WO2023042550A1 - Procédé et dispositif de traitement d'eaux usées organiques - Google Patents

Procédé et dispositif de traitement d'eaux usées organiques Download PDF

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WO2023042550A1
WO2023042550A1 PCT/JP2022/028835 JP2022028835W WO2023042550A1 WO 2023042550 A1 WO2023042550 A1 WO 2023042550A1 JP 2022028835 W JP2022028835 W JP 2022028835W WO 2023042550 A1 WO2023042550 A1 WO 2023042550A1
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Prior art keywords
organic wastewater
membrane carrier
biofilm
air
reaction tank
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PCT/JP2022/028835
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English (en)
Japanese (ja)
Inventor
柳瀬哲也
安井英斉
寺嶋光春
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メタウォーター株式会社
公立大学法人北九州市立大学
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Publication of WO2023042550A1 publication Critical patent/WO2023042550A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • 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
    • 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
    • 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
    • C02F3/06—Aerobic processes using submerged filters
    • 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
    • C02F3/10—Packings; Fillings; Grids
    • 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
    • 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
    • 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 method and apparatus for treating organic wastewater.
  • a treatment device that treats organic wastewater such as sewage uses a method of removing, for example, contaminants (hereinafter simply referred to as contaminants) contained in wastewater.
  • This method is, for example, an activated sludge method in which organic matter is decomposed by microorganisms propagated in a reaction tank (hereinafter also referred to as activated sludge).
  • Contaminants are, for example, organic substances, suspended substances, etc. (hereinafter simply referred to as organic substances or substrates) (see Patent Document 1).
  • an organic wastewater treatment method in an organic wastewater treatment apparatus wherein the organic wastewater treatment apparatus includes a reaction tank for biologically treating contaminants contained in the organic wastewater. , a solid-liquid separation device for separating sludge from wastewater discharged from the reaction tank, and a feeder for supplying at least oxygen to the reaction tank, wherein the reaction tank is supplied by the feeder. It has a tubular membrane carrier for molecularly diffusing the oxygen into the reaction vessel through the plurality of holes, and the membrane carrier causes the oxygen to molecularly diffuse into the reaction vessel through the plurality of holes.
  • a biofilm containing aerobic bacteria is formed on the outer periphery of the membrane carrier, the biofilm is a biofilm that performs biological treatment of the contaminants with the aerobic bacteria, and the solid-liquid separation device is and separating said sludge containing said biofilm from said waste water.
  • FIG. 1 is a diagram illustrating the configuration of an organic wastewater treatment apparatus 800 in a first comparative example.
  • FIG. 2 is a diagram illustrating the configuration of an organic wastewater treatment apparatus 900 in a second comparative example.
  • FIG. 3 is a diagram illustrating the configuration of the organic wastewater treatment apparatus 100 according to the first embodiment.
  • FIG. 4 is a vertical sectional view for explaining the configuration of the film carrier 72 in the first embodiment.
  • FIG. 5 is a vertical sectional view for explaining the configuration of the film carrier 72 in the first embodiment.
  • FIG. 6 is a diagram for explaining the effects of the first embodiment.
  • FIG. 7 is a diagram for explaining the effects of the first embodiment.
  • FIG. 8 is a diagram for explaining the effects of the first embodiment.
  • FIG. 1 is a diagram illustrating the configuration of an organic wastewater treatment apparatus 800 in a first comparative example.
  • FIG. 2 is a diagram illustrating the configuration of an organic wastewater treatment apparatus 900 in a second comparative example.
  • FIG. 3 is a diagram
  • FIG. 9 is a diagram illustrating the configuration of the reaction vessel 70 in the first modified example.
  • FIG. 10 is a diagram illustrating the configuration of the membrane carrier 72 in the first modified example.
  • FIG. 11 is a diagram illustrating the configuration of the membrane carrier 72 in the first modified example.
  • FIG. 1 is a diagram illustrating the configuration of an organic wastewater treatment apparatus 800 in a first comparative example.
  • the organic wastewater treatment apparatus 800 treats contaminants by a so-called activated sludge method.
  • the organic wastewater treatment apparatus 800 has, for example, a primary sedimentation tank 10, a reaction tank 20, a final sedimentation tank 30, and an air feeder 40, as shown in FIG.
  • the primary sedimentation tank 10 sediments and separates organic substances (eg, solid organic substances) contained in the wastewater 1 .
  • the primary sedimentation tank 10 discharges the separated organic matter as primary sedimentation sludge to a thickener (not shown), and discharges the waste water 1 from which the organic matter has been separated to the reaction tank 20 .
  • the reaction tank 20 includes, for example, a tank body 21 from which waste water 1 is discharged from the primary sedimentation tank 10, and air 2 (oxygen ) to treat the wastewater 1 by biological treatment.
  • reaction tank 20 for example, an aeration process is performed in which air 2 is supplied to the activated sludge existing in the tank main body 21.
  • organic matter eg, soluble organic matter contained in the wastewater 1 is decomposed (consumed) by activated sludge supplied with the air 2 .
  • the reaction tank 20 discharges the wastewater 1 after decomposition of organic matter by activated sludge, for example, to the final sedimentation tank 30 .
  • the final sedimentation tank 30, for example, sediments and separates the sludge contained in the wastewater 1 discharged from the reaction tank 20, and discharges the separated sludge as activated sludge.
  • the final sedimentation tank 30 supplies part of the activated sludge as excess sludge to a thickener (not shown), and returns activated sludge other than the excess sludge to the reaction tank 20 as return sludge.
