaining a constant amount of air diffused from each air diffuser of the air diffuser.
- the subtle difference in height of each air diffuser is due to the change in the fixed state of the air diffuser tube due to the installation of the membrane separator and the water pressure during the inflow (because the dynamic water pressure works instead of the hydrostatic pressure). Even if devised, the effect is limited.
- the air diffuser of the air diffuser has a slit shape, the gas supply from the air diffuser does not become insufficient due to the blockage of the air diffuser. However, the air diffused state becomes uneven in a plan view, and the cleaning surface of the separation membrane tends to be uneven.
- the dispersion means according to the membrane separation devices of Patent Documents 2 to 4 can be any one selected from a wire mesh, a perforated plate, a pipe, a wire, a lattice, etc. in order to achieve both the effect of dispersing bubbles and the suppression of clogging simultaneously.
- a horizontal arrangement is applied.
- the aperture ratio of the dispersing means is set to 20 to 70%, and the mesh width is set to about 2 to 10 mm.
- the coarse bubbles are subdivided by the insert having openings, the dissolution efficiency is improved by the dispersion effect of the bubbles, and the bubbles are uniformly distributed to the membrane portion by the dispersion effect of the bubbles at that time.
- the purpose is to introduce. This is in order to improve a significant decrease in oxygen dissolution efficiency due to the coarsening of bubbles and partial film contamination due to uneven introduction of bubbles between the films.
- the specifications of the bubble diameter required for the diffuser that combines oxygen supply and membrane cleaning require fine bubbles for oxygen supply, while coarse bubbles are required for membrane cleaning.
- the aeration method must be selected based on conflicting requirements.
- the membrane separation apparatus of Patent Document 4 since the bubble group provided from the air diffuser is subdivided by the mesh-like or lattice-like dispersion means, the membrane surface of the separation membrane is likely to be unevenly washed, and the membrane cleaning is performed. The function is inferior. Furthermore, a plurality of diffuser tubes must be installed or added according to the width of the lower surface of the dispersing means.
- the installation or addition of the plurality of air diffusion pipes increases the number of air diffusion points, but the state of the air diffusion becomes uneven when viewed in plan, and cleaning of the membrane surface of the separation membrane is likely to occur. This leads to a decrease in the separation efficiency of the entire membrane, and further to a decrease in the reliability of the membrane separation process.
- the membrane separation apparatus of the present invention diffuses a membrane unit formed by stacking a plurality of membrane modules in the depth direction of a water tank, and air for membrane cleaning disposed below the membrane unit. And a bubble group dividing member that is disposed between the membrane unit and the diffusion member and divides the air bubble group provided from the diffusion member into a plurality of bubble groups.
- the bubble group dividing member is a three-dimensional obstacle member having a diameter larger than the diameter of the air diffuser member and arranged parallel to the axis of the air diffuser member, the air bubble group dividing member is provided from the air diffuser hole of the air diffuser member.
- the bubble group is divided equally with the axis of this member as the center line by the collision with the bubble group dividing member. Thereby, the divided bubble group can be uniformly supplied to the lower end of the membrane unit without adding a diffuser member or a diffuser point.
- the resistance to the bubble group diffused from the diffuser holes of the diffuser member is relaxed, so the gas-liquid mixing flow rate is reduced.
- the bubble group can be decomposed into a plurality of bubble groups without causing them to occur.
- the bubble group colliding with the member is divided into a plurality of bubble groups while maintaining a turbulent state on the curved surface of the member. Divided. Furthermore, if the upper side of the longitudinal section is formed to form a triangle, the suspended substance can be efficiently guided below the bubble group dividing member.
- the bubble group dividing member is formed so that the longitudinal section is circular, or the upper side of the longitudinal section is bell-shaped while the lower half is formed in a semicircular shape, the curved surface of the lower surface of the member The gas-liquid mixed flow rising along the line swirls above the member and the swirl flow is maintained.