  • the final sedimentation tank 30 discharges the waste water 1 (supernatant liquid) from which the activated sludge has been separated, for example, to a post-stage sterilization apparatus (not shown). After that, the sterilization apparatus sterilizes the wastewater 1 discharged from the final sedimentation tank 30, for example, and discharges the sterilized treated water.
  • the air supplier 40 is, for example, an air blower and supplies the air 2 to the reaction vessel 20. Specifically, the air supplier 40 supplies the air 2 into the reaction vessel 20 through the air supply pipe 22 provided at the bottom of the reaction vessel 20 .
  • the organic wastewater treatment apparatus 800 separation of activated sludge in the final sedimentation tank 30 is performed by natural sedimentation. Therefore, for example, if the activated sludge does not settle sufficiently due to bulking or the like, the organic wastewater treatment apparatus 800 may carry over the activated sludge to the subsequent apparatus.
  • the concentration of activated sludge in the reaction tank 20 changes depending on the amount of returned sludge from the final sedimentation tank 30 . Therefore, the concentration of activated sludge in the reaction tank 20 depends on the natural settling property in the final sedimentation tank 30 and the size of the final sedimentation tank 30, and may become unstable.
  • the power for supplying the air 2 by the air supplier 40 may be increased due to the need to maintain the concentration of activated sludge in the reaction tank 20.
  • a membrane separation activated sludge method has been proposed as a method for treating pollutants. The membrane separation activated sludge method will be explained with reference to FIG.
  • FIG. 2 is a diagram illustrating the configuration of an organic wastewater treatment apparatus 900 in a second comparative example.
  • the organic wastewater treatment apparatus 900 is, for example, an organic wastewater treatment apparatus using a membrane separation activated sludge method.
  • the organic wastewater treatment apparatus 900 includes, as shown in FIG. have That is, the organic wastewater treatment apparatus 900 has, for example, a solid-liquid separation tank 50 in place of the final sedimentation tank 30 compared to the organic wastewater treatment apparatus 800 .
  • the organic wastewater treatment device 900 further comprises an air feeder 60, for example.
  • the solid-liquid separation tank 50 includes, for example, a tank body 51 from which waste water 1 is discharged from the reaction tank 20, and air 2 ( oxygen) and a separation membrane 53 for separating activated sludge contained in the wastewater 1 .
  • the separation membrane 53 is, for example, a microfiltration membrane or an ultrafiltration membrane.
  • the solid-liquid separation tank 50 for example, by aerating the separation membrane 53 from below with the air 2 supplied from the air supply pipe 52, an upward flow of the air 2 and the waste water 1 is generated, and the separation membrane The activated sludge is separated while suppressing clogging caused by proliferation (coating) of the activated sludge in the membrane 53 and clogging of the separation membrane 53 .
  • the solid-liquid separation tank 50 supplies part of the activated sludge as excess sludge to the thickener, and returns the activated sludge other than the excess sludge to the reaction tank 20 as return sludge.
  • the solid-liquid separation tank 50 discharges the wastewater 1 (supernatant liquid) after the separation of the activated sludge to the subsequent sterilization apparatus by sucking it from above with a pump (not shown).
  • the air supply device 60 is, for example, an air blower, and supplies air 2 to the solid-liquid separation tank 50. Specifically, the air supply device 60 supplies the air 2 to the air supply pipe 52 provided at the bottom of the solid-liquid separation tank 50 .
  • the organic wastewater treatment apparatus 900 separates activated sludge using the separation membrane 53 instead of separating activated sludge by natural sedimentation. As a result, the organic wastewater treatment apparatus 900 can prevent the activated sludge from flowing out to the subsequent apparatus.
  • the concentration of activated sludge separated from the wastewater 1 in the solid-liquid separation tank 50 can be increased. Therefore, in the organic wastewater treatment apparatus 900, for example, the size of the reaction tank 20 can be reduced compared to the organic wastewater treatment apparatus 800 described with reference to FIG.
  • the organic wastewater treatment apparatus 900 uses, for example, a circulation pump (not shown) to circulate the activated sludge between the reaction tank 20 and the solid-liquid separation tank 50, and the activated sludge by the separation membrane 53. may be used to separate the Further, the organic wastewater treatment apparatus 900 may have a separation membrane 53 in the reaction tank 20 instead of having the solid-liquid separation tank 50, for example. Moreover, in the membrane separation activated sludge process of FIG. 2, in order to maintain the performance of the reaction tank 50, the excess sludge adhering to the separation membrane 53 can be removed by washing.
  • the separation membrane 53 is periodically washed with a chemical such as hypochlorous acid or alkali in order to prevent clogging of the separation membrane 53. There is a need. Further, in the organic wastewater treatment apparatus 900, for example, the separation membrane 53 needs to be replaced periodically.
  • the power of the air supply device 40, the circulation pump, etc. may be increased. .
  • the main component of the activated sludge separated by the separation membrane 53 is the fungus grown in the wastewater 1.
  • Such excess sludge is dispersed and has the property of being difficult to dewater. Therefore, in the organic wastewater treatment apparatus 900, for example, it is necessary to put a large amount of coagulant in a concentrator or the like.
  • running costs for example, air supply power, separation membrane replacement costs, cleaning costs, flocculant costs
  • FIG. 3 is a diagram illustrating the configuration of the organic wastewater treatment apparatus 100 according to the first embodiment.
  • 4 and 5 are vertical cross-sectional views illustrating the configuration of the film carrier 72 in the first embodiment.
  • the organic wastewater treatment device 100 performs biological treatment on contaminants contained in the organic wastewater 1 .
  • the organic wastewater treatment apparatus 100 has, for example, a primary sedimentation tank 10, a reaction tank 70, an air feeder 80, and a solid-liquid separation apparatus 90, as shown in FIG. That is, the organic wastewater treatment apparatus 100 has a reaction tank 70 instead of the reaction tank 20, for example, compared with the organic wastewater treatment apparatus 900.
  • the organic wastewater treatment apparatus 100 has, for example, an air supplier 80 (hereinafter also referred to as a supplier) in place of the air supplier 40 .
  • the organic wastewater treatment apparatus 100 has, for example, a solid-liquid separation device 90 instead of the solid-liquid separation tank 50 .
  • the air supplier 80 is, for example, a blower such as an air blower or a fan, and supplies at least oxygen to the reaction vessel 70 .
  • the gas supplied by the air supply device 80 may be any other gas as long as it contains oxygen, and hereinafter, air is exemplified as the gas containing oxygen.
  • the reaction tank 70 performs biological treatment on contaminants contained in organic wastewater.
  • the reaction tank 70 is, for example, a membrane aerated biofilm reactor (MABR: Membrane Aerated Biofilm Reactor).
  • MABR Membrane Aerated Biofilm Reactor
  • the reaction tank 70 includes, for example, a tank body 71 into which the wastewater 1 flows from the primary sedimentation tank 10, and one or more membrane carriers 72 into which the air 2 supplied by the air supply device 80 is supplied. have The amount of air supplied by the air supply device 80 is smaller than the amount of air supplied by the air supply device described in FIGS.
  • the membrane carrier 72 is a tubular membrane carrier that molecularly diffuses the air supplied by the air supplier 80 into the reaction vessel 70 through a plurality of holes.
  • the membrane carrier 72 is a hydrophobic hollow fiber membrane, for example, a Teflon (registered trademark) membrane.
  • the membrane carrier 72 is, for example, a tubular membrane whose axial direction extends in the vertical direction (the height direction of the reaction vessel 70).
  • a large number of fine pores for example, pores of about 0.1 micron
  • a case where four membrane carriers 72 are arranged in the horizontal direction in the reaction vessel 70 will be described below, but the number of membrane carriers 72 other than four may be arranged in the reaction vessel 70. There may be. Further, hereinafter, the case where the air 2 supplied from the air supplier 80 is supplied from the vertically downward direction to the vertically upward direction inside the membrane carrier 72 will be described. 2 may be supplied from the vertical upward direction to the vertical downward direction inside the membrane carrier 72 .
  • the membrane carrier 72 may be, for example, U-shaped with both ends facing vertically upward. Further, the membrane carrier 72 may be, for example, U-shaped with both ends facing vertically downward.
  • the membrane carrier 72 emits the air 2 supplied from the air supplier 80 toward the outside (inside the reaction vessel 70) from a plurality of holes on the surface (molecular diffusion). do.
  • a biofilm containing aerobic bacteria hereinafter referred to as biofilm R1
  • This biofilm is a biofilm that biologically treats contaminants with aerobic bacteria. For example, as shown in FIG.
  • activated sludge adheres to form a massive biofilm, which is a biofilm.
  • R1 is formed.
  • the biofilm R1 adhered to the surface of the membrane carrier 72 decomposes the organic matter contained in the wastewater 1 and proliferates.
  • the air supplier 80 preferably maintains the internal pressure of the membrane carrier 72 at a level that does not generate air bubbles from the pores on the surface (for example, a pressure equal to or lower than the water pressure).
  • the pressure of the air supplied by the air supplier 80 can be made lower than the water pressure, so that the pressure of the air supplied by the air supplier 40 described in FIGS. 1 and 2 can be lowered. can. Therefore, the operating power of the air supplier 80 can be reduced compared to the operating power of the air supplier 40 .
  • the reaction tank 70 discharges the waste water 1 (waste water) after the reaction with the biofilm R1 to the solid-liquid separation device 90.
  • the solid-liquid separator 90 separates lumpy sludge containing biofilm R1 from the waste water discharged from the reaction tank 70 .
  • the sludge to be separated contains various bacteria in addition to living or dead aerobic bacteria.
  • the solid-liquid separation device 90 only needs to have a sludge separation function, and may be, for example, a device including the separation membrane described in FIG. Further, the solid-liquid separator 90 may separate the sludge to be separated from the wastewater by gravity sedimentation, or may separate the sludge to be separated from the wastewater by sand filtration. In addition, the solid-liquid separation device 90 may separate the sludge to be separated from the wastewater using a carrier (so-called high-speed carrier filtration).
  • a carrier so-called high-speed carrier filtration
  • the organic wastewater treatment apparatus 100 further includes a stripping device 73 and a control device 74, for example.
  • the stripping device 73 is, for example, a device that strips the biofilm R1 adhering to the membrane carrier 72 from the membrane carrier 72 by vibrating the membrane carrier 72 .
  • the control device 74 is, for example, a computer having a CPU (Central Computing Unit), a memory, etc., and a program stored in a storage device (not shown) cooperates with the CPU to enable the peeling device 73 to remove biofilms.
  • the timing of peeling R1 (hereinafter also referred to as peeling timing) is controlled.
  • the biofilm R1 is peeled off by using the peeling device 73 in the reaction tank 70. Detachment may be performed (so-called membrane cleaning).
  • the control device 74 may control the timing of jetting, for example.
  • the reaction tank 70 in the present embodiment decomposes the organic substances contained in the wastewater 1 discharged from the primary sedimentation tank 10 to the reaction tank 70 by the biofilm R1 adhered to the membrane carrier 72, and takes in the organic substances.
  • the aggregated biofilm R1 is intermittently separated from the membrane carrier 72, and the sludge containing the biofilm R1 is discharged to the solid-liquid separation device 90.