- Sectional drawing which showed schematic structure of the membrane separator which concerns on Embodiment 1 of this invention.
- FIG. A) The bottom view of the diffuser member which concerns on Embodiment 2, (b) The longitudinal cross-sectional view of the said diffuser member, (c) The bottom view of the diffuser member which concerns on Embodiment 1.
- FIG. A) The bottom view of the diffuser which concerns on Embodiment 3, (b) The longitudinal cross-sectional view of the said diffuser.
- the membrane separation apparatus 1 has a bubble cleaning air bubble group 401 diffused from the diffusion member 4 to the membrane module 3 in the MBR bioreactor 10.
- the cleaning effect of the membrane module is made uniform. That is, the division of the bubble group according to the present embodiment is not intended to improve the dissolution efficiency of oxygen by refining the bubble in order to increase the activation of the activated sludge, but the bubble provided from the diffuser member
- An object is to divide a group by colliding with a bubble group dividing member and distribute the group in multiple directions.
- the membrane separation apparatus 1 includes a membrane unit 3 configured by stacking a plurality of membrane modules 2 in the depth direction of the biological reaction tank 10, and air bubbles for aeration and membrane cleaning for the membrane unit 3. It consists of a diffuser member 4 that diffuses and a bubble group dividing member 5 that divides the bubble group into a plurality of bubble groups.
- the membrane separation apparatus 1 is installed so as to be immersed in the liquid phase 11 in the MBR biological reaction tank 10.
- the membrane module 2 includes a plurality of flat separation membranes 21 arranged in parallel, a pair of support portions 22 that support both ends of the separation membrane 21, and the pair of support portions. 22 and a pair of guides 23 for closing the gaps near both ends.
- the support 22 and the guide 23 constitute a housing having openings on the top and bottom.
- the separation membrane 21 has a flat shape, but the separation membrane according to the invention is not limited to this embodiment.
- an organic hollow fiber membrane, an organic flat membrane, an inorganic flat membrane, an inorganic single tube membrane, etc. which are well-known separation membranes applied to MBR, may be applied.
- the material of the separation membrane 21 include cellulose, polyolefin, polysulfone, PVDF (polyvinylidene fluoride), PTFE (polytetrafluoroethylene), ceramics, and the like.
- a plurality of separation membranes 21 arranged in the membrane module 2 are installed so that the water collection channels 211 in the separation membrane 21 are arranged in the vertical direction, and the water collection unit communicating with the water collection channel 211 is disposed on the separation membrane 21. You may provide in an edge part (upper one or both edge parts).
- a water collecting part (not shown) communicating with the water collecting path 211 inside the separation membrane 21 is formed inside the support part 22.
- the water collecting part communicates with a filtration suction port 24 formed in the support part 22.
- the filtration suction port 24 is connected to a pipe of a pump for sucking filtrate (not shown).
- the guide 23 is attached to the support 22 so that the upper opening end cross-sectional area of the membrane module 2 is smaller than the lower opening end cross-sectional area, so that the filtration efficiency by the separation membrane 21 is improved. That is, when the membrane modules 2 are stacked, a gap is formed between the upper opening end of the membrane module 2 and the lower opening end of another membrane module (not shown) stacked on the membrane module 2.
- a gap is formed between the upper opening end of the membrane module 2 and the lower opening end of another membrane module (not shown) stacked on the membrane module 2.
- the number of the membrane modules 2 to be stacked is selected from the weight and the outer shape considering the water depth and maintainability of the biological reaction tank 10.
- the number of membrane modules 2 is selected so that the height of the membrane unit 3 is about 2 m to 3 m.
- the flow of water to be treated inside the membrane unit 3 is a flow from the lower opening of the membrane unit 3 toward the upper opening. Since the liquid phase in the membrane unit 3 is filtered by the separation membrane 21, the concentration of the activated sludge in the liquid phase increases as the upper part of the membrane unit 3 is reached. In the membrane unit 3, since the water to be treated is sucked into the membrane unit 3 from the gaps 25 of the membrane modules 2 stacked as shown in FIG.
- the activated sludge concentration inside the membrane unit 3 is greatly increased. Can be suppressed. As a result, the load on filtration is reduced, leading to relaxation of membrane clogging and reduction of energy consumption.
- sucks to-be-processed water into the inside of the membrane unit 3 arises by the upward flow of the bubble groups 401 and 402, it is not necessary to provide the motive power source for attracting
- the aeration member 4 is a member for supplying air for membrane cleaning to the membrane unit 3.
- the aeration diffuser 12 is a member for supplying oxygen necessary for biological treatment with activated sludge.
- the air and oxygen are supplied from a blower or a compressor (not shown) outside the biological reaction tank 10. What is necessary is just to apply the thing of a known specification to the aeration member 4.
- the 2A includes a diffuser tube 41 in which a plurality of diffuser holes 42 are formed.
- the air diffuser 41 is disposed horizontally below the membrane unit 3 as shown in FIG.
- the plurality of air diffusion holes 42 are formed on the lower surface of the air diffusion pipe 41 so as to be arranged in parallel to the axis of the pipe 41.
- a plurality of air diffusion holes 42 are formed on the lower surface of the air diffusion tube 41 with a diameter of 5 to 10 mm and a pitch of 100 to 200 mm so that the air diffusion speed is 10 m / second or more.
- the total aeration volume Dm 3 / min is selected from numerical values such as 3Q, 6Q, and 9Q as 3, 6, and 9 multiples of the design throughput Qm 3 / day of the biological reaction tank 10.
- a plurality of membrane separation apparatuses 1 are installed according to the planned processing capacity, but the above setting method performs calculation based on the unit membrane unit 3 standard.
- the total area of the diffuser holes 42 per unit membrane unit 3 is calculated.
- the total amount of air diffused D is divided by the number of unit membrane units 3 to calculate the amount of air diffused per unit membrane unit 3, and further, the amount of air diffused from the air diffuser holes 42 is calculated based on the total area.
- the flow rate Em / second is calculated.
- a specific example of setting the diameter and the number of the air diffusion holes 42 will be described.
- An example of setting the diameter and number of diffuser holes when the design throughput Q is 0.6 m 3 / m 2 ⁇ day (19.8 m 3 / day) and the total diffused air volume Dm 3 / min is 6Q will be described.
- the diffuser flow velocity E from the diffuser holes is approximately 12 m / second according to the above calculation. Is calculated. Since the calculated value of E is larger than 10 m / sec, the diffused hole diameter Bmm and the number of diffused holes C of the membrane unit according to the specific example are set to appropriate specifications.
- the bubble group dividing member 5 is not like a mesh structure, and is formed in a form that does not allow the bubble group to pass through.
- the bubble group dividing member 5 is a three-dimensional obstacle member having a diameter larger than that of the air diffusing member 4.
- the bubble group dividing member 5 is arranged such that its axis is parallel to the axis of the air diffuser 4 between the membrane unit 3 and the air diffuser 4.
- the bubble group dividing member 5 is arranged so that the bubble group 401 ejected from the diffusion hole 42 of the diffusion member 4 is equally divided from side to side with the axis line of the member 5 as a center line by collision with the bubble group dividing member 5. The Thereby, the divided bubble group 402 can be evenly supplied to the lower end of the membrane unit 3.
- the material of the bubble group dividing member 5 is exemplified by resin, metal, ceramics and the like, but is not particularly limited as long as it does not deform due to intense water flow caused by air diffusion or can maintain the function as an obstructing member even when deformed.
- the bubble group dividing member 5 is formed in a three-dimensional shape with at least the lower side of the longitudinal section projecting downward. According to this aspect, the resistance to the bubble group 401 provided from the diffusion hole 42 of the diffusion member 4 can be relaxed, and the bubble group can be divided into a plurality of bubble groups 402 without reducing the gas-liquid mixing flow rate. Yes.