  • the solid-liquid separator It is possible to suppress the amount of sludge discharged to 90. Therefore, in the reaction tank 70 , in this case, it is possible to discharge the wastewater 1 with low growth potential to the solid-liquid separation device 90 . Therefore, it becomes possible to prevent the proliferation of activated sludge in the solid-liquid separator 90 . Further, when the solid-liquid separation device 90 performs solid-liquid separation using a separation membrane, it is possible to prevent clogging of the separation membrane.
  • the sludge containing the biofilm R1 is discharged to the solid-liquid separation device 90, so that solid-liquid separation is performed.
  • the device 90 performs solid-liquid separation using a separation membrane, it is possible to prevent clogging of the separation membrane.
  • the solid-liquid separation device 90 since the solid-liquid separation device 90 according to the present embodiment solid-liquid separates solid-liquid lumps of sludge from waste water, it is possible to easily dewater the separated sludge. Therefore, in the organic wastewater treatment apparatus 100 according to the present embodiment, it is possible to reduce the amount of flocculant that needs to be put in a dewatering machine or the like for dehydrating sludge, thereby reducing the cost required for dehydrating sludge. it becomes possible to
  • the reaction vessel 70 of the present embodiment by using the tubular membrane carrier 72, it is possible to increase the surface area compared to the case of using a membrane carrier having a shape other than tubular. Therefore, in the organic wastewater treatment apparatus 100 of the present embodiment, it is possible to reduce the volume of reaction between the activated sludge (aerobic microorganisms) and the organic matter, and it is possible to reduce the size of the reaction tank 70. . Specifically, in the organic wastewater treatment apparatus 100, for example, the vertical height (water depth) of the reaction tank 70 can be reduced.
  • the air supplier 80 can keep the pressure inside the membrane carrier 72 at a level that does not generate air bubbles from the pores on the surface, for example, the air supplier 40 described in FIG. It is possible to suppress the power associated with the supply of the air 2 more than when is used.
  • each of the anaerobic layers R3 from the surface of the membrane carrier 72 toward the liquid phase side. That is, in this case, between the two membrane carriers 72, as shown in FIG. be. Therefore, in the reaction tank 70, for example, ammonia contained in the wastewater 1 can be nitrified by the nitrification action in the aerobic layer R1. Then, in the anoxic layer R2 and the anaerobic layer R3, nitrogen contained in the wastewater 1 (for example, nitrite nitrogen) can be removed (denitrified) by a denitrification reaction.
  • the biofilm R1 adhered to the membrane carrier 72 is treated with organic matter.
  • the concentration of activated sludge at a constant level there is no need to maintain the concentration of activated sludge at a constant level. Therefore, in the organic wastewater treatment apparatus 100 of the present embodiment, for example, like the organic wastewater treatment apparatus 900 described in FIG. no need to send it back to As a result, in the organic wastewater treatment apparatus 100, for example, it is possible to substantially omit equipment necessary for returning sludge. If the sludge is returned to the reaction tank 70 , the returned sludge grows as activated sludge in the reaction tank 70 .
  • the sludge is not substantially returned, as long as it does not deviate from the gist of the present invention. indicates that the sludge is allowed to be returned. Specifically, if the dewaterability of the sludge separated in the solid-liquid separation device 90 can be maintained in a state higher than the dewaterability of the sludge in the organic wastewater treatment device described in FIG. Sludge may be returned to the reaction tank 70 . When such return is performed, the amount of sludge returned (return time) in the organic wastewater treatment apparatus described in FIG. 2 is reduced (shortened).
  • the organic wastewater treatment apparatus 900 membrane separation activated sludge method described in FIG. Liquor Suspended Solids
  • the reaction tank 70 of the present embodiment since various biological treatments proceed with the biofilm attached to the surface of the membrane carrier 72, the MLSS concentration can be lowered compared to the membrane separation activated sludge method, and the solid The amount of sludge that flows into the liquid separator 90 and clogs the solid-liquid separation 80 can be minimized.
  • a gas having a higher oxygen concentration than air may be supplied to the membrane carrier 72 from the air supply device 80 in the present embodiment.
  • a gas having a higher oxygen concentration than air may be supplied to the membrane carrier 72 from the air supply device 80 in the present embodiment.
  • the oxygen supplied to the membrane carrier 72 may be, for example, oxygen obtained by water electrolysis using renewable energy.
  • oxygen obtained by electrolyzing water using electric energy generated by using waste heat in sludge incineration may be used.
  • various power generation technologies such as organic Rankine cycle (ORC) can be used.
  • FIG. 6 is a graph showing the relationship between the detachment interval of biofilm R1 and the removal rate of organic matter.
  • the horizontal axis in the graph shown in FIG. 6 indicates the separation interval of the biofilm R1 (hereinafter simply referred to as the separation interval), and the vertical axis in the graph shown in FIG. (also called removal rate).
  • the graph shown in FIG. 6 indicates that the removal rate increases until the separation interval reaches around 24 (h), and further, the removal rate decreases as the separation interval increases from around 24 (h). Further, the graph shown in FIG. 6 indicates that the removal rate is about 88 (%) when the peeling interval is around 24 (h), and the peeling interval is around 12 (h) or 48 ( h) indicates that the removal rate is about 80 (%).
  • the graph shown in FIG. 6 shows that, for example, when the separation interval is 12 (h) or more and 48 (h) or less, the removal rate can be maintained at 80 (%) or more, and the solid-liquid separation This indicates that it is possible to suppress the organic matter discharged to the device 90 to 20(%) or less.
  • the graph shown in FIG. 6 indicates that, for example, when the separation interval is 48 (h) or more, the removal rate decreases.