- FIGS. 3 (a) to 3 (e) Specific examples of the bubble group dividing member 5 are illustrated in FIGS. 3 (a) to 3 (e).
- the bubble group dividing member 5 illustrated in FIG. 3A has a semicircular lower side in the longitudinal section.
- the upper side of the longitudinal section is an obtuse triangle, while the lower side is a semicircle.
- the bubble group dividing member 5 illustrated in FIG. 3C has an acute triangle on the upper side of the vertical cross section, and a semicircular shape on the lower side.
- the bubble group dividing member 5 illustrated in FIG. 3D has a circular longitudinal section.
- the bubble group splitting member 5 illustrated in FIG. 3 (e) has a bell-shaped upper side in its longitudinal section, while its lower side has a semicircular shape.
- the bubble group dividing member 5 illustrated in FIGS. 3 (a) to 3 (e) has at least a lower surface formed in a curved surface, so that the bubble group colliding with the lower surface is in a turbulent state on the curved surface. While maintaining, it can be divided into a plurality of bubble groups.
- the upper surface of the bubble group dividing member 5 illustrated in FIGS. 3B to 3E is formed in a convex shape upward, the activated sludge can be efficiently placed below the member 5. It is possible to guide, and accumulation of activated sludge on the member 5 can be avoided.
- 3D and 3E is formed in a curved surface, the air is rising along the curved surface on the lower surface of the member 5.
- the mixed liquid flow is swirled above the member 5 and the swirl flow can be maintained. Thereby, a vigorous gas-liquid mixed flow can be continued above the bubble group dividing member 5, and the division of the bubble group can be promoted. Then, this vigorous gas-liquid mixed flow bypassing the division can be provided between the separation membranes 21 of the membrane module 2, and the membrane surface cleaning effect can be maintained.
- the diffuser member 4 and the bubble group dividing member 5 are accommodated in a cylinder 7 disposed at the lower end of the membrane unit 3 as shown in FIG.
- the relationship between the axial centers of the diffuser member 4 and the bubble group dividing member 5 and the direction of the membrane surface of the separation membrane 21 arranged in the membrane module 2 is not limited to the arrangement illustrated in FIG.
- the angle between the axis of the diffuser member 4 and the bubble group dividing member 5 and the direction of the membrane surface of the separation membrane 21 disposed in the membrane module 2 is 90 degrees instead of 0 degrees as illustrated in FIG.
- the arrangement may be as follows.
- the liquid phase in the biological reaction tank 10 to which the water to be treated is supplied is always aerated by the aeration diffuser 12.
- the activated sludge in the liquid phase biologically decomposes pollutants in the treated water using oxygen provided by this aeration.
- the liquid phase in the biological reaction tank 10 is introduced into the membrane separation apparatus 1 from the lower end opening of the housing 7 and the gap 25 between the membrane modules 2 by the water flow by the aeration, and is subjected to the solid-liquid separation process.
- the bubble group 401 is constantly released from the diffuser member 4.
- the bubble group 401 is divided into a plurality of bubble groups 402 by collision with the bubble group dividing member 5. Since the bubble group dividing member 5 has a circular longitudinal section, the bubble group 401 colliding with the lower surface of the member 5 is divided into a plurality of bubble groups 402 while being in a turbulent state on the outer peripheral surface of the member 5. Is done. Further, since the upper half of the vertical cross section of the bubble group dividing member 5 is a semicircle, the activated sludge staying near the lower end of the membrane unit 3 is guided downward along the peripheral surface of the member 5. Thus, the accumulation of activated sludge on the upper surface of the member 5 is avoided.
- the violent gas-liquid mixed flow bypassing the division is introduced between the individual separation membranes 21 of each membrane module 2 of the membrane unit 3 and used for cleaning the surface of the separation membrane 21.
- Contaminants separated from the surface of the separation membrane 21 by this washing ride on the gas-liquid mixed flow and are discharged from the upper end opening of the uppermost membrane module 2 of the membrane unit 3, or the biological reaction tank 10 Sedimentation near the bottom.
- the activated sludge contained in the separated impurities is again used for biological decomposition of the pollutant in the biological reaction tank 10.
- each separation membrane 21 of each membrane module 2 is in a negative pressure state by a suction pump (not shown), and the solid-liquid separation treated water that has permeated into the water collecting channel inside the separation membrane 21 is It is carried out of the biological reaction tank 10 by the suction pump.
- the membrane unit 3 an upward flow is generated by the aeration diffuser 12 and the diffuser 4, and the liquid phase introduced into the membrane module 2 is subjected to solid-liquid separation treatment by the separation membrane 21.
- the concentration of the activated sludge in the liquid phase that circulates inside increases as it reaches the upper part of the apparatus 1. Therefore, the sludge load on the separation membrane 21 of the upper membrane module 2 in the membrane unit 3 is increased, and there is a possibility that the membrane clogging is accelerated and the energy consumption is increased.
- a gap 25 between the lower end of the water flow guide 23 of the membrane module 2 and the upper end of the water flow guide 23 of another membrane module 2 connected to the lower side of the membrane module 2 is used.
- the liquid phase staying on the outer periphery rides on the upward flow and is introduced into the membrane module 2.
- an increase in the activated sludge concentration inside the membrane unit 3 is suppressed, and adverse effects due to an increase in the sludge load are avoided.
- the flow path of the gas-liquid mixed flow including the bubble group 402 is narrowed by the water flow guide 23 as it approaches the upper end of the membrane module 2, the mixed flow is converged and the speed thereof is increased. The cleaning effect of the film 21 is enhanced.
- the bubble group 401 of the membrane cleaning air provided from the diffuser member 4 to the membrane unit 3 in the biological reaction tank 10 is divided into a plurality of bubble groups 402 by the bubble group dividing member 5. Is done. And since this divided
- the membrane surface cleaning is possible to prevent the membrane surface cleaning from becoming nonuniform and maintain the solid-liquid separation function of the separation membrane of the membrane module 3 without increasing the number of diffuser members or diffuser points.
- the above-described air diffuser 4 is of the air diffuser type, the air bubbles provided from the air diffuser 4 are not affected even if the air diffuser having the air diffuser hole upward, such as the nozzle type, is employed. It can be divided by the bubble group dividing member 5.
- the air diffuser 4 of the second embodiment is formed such that the air diffuser holes 42 are distributed to the lower side of the air diffuser 41 to the left and right. According to this aspect, due to the synergistic effect with the bubble group dividing member 5, it can be expected that the supply of the bubble groups will be more uniform.
- the adjacent air diffusing holes 42 are arranged obliquely with respect to the axis L of the air diffusing pipe 41.
- Adjacent air diffusion holes 42a and 42b have an angle formed by a straight line L1 passing through one air diffusion hole 42a and the axis O of the air diffusion tube 41 and L2 passing through the other air diffusion hole 42b and the axis O less than 180 degrees, preferably Is formed to be 170 degrees or less.
- the adjacent diffuser holes 42a and 42b are a straight line L1 passing through the diffuser hole 42a and the axis O of the diffuser tube 41, and the diffuser hole 42b and the axis O. Are formed so that the angle formed by the straight line L2 passing through the angle is 90 degrees.
- a specific example of setting the diameter and the number of the air holes 42 of the air diffusion member 4 of the present embodiment will be described.
- An example of setting the diameter and number of diffuser holes when the design throughput Q is 0.6 m 3 / m 2 ⁇ day (19.8 m 3 / day) and the total diffused air volume Dm 3 / min is 6Q will be described.