  • the thickness of the biofilm R1 which is a lump of sludge, reaches a predetermined thickness or more, the membrane carrier 72 side of the biofilm R1 (the portion that can directly receive the supply of oxygen from the membrane carrier 72) This is because the wastewater 1 is not sufficiently supplied, and the removal of organic matter is not efficiently performed.
  • the control device 74 controls the biofilm R1 such that the separation interval is 12 (h) or more and 48 (h) or less, that is, the biofilm R1 is maintained at a removal rate of 80 (%) or more. may control the peeling timing of the . Specifically, the control device 74 may control the peeling timing of the biofilm R1 so that the peeling interval is 24 (h) or 48 (h), for example.
  • the solid-liquid separator 90 performs solid-liquid separation using a separation membrane will be described as an example.
  • FIG. 7 is a graph showing the relationship between the biofilm R1 detachment interval and the flux in the solid-liquid separator 90. As shown in FIG. The horizontal axis in the graph shown in FIG. 7 indicates the peeling interval of the biofilm R1, and the vertical axis in the graph shown in FIG. (%) shows the flux of the solid-liquid separator 90.
  • the graph shown in FIG. 7 indicates that the flux increases until the separation interval reaches around 24 (h). Moreover, the graph shown in FIG. 7 indicates that the flux becomes almost 100(%) when the separation interval is 24(h) or more.
  • the graph shown in FIG. 7 shows that, for example, when the separation interval is 24 (h) or more, it is possible to form a sufficiently large biofilm R1 on the membrane carrier 72, and the solid-liquid separation device 90 Since it becomes possible to suppress the occurrence of clogging, it is possible to keep the flux at a high level.
  • the graph shown in FIG. 7 shows that, for example, when the peeling time is 24 (h) or less, the biofilm R1 that is not large enough is discharged to the solid-liquid separator 90, so the solid-liquid separator Clogging occurs at 90, indicating a drop in flux.
  • control device 74 controls the peeling timing of the biofilm R1, for example, so that the peeling interval is 24 (h) or more, that is, so that the flux close to 100 (%) is maintained. you can
  • control device 74 controls the peeling timing of the biofilm R1, for example, so that the amount of substrates such as organic substances discharged from the reaction tank 70 to the solid-liquid separation device 90 satisfies a predetermined condition. good.
  • control device 74 controls, for example, the amount of substrate discharged from the reaction tank 70 to the solid-liquid separation device 90 (that is, the amount of substrate in the waste water) is the amount of waste water flowing into the reaction tank 70 from the primary sedimentation tank 10 .
  • the peeling timing of the biofilm R1 may be controlled so that the amount of the substrate is less than a predetermined ratio, preferably about 1/5.
  • control device 74 is arranged so that, for example, the return sludge from the solid-liquid separation device 90 to the reaction tank 70 does not need to be returned, that is, the control device 74 controls, for example, the necessary amount of activated sludge by increasing the activated sludge.
  • the separation timing of the biofilm R1 may be controlled so that the sludge is maintained in the reaction tank 70.
  • FIG. 8 is a graph showing the relationship between the detachment interval of biofilm R1 and the moisture content of the dehydrated cake.
  • the horizontal axis in the graph shown in FIG. 8 indicates the peeling interval of the biofilm R1, and the vertical axis in the graph shown in FIG. there is
  • the graph shown in FIG. 8 shows that the moisture content decreases as the separation interval increases. Moreover, the graph shown in FIG. 8 shows that when the peeling interval is longer than 24 (h), the moisture content is much lower than when the peeling time is shorter than 24 (h).
  • the graph shown in FIG. 8 indicates that, for example, when the separation interval is 24 (h) or more, the moisture content of the dehydrated cake can be effectively reduced.
  • the sludge containing exfoliated biofilm R1 obtained when the exfoliation interval is 24 (h) or more is dense. Dehydration of dense sludge in this manner yields sludge with a low moisture content.
  • control device 74 controls the peeling timing of the biofilm R1, for example, so that the peeling interval is 24 (h) or more, that is, the water content of the dehydrated cake is 75 (%) or less.
  • the control device 74 controls the peeling timing of the biofilm R1 according to all the graphs shown in FIGS. 6 to 8, for example, so that the peeling interval is 24 (h) or more and 48 (h) or less. It may be something to do.
  • the biofilm R1 adhering to the membrane carrier 72 takes in organic matter and becomes agglomerate on the membrane carrier 72 . Therefore, in the organic wastewater treatment apparatus 100 , it is possible to discharge wastewater containing sludge (lump sludge) containing the biofilm R ⁇ b>1 in the form of blocks to the solid-liquid separator 90 . In addition, in the organic wastewater treatment apparatus 100, by forming the massive biofilm R1 on the membrane carrier 72, it is possible to reduce the amount of organic matter and activated sludge discharged from the reaction tank 70 to the solid-liquid separation apparatus 90. become.
  • the organic wastewater treatment apparatus 100 it is possible to prevent the growth of activated sludge in the solid-liquid separation device 90 and the occurrence of clogging in the solid-liquid separation device 90, and the occurrence of clogging of the solid-liquid separation device 90. can be prevented.
  • the massive biofilm R1 has a large particle size and tends to settle. Therefore, in the organic wastewater treatment apparatus 100, the sludge separated from the wastewater in the solid-liquid separator 90 can be easily dewatered, and the amount of flocculant that needs to be put in a dehydrator or the like can be reduced. . Therefore, in the organic wastewater treatment apparatus 100, for example, it is possible to reduce costs required for dehydration of sludge.
  • the sludge (separated sludge) contained in the wastewater discharged to the solid-liquid separator 90 is lumpy sludge.
  • This blocky sludge is mainly composed of blocky biofilm R1, and this blocky sludge (hereinafter referred to as sludge of the present embodiment) is dense as described above and is easily dewatered. Then, this clumped sludge is separated by the solid-liquid separator 90 .