- the diffuser flow velocity E from the diffuser holes is described in the description of the first embodiment. According to the calculation method, it is calculated as about 12 m / sec. Since the calculated value of E is larger than 10 m / sec, the air diffusion hole diameter Bmm and the number C of air diffusion holes of the membrane unit according to the specific example are appropriate specifications.
- the air bubbles 42 can be ejected evenly from side to side with the axis of the member 4 as the center line, so the diffuser holes 42 shown in FIG. 4C are linearly arranged.
- the bubble group can be supplied to the membrane unit 3 more uniformly.
- the air diffusing member 4 of the third embodiment is formed such that a plurality of air diffusing holes 42 are arranged in two rows in the direction of the axis L of the air diffusing pipe 41 as shown in FIG.
- the illustrated air diffusion holes 42a and 42b include a straight line L1 passing through the air diffusion holes 42a in one row and the axis O of the air diffusion tube 41, and the air diffusion holes 42b and the shaft center O in the other row facing the air diffusion holes 42a.
- the angle formed by the straight line L2 is less than 180 degrees, preferably 170 degrees or less. In the specific mode shown in FIG.
- the air diffuser holes 42a and 42b facing each other include a straight line L1 passing through the air diffuser hole 42a and the axis O of the air diffuser tube 41, and the air diffuser hole 42b and the axis O. Are formed so that the angle formed by the straight line L2 passing through the angle is 90 degrees.
- a specific example of setting the diameter and the number of the air holes 42 of the air diffusion member 4 of the present embodiment will be described.
- An example of setting the diameter and number of diffuser holes when the design throughput Q is 0.6 m 3 / m 2 ⁇ day (19.8 m 3 / day) and the total diffused air volume Dm 3 / min is 12Q will be described.
- the diffused flow velocity E from the diffused holes is described in the description of the first embodiment. According to the calculation method, it is calculated as about 12 m / sec. Since the calculated value of E is larger than 10 m / sec, the air diffusion hole diameter Bmm and the number C of air diffusion holes of the membrane unit according to the specific example are appropriate specifications.
- the air bubble group can be ejected equally left and right with the axis of the member 4 as the center line, the air bubble group can be more uniformly compared with the air diffusing member 4 of the first embodiment. It can be supplied to the membrane unit 3.
- the plurality of air diffusion holes 42 are arranged in two rows in the axial direction of the air diffusion tube 41, the air bubble group can be supplied with high density and uniformity compared to the air diffusion member 4 of the second embodiment.
- the diffuser member 4 of the fourth embodiment shown in FIG. 6 has the diffuser holes 43 having a larger diameter than the diffuser holes 42 of the diffuser member 4 of the first embodiment, while the number of the diffuser holes 43 is the diffuser holes. The number is set to be less than 42. As shown in FIGS. 6A and 6B, the air diffusion holes 43 are formed on the lower surface of the air diffusion member 4.
- a specific example of setting the diameter and the number of the air holes 43 of the air diffusion member 4 of the present embodiment will be described.
- An example of setting the diameter and number of diffuser holes when the design throughput Q is 0.6 m 3 / m 2 ⁇ day (19.8 m 3 / day) and the total diffused air volume Dm 3 / min is 6Q will be described.
- the diffuser flow velocity E from the diffuser holes is described in the description of the first embodiment. According to the calculation method, it is calculated as about 12 m / sec. Since the calculated value of E is larger than 10 m / sec, the air diffusion hole diameter Bmm and the number C of air diffusion holes of the membrane unit according to the specific example are appropriate specifications.
- the diffuser member 4 of the present embodiment described above has a total diffused air volume of 6 ⁇ Qm 3 / min equivalent to that of the diffuser member 4 of the first embodiment (aeration flow velocity E of about 12 m / second). Since the number of diffuser holes in the diffuser member 4 is smaller than that of the diffuser member 4 of the first embodiment, the amount of diffused air per unit diffuser hole (m 3 / min) is larger than that of the diffuser member 4. Thereby, a gas-liquid mixed flow larger than at least the air diffusing member 4 is formed.