  • the sludge separated from the separation membrane 53 of the reaction tank 50 of FIG. The body is the subject. Such sludge is dispersed and difficult to dewater.
  • the main sludge of the present embodiment and the main sludge of FIG. 2 are different.
  • the amount of flocculant added can be reduced in this embodiment compared to the amount of flocculant added when dewatering the sludge in FIG.
  • the amount of coagulant added can be reduced, and running costs can be suppressed.
  • the stripping interval is several weeks or more, so activated sludge with low strength (soft activated sludge) is stripped. Therefore, the moisture content of the dewatered cake produced from the separated activated sludge is approximately the same as that of the dehydrated cake produced from ordinary activated sludge.
  • a biofilm capable of producing a dehydrated cake with a low moisture content (biofilm peeled from the membrane carrier 72 R1) can be obtained.
  • the organic wastewater treatment apparatus 100 in the first embodiment for example, instead of the primary sedimentation tank 10, a solid-liquid separation apparatus (not shown) that performs high-speed filtration may be used.
  • a solid-liquid separation apparatus (not shown) that performs high-speed filtration may be used.
  • the amount of organic substances (for example, solid organic substances) supplied to the reaction tank 70 can be further suppressed, and the decomposition of the organic substances in the membrane carrier 72 can be made more efficient. It becomes possible to go to
  • FIG. 9 is a diagram illustrating the configuration of the reaction vessel 70 in the first modified example.
  • 10 and 11 are diagrams for explaining the configuration of the membrane carrier 72 in the first modified example.
  • the peeling device 73 in the first modified example peels the biofilm R1 by supplying gas such as air (hereinafter also simply referred to as air). Then, the control device 74 in the first modification controls, for example, the timing at which the peeling device 73 supplies air.
  • gas such as air
  • the peeling device 73 as shown in FIG. 9, has an air supply device 73a such as a compressor that compresses air taken in from the outside to generate compressed air (not shown), and an air supply device 73a. and an air tank 73b for storing compressed air.
  • an air supply device 73a such as a compressor that compresses air taken in from the outside to generate compressed air (not shown)
  • an air supply device 73a such as a compressor that compresses air taken in from the outside to generate compressed air (not shown)
  • an air supply device 73a such as a compressor that compresses air taken in from the outside to generate compressed air (not shown)
  • an air supply device 73a such as a compressor that compresses air taken in from the outside to generate compressed air (not shown)
  • an air supply device 73a such as a compressor that compresses air taken in from the outside to generate compressed air (not shown)
  • an air supply device 73a such as a compressor that compresses air taken in from the outside to generate compressed air (
  • control device 74 controls the supply (jetting) of the compressed air stored in the air tank 73b to the reaction tank 70, for example.
  • the control device 74 supplies the compressed air stored in the air tank 73b to a plurality of locations in the reaction tank 70 via the line L3.
  • Biofilm R1 is stripped from membrane carrier 72 .
  • the line L3 is, for example, a pipe that connects the air tank 73b and multiple locations in the reaction tank 70 .
  • the control device 74 controls the separation interval of the biofilm R1 to be 24 (h) or longer, for example, as described with reference to FIG. 6 and the like.
  • control device 74 controls, for example, the generation timing of the compressed air by the air supplier 73a (compressed air for the air tank 73b) so that the pressure in the air tank 73b is maintained within a certain range. supply timing) may be controlled.
  • control device 74 controls the amount of air 2 supplied by the air supplier 80 so that the amount of air 2 supplied to the membrane carrier 72 is constant. may be
  • control device 74 controls, for example, a measuring instrument (Fig. (not shown).
  • the controller 74 may control the amount of air 2 supplied from the air supplier 80 to the membrane carrier 72, for example, according to the acquired measurement value. In the following description, it is assumed that the controller 74 controls the amount of air 2 supplied by the air supplier 80 .
  • the compressed air may be supplied, for example, to the lower ends or below the membrane carriers 72. good.
  • a unit UN1 is formed by bundling a plurality of membrane carriers 72.
  • the number of pipes constituting the line L1 for supplying the air 2 to each membrane carrier 72 and the line L2 for discharging the air 2 from each membrane carrier 72 It is possible to reduce the number of pipes that make up the
  • FIG. 9 shows a case where four units UN1 formed by bundling four membrane carriers 72 are arranged in the reaction vessel 70 .
  • a case where four membrane carriers 72 constitute a single unit UN1 will be described below, but the number of membrane carriers 72 other than four may constitute a single unit UN1. .
  • the plurality of membrane carriers 72 forming a single unit UN1 (hereinafter also simply referred to as the plurality of membrane carriers 72) are, as shown in FIG. For example, it has a first mold portion 72a formed by molding with a resin or the like, and a second mold portion 72b formed by molding the upper end portions 72d of each of the plurality of film carriers 72 with resin or the like. . That is, the plurality of film carriers 72 form a single unit UN1, for example, by molding the lower end portion 72c and the upper end portion 72d of each film carrier 72 .
  • the first mold portion 72a has, for example, a first air hole 72a1 for introducing the air 2 supplied from the air supplier 80 through the line L1 into the first mold portion 72a.
  • the line L1 is, for example, a pipe that connects the air supplier 80 and the first air holes 72a1 in each of the plurality of units UN1, as shown in FIGS. Then, the air 2 introduced into the inside of the first mold portion 72a through the air holes 72a1 is supplied to the inside of each of the plurality of membrane carriers 72 from the respective lower end portions 72c of the plurality of membrane carriers 72, for example.
  • the second mold portion 72b has, for example, a second air hole 72b1 for discharging the air 2 inside the second mold portion 72b to the outside via the line L2.
  • the line L2 is, for example, a pipe that connects the second air hole 72b1 in each of the plurality of units UN1 to the outside, as shown in FIGS. That is, the second air holes 72b1, for example, discharge the air 2 discharged into the second mold portion 72b from the upper end portions 72d of the plurality of film carriers 72 to the outside.
  • the air 2 supplied (pressurized) into the first mold portion 72a via the line L1 and the first air holes 72a1 is applied to each of the plurality of membrane carriers 72 as indicated by solid line arrows in FIG. supplied internally. At least a portion of the air 2 supplied to each membrane carrier 72 moves inside each membrane carrier 72 from the lower end 72c to the upper end 72d, as described with reference to FIG.
  • the molecules diffuse into the reaction vessel 70 through a plurality of holes h1 (for example, holes of about 0.1 microns) provided in the membrane carrier 72 .
  • the air 2 that has moved inside each film carrier 72 from the lower end portion 72c to the upper end portion 72d (the air 2 that has not been molecularly diffused into the reaction chamber 70) is discharged from the upper end portion 72d to the second mold portion, for example. 72b. After that, the air 2 supplied into the second mold portion 72b is discharged to the outside through, for example, the second air hole 72b1 and the line L2.
  • the air supplier 80 supplies air to the inside of the membrane carrier 72 from the lower end 72c (hereinafter simply referred to as the lower end) of the membrane carrier 72, for example. 2 (air 2 containing at least oxygen). Then, the membrane carrier 72 causes, for example, at least a part of the air 2 supplied from the lower end portion 72c to molecularly diffuse into the reaction vessel 70 through the plurality of holes h1, thereby dispersing the air 2 supplied from the lower end portion 72c.
  • the air 2 that has not been molecularly diffused in the reaction tank 70 is discharged outside from the upper end portion 72d (hereinafter simply referred to as the upper end) of the membrane carrier 72 .
  • the membrane carrier 72 shown in FIG. 10 has a linear shape (I shape), it is not limited to this. Specifically, the membrane carrier 72 may have any shape, for example, in which the air 2 supplied from the lower end portion 72c is discharged from the upper end portion 72d. may have
  • the air 2 is supplied (pressurized) into the membrane carrier 72 from the lower end 72c, and the air 2 in the membrane carrier 72 is discharged from the upper end 72d.
  • the membrane carrier 72 may, for example, supply the air 2 into the inside of the membrane carrier 72 from the upper end 72d and discharge the air 2 inside the membrane carrier 72 from the lower end 72c.
  • the amount of air 2 supplied to each of the plurality of membrane carriers 72 is, for example, the amount of air 2 molecularly diffused into the reaction vessel 70 through the plurality of holes h1 on the lower end portion 72c side and the amount of air 2 on the upper end portion 72d side. may be determined so that the amount of the air 2 molecularly diffused into the reaction vessel 70 from the hole h1 of is the same. That is, the amount of air 2 supplied to each of the plurality of membrane carriers 72 is determined, for example, so that the oxygen partial pressure at each position in each membrane carrier 72 is maximized (the same pressure as the atmospheric pressure). you can
  • the line L1 may be provided with a filter (not shown) for removing fine particles (for example, dust, etc.) contained in the air 2 supplied from the air supplier 80, for example.
  • a filter not shown for removing fine particles (for example, dust, etc.) contained in the air 2 supplied from the air supplier 80, for example.
  • both ends face downward (for example, vertically downward direction) in a U shape (hereinafter referred to as an inverted U).
  • the membrane carrier 72 may be arranged to form a letter shape. That is, in the reaction vessel 70, as shown in FIG. 11, for example, the membrane carrier 72 may be arranged in a state in which at least one portion (hereinafter also referred to as a curved portion 72e) is curved.
  • the unit UN2 may be formed by bundling a plurality of membrane carriers 72 arranged to form an inverted U shape. A case where two membrane carriers 72 arranged to form an inverted U shape form a single unit UN2 will be described below. may constitute the unit UN2.
  • the air 2 supplied (pressurized) into the inside of the first mold portion 72a from the air holes 72a1 is, for example, discharged from both ends 72f of the plurality of membrane carriers 72 to each of the plurality of membrane carriers 72. supplied inside the That is, each of the end portions 72f shown in FIG. 11 has the same function as the lower end portion 72c described in FIG. 10, for example.
  • the air 2 supplied from the air supplier 80 into the first mold portion 72a via the line L1 and the first air holes 72a1 is, for example, applied to a plurality of membranes as indicated by solid line arrows in FIG. supplied to each of the carriers 72 .
  • the air 2 supplied to each membrane carrier 72 moves inside each membrane carrier 72 from both end portions 72f to curved portions 72e, for example, in each membrane carrier 72 as described with reference to FIG.
  • Molecules diffuse into the reaction chamber 70 through a plurality of holes h2 (for example, holes of about 0.1 micron) provided in portions positioned outside the first mold portion 72a and the second mold portion 72b.
  • the air 2 that has moved inside each membrane carrier 72 from both end portions 72f to the curved portion 72e (the air 2 that has not been molecularly diffused into the reaction vessel 70) is, for example, the curved portion 72e of each membrane carrier 72.
  • the air 2 supplied into the second mold portion 72b is discharged to the outside through, for example, the second air hole 72b1 and the line L2. That is, the plurality of holes h3 provided in the curved portion 72e shown in FIG. 11 have the same function as the upper end portion 72d described in FIG. 10, for example.
  • the membrane carrier 72 has, for example, curved portions 72e that curve the membrane carrier 72 so that both ends 72f of the membrane carrier 72 face downward.