- the bubble group 401 provided from the diffuser member 4 rises by the gas-liquid mixed flow and is divided into a plurality of bubble groups 402 by collision with the bubble group dividing member 5. Since the gas-liquid mixed flow is not reduced so much by the collision, the cleaning effect of the membrane unit 3 is maintained. As described above, according to the air diffusing member 4 of the present embodiment, the cleaning effect of the membrane unit is improved and maintained.
- the membrane separation apparatus according to the present invention is not limited to the application to the biological reaction tank in which the activated sludge is retained as in Embodiments 1 to 4 above, but is also a water purification facility and an industrial wastewater treatment facility using a flocculant.
- the present invention can also be applied to general water treatment facilities that require solid-liquid separation of suspended substances.
Abstract
Description
図1に示された本実施形態の膜分離装置1はMBR方式の生物反応槽10内の膜モジュール3に対して散気部材4から散気された膜洗浄用の空気の気泡群401を気泡群分割部材5によって複数の気泡群402に分割させることで膜モジュールの洗浄効果の均一化を図る。すなわち、本実施形態に係る気泡群の分割は、活性汚泥の活性化を高めるために気泡を微細化させて酸素の溶解効率の向上を目的とするものではなく、散気部材から供された気泡群を気泡群分割部材と衝突させて分割して多方向に振分けることを目的とする。
膜分離装置1は、膜モジュール2を生物反応槽10の深さ方向に複数積重して構成される膜ユニット3と、膜ユニット3に対して曝気用及び膜洗浄用の空気の気泡群を散気させる散気部材4と、前記気泡群を複数の気泡群に分割させる気泡群分割部材5とから成る。膜分離装置1はMBRの生物反応槽10内の液相11に浸漬されるように設置される。
図1を参照しながら膜分離装置1の作用について説明する。ここでは、縦断面が円形を成す気泡群分割部材5を備えた膜分離装置1の作用について説明する。
膜分離装置1によれば生物反応槽10内の膜ユニット3に対して散気部材4から供された膜洗浄用の空気の気泡群401が気泡群分割部材5によって複数の気泡群402に分割される。そして、この分割された気泡群402が膜ユニット3の各膜モジュール2に対して均一に供されるので、膜モジュール3の膜面の洗浄むらが生じにくくなる。これにより、有効な膜面比率が高く維持され、効率の高い固液分離が可能となる。また、気泡群401の細分化が回避されることで、微細化された気泡に比べてその平均気泡径が大きく上昇浮力も高いので、気液混合流速を高く維持できる。以上のように散気部材やその散気点を増設させることなく膜面洗浄の不均一化を防止して膜モジュール3の分離膜の固液分離機能を維持できる。尚、上述の散気部材4は散気管タイプのものであるがノズルタイプのような散気孔が上方へ向いている態様のものが採用されてもこの散気部材4から供された気泡群を気泡群分割部材5によって分割できる。
実施形態2の散気部材4は図4(a)に示したように散気孔42が散気管41下側に散気孔を左右に振り分けるように形成されている。この態様によれば気泡群分割部材5との相乗効果により、気泡群の分割がより均一となる供給が期待できる。