  • the air supplier 80 supplies air 2 (air 2 containing at least oxygen) into the inside of the membrane carrier 72 from, for example, both ends 72f of the membrane carrier 72 (in other words, each of the lower ends of the membrane carrier 72). do.
  • the membrane carrier 72 allows, for example, at least part of the air 2 supplied from at least one of both ends of the membrane carrier 72 to flow through the plurality of holes h2 (hereinafter also referred to as the plurality of first holes) into the reaction tank.
  • the air 2 that has molecularly diffused into the membrane carrier 70 and has not been molecularly diffused into the reaction vessel 70 out of the air 2 that has been supplied from at least one of both ends of the membrane carrier 72 is removed from the curved surface positioned above the plurality of holes h2. It is discharged to the outside through a plurality of holes h3 (hereinafter also referred to as a plurality of second holes) provided in the portion 72e (in other words, the upper end of the membrane carrier 72).
  • a plurality of holes h3 hereinafter also referred to as a plurality of second holes
  • the membrane carrier 72 shown in FIG. 11 is discharged into the second mold portion 72b through a plurality of holes h3 provided in the curved portion 72e, unlike the case of the film carrier 72 shown in FIG. be. Therefore, in the membrane carrier 72 shown in FIG. 11, the pressure loss associated with the discharge of the air 2 is greater than in the case of the membrane carrier 72 shown in FIG. Therefore, the membrane carrier 72 shown in FIG. 11 can increase the amount of air 2 supplied into the reaction chamber 70 by molecular diffusion, compared to the membrane carrier 72 shown in FIG.

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  • Life Sciences & Earth Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

L'invention concerne un procédé de traitement d'eaux usées organiques dans un dispositif de traitement d'eaux usées organiques. Le dispositif de traitement d'eaux usées organiques comprend : un réservoir de réaction dans lequel un traitement biologique est effectué sur un polluant qui est contenu dans les eaux usées organiques; un dispositif de séparation solide-liquide qui sépare les boues des eaux usées qui ont été évacuées du réservoir de réaction; et un dispositif d'alimentation qui alimente au moins de l'oxygène dans le réservoir de réaction. Le réservoir de réaction a un support de membrane tubulaire qui provoque une diffusion moléculaire, dans le réservoir de réaction par l'intermédiaire d'une pluralité de trous, d'oxygène qui a été alimenté par le dispositif d'alimentation. Le support de membrane provoque la diffusion moléculaire de l'oxygène dans le réservoir de réaction par l'intermédiaire de la pluralité de trous de façon à former une membrane biologique qui contient des bactéries aérobies sur la circonférence externe du support de membrane. La membrane biologique soumet le polluant à un traitement biologique par l'intermédiaire des bactéries aérobies. Le dispositif de séparation solide-liquide sépare les boues contenant la membrane biologique des eaux usées.
PCT/JP2022/028835 2021-09-15 2022-07-26 Procédé et dispositif de traitement d'eaux usées organiques WO2023042550A1 (fr)

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Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH04371298A (ja) * 1991-06-20 1992-12-24 Ebara Infilco Co Ltd 有機性汚水の処理方法および装置
JPH07256284A (ja) * 1994-03-18 1995-10-09 Nippon Kentetsu Co Ltd 廃水処理装置における生物接触濾材の逆洗方法および装置
JPH11333496A (ja) * 1998-05-22 1999-12-07 Nissin Electric Co Ltd 窒素除去用微生物保持担体
JP2000218290A (ja) * 1999-02-01 2000-08-08 Kitakyushu City 下水処理方法及び下水処理装置
JP2003033764A (ja) * 2001-07-26 2003-02-04 Ebara Corp オゾンを用いたろ過体の洗浄方法及び装置
JP2003251381A (ja) * 2002-02-28 2003-09-09 Asahi Kasei Corp メンブレンバイオリアクタによる窒素除去方法
JP2009011965A (ja) * 2007-07-06 2009-01-22 Mitsubishi Rayon Eng Co Ltd 中空糸膜モジュールおよびこれを用いた中空糸膜ユニット
JP2010284617A (ja) * 2009-06-15 2010-12-24 Eidensha:Kk バイオリアクター素子、該素子の製造方法及び使用方法
KR20180005556A (ko) * 2016-07-06 2018-01-16 롯데케미칼 주식회사 수처리 장치

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH04371298A (ja) * 1991-06-20 1992-12-24 Ebara Infilco Co Ltd 有機性汚水の処理方法および装置
JPH07256284A (ja) * 1994-03-18 1995-10-09 Nippon Kentetsu Co Ltd 廃水処理装置における生物接触濾材の逆洗方法および装置
JPH11333496A (ja) * 1998-05-22 1999-12-07 Nissin Electric Co Ltd 窒素除去用微生物保持担体
JP2000218290A (ja) * 1999-02-01 2000-08-08 Kitakyushu City 下水処理方法及び下水処理装置
JP2003033764A (ja) * 2001-07-26 2003-02-04 Ebara Corp オゾンを用いたろ過体の洗浄方法及び装置
JP2003251381A (ja) * 2002-02-28 2003-09-09 Asahi Kasei Corp メンブレンバイオリアクタによる窒素除去方法
JP2009011965A (ja) * 2007-07-06 2009-01-22 Mitsubishi Rayon Eng Co Ltd 中空糸膜モジュールおよびこれを用いた中空糸膜ユニット
JP2010284617A (ja) * 2009-06-15 2010-12-24 Eidensha:Kk バイオリアクター素子、該素子の製造方法及び使用方法
KR20180005556A (ko) * 2016-07-06 2018-01-16 롯데케미칼 주식회사 수처리 장치

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