実施形態3の散気部材4は図5(a)に示すように複数の散気孔42が散気管41の軸L方向に二列に配置されるように形成されている。図示された散気孔42a,42bは一方の列の散気孔42aと散気管41の軸心Oとを通る直線L1と前記散気孔42aと対向する他方の列の散気孔42bと軸心Oとを通る直線L2とで成す角度が180度未満、好ましくは170度以下となるように形成される。図5(b)に示された具体的な態様においては、対向する散気孔42a,42bは、散気孔42aと散気管41の軸心Oとを通る直線L1と、散気孔42bと軸心Oとを通る直線L2とで成す角度が90度となるように形成されている。
図6に示された実施形態4の散気部材4はその散気孔43が実施形態1の散気部材4の散気孔42よりも大径に形成される一方で散気孔43の数は散気孔42の数よりも少なく設定されている。図6(a)、図6(b)に示されたように散気孔43は散気部材4の下面にて形成されている。
本発明に係る膜分離装置は、上記の実施形態1~4のような活性汚泥を滞留させた生物反応槽への適用に限定されることなく、凝集剤が用いられる浄水設備、産業排水処理設備に例示される懸濁物質の固液分離が必要な一般的な水処理設備にも適用できる。
2…膜モジュール
3…膜ユニット
4…散気部材、42,42a,42b,43…散気孔
5…気泡群分割部材
401,402…気泡群
Claims (11)
- 膜モジュールを水槽の深さ方向に複数積重させて成る膜ユニットと、
前記膜ユニットの下方に配置され当該膜ユニットへの膜洗浄用の空気を散気する散気部材と、
前記膜ユニットと前記散気部材との間に配置され当該散気部材から供された空気の気泡群を複数の気泡群に分割させる気泡群分割部材と
を備えたこと
を特徴とする膜分離装置。 - 前記気泡群分割部材は前記散気部材の径よりも大径であると共に当該散気部材の軸と平行に配置される立体形状の障害部材からなること
を特徴とする請求項1に記載の膜分離装置。 - 前記気泡群分割部材はその縦断面の下辺が下に凸の立体に形成されたこと
を特徴とする請求項2に記載の膜分離装置。 - 前記気泡群分割部材はその縦断面の下辺が半円形を成すこと
を特徴とする請求項3に記載の膜分離装置。 - 前記気泡群分割部材はその縦断面の上辺が三角形である一方で下半部が半円形を成すこと
を特徴とする請求項3に記載の膜分離装置。 - 前記気泡群分割部材はその縦断面が円形を成すこと、または、その縦断面の上辺が釣鐘状である一方で下半部が半円形を成すこと
を特徴とする請求項3に記載の膜分離装置。 - 前記散気部材は管状の散気管からなりこの散気管の下面に複数の散気孔が形成されたことを特徴とする請求項1に記載の膜分離装置。
- 前記散気孔は隣接する散気孔が前記散気部材の軸線に対して斜めに配置されるように形成されたこと
を特徴とする請求項7に記載の膜分離装置。 - 前記隣接する散気孔は一方の散気孔と前記散気管の軸心とを通る直線と他方の散気孔と前記軸心とを通る直線とで成す角度が180度未満となるように形成されたこと
を特徴とする請求項8に記載の膜分離装置。 - 前記複数の散気孔は前記散気管の軸方向に二列に配置されるように形成されたこと
を特徴とする請求項7に記載の膜分離装置。 - 前記散気孔は、前記一方の列の散気孔と前記散気管の軸心とを通る直線と前記散気孔と対向する他方の列の散気孔と前記軸心とを通る直線とで成す角度が180度未満となるように形成されたこと
を特徴とする請求項10に記載の膜分離装置。
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CA2825744A CA2825744C (en) | 2011-02-28 | 2012-01-23 | Membrane separation device with air bubble group splitting member |
SG2013055041A SG192034A1 (en) | 2011-02-28 | 2012-01-23 | Membrane separation device |
JP2013502211A JP5823489B2 (ja) | 2011-02-28 | 2012-01-23 | 膜分離装置 |
KR1020137019600A KR101501998B1 (ko) | 2011-02-28 | 2012-01-23 | 막 분리장치 |
AU2012224335A AU2012224335B2 (en) | 2011-02-28 | 2012-01-23 | Membrane separation device |
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CN103861348B (zh) * | 2014-03-24 | 2016-10-05 | 广西国宏智鸿环境科技发展有限公司 | 一种具有在线自动冲洗功能的双滤筒过滤器 |
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