WO2018168022A1 - Dispositif de traitement biologique aérobie - Google Patents

Dispositif de traitement biologique aérobie Download PDF

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Publication number
WO2018168022A1
WO2018168022A1 PCT/JP2017/033545 JP2017033545W WO2018168022A1 WO 2018168022 A1 WO2018168022 A1 WO 2018168022A1 JP 2017033545 W JP2017033545 W JP 2017033545W WO 2018168022 A1 WO2018168022 A1 WO 2018168022A1
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Prior art keywords
reaction tank
oxygen
biological treatment
mabr
membrane module
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PCT/JP2017/033545
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English (en)
Japanese (ja)
Inventor
東　ひろみ
小林　秀樹
哲朗 深瀬
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栗田工業株式会社
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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
    • B01F21/00—Dissolving
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/40—Static mixers
    • 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
    • C02F3/08—Aerobic processes using moving contact bodies
    • 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
    • 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
    • C02F3/26—Activated sludge processes using pure oxygen or oxygen-rich gas
    • 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 an aerobic biological treatment apparatus suitable for anaerobic biological treatment of organic wastewater containing volatile substances and substances that generate odors, and in particular, water to be treated in a reaction tank using an oxygen-dissolving membrane.
  • the present invention relates to an aerobic biological treatment apparatus that employs a MABR (membrane aeration bioreactor) system in which oxygen is dissolved in the water.
  • MABR membrane aeration bioreactor
  • a multistage reaction tank in which a plurality of reaction tanks are connected in series is used.
  • a part of the remaining odorous substance is volatilized by aeration, and the odor is generated or the toxic substance is volatilized.
  • oxygen is dissolved in the water to be treated by the oxygen-dissolving membrane to perform the aerobic biological treatment.
  • a hollow fiber membrane is often used as in Patent Document 1.
  • the present invention provides an aerobic biological treatment apparatus capable of performing an aerobic biological treatment without generation of odor or volatilization of harmful substances even with organic wastewater containing volatile substances or substances that generate odors. With the goal.
  • the gist of the present invention is as follows.
  • an aerobic biological treatment apparatus that includes first to n-th (n is 2 or more) reaction tanks connected in series and performs aerobic biological treatment in each reaction tank, at least the first reaction tank includes:
  • An aerobic biological treatment apparatus which is a MABR reaction tank in which oxygen is dissolved in water to be treated by an oxygen dissolving film disposed in the reaction tank, and at least the final reaction tank is a reaction tank other than MABR.
  • reaction tank other than the MABR is a sludge floating reaction tank or a carrier flow reaction tank.
  • the reaction tank is a plug flow reaction tank, and the treated water inflow side in the reaction tank is supplied with oxygen by an oxygen-dissolving film.
  • An aerobic biological treatment apparatus characterized in that it is a MABR system that dissolves in water to be treated in a reaction tank, and the treated water outlet side of the reaction tank is a treatment system other than MABR.
  • MABR can dissolve oxygen without the generation of bubbles, so that volatile substances do not escape from the reaction tank into the exhaust.
  • the reaction tank excluding the final stage is designated as MABR
  • the BOD removal tank at the final tank finish is a biological organism other than MABR.
  • FIG. 1 It is a typical longitudinal cross-sectional view of the aerobic biological treatment apparatus of this invention. It is a block diagram of the biological activated carbon processing apparatus used by embodiment. It is a longitudinal cross-sectional view of the biological activated carbon processing apparatus used by embodiment. It is a longitudinal cross-sectional view of the biological activated carbon processing apparatus used by embodiment. It is a longitudinal cross-sectional view of the biological activated carbon processing apparatus used by embodiment. It is a longitudinal cross-sectional view of the biological activated carbon processing apparatus used by embodiment. (A) is a side view of an oxygen supply permeable membrane module, (b) is a perspective view of an oxygen supply permeable membrane module. It is a front view of a hollow fiber membrane module.
  • FIG. 1 It is a perspective view explaining the arrangement
  • A) is a front view which shows the arrangement
  • (b) is the side view. It is a perspective view of a hollow fiber membrane module.
  • the apparatus of the present invention is a substance that generates odors, for example, volatile malodorous substances (22 substances designated by the malodorous prevention method such as ammonia and hydrogen sulfide, etc. discharged from waste disposal plants, sewage treatment plants, and pulp manufacturing plants: “ 4th edition Handbook Odor Prevention Law (August 2001, edited by Odor Law Study Group, published by Gyosei) ”, volatile poisons (vinyl chloride, trichlorethylene, etc.) discharged from vinyl chloride resin manufacturing factories, semiconductor factories It is suitable for treating organic wastewater containing malodorous substances such as methyl sulfide and methyl mercaptan generated in the DMSO decomposition process discharged from the waste water.
  • volatile malodorous substances 22 substances designated by the malodorous prevention method such as ammonia and hydrogen sulfide, etc. discharged from waste disposal plants, sewage treatment plants, and pulp manufacturing plants: “ 4th edition Handbook Odor Prevention Law (August 2001, edited by Odor Law Study Group, published by Gyosei
  • At least the first tank of the multistage reaction tank is a MABR tank
  • at least the final reaction tank is a reaction tank other than MABR.
  • the reaction tank has three or more stages, it is preferable that at least the first tank and the second tank be MABR, and the final tank be a treatment other than MABR, for example, a floating method, a carrier fluidized bed, or the like.
  • a carrier such as sponge is introduced so as to have a volume of 30 to 50%, and a screen for preventing the carrier such as sponge is provided at the outlet of the reaction tank.
  • reaction vessels other than the final reaction vessel be MABR reaction vessels.
  • the proportion of the volatile component in the organic substance is small, it is desirable that about 1/2 of the first half side should be other than MABR and about 1/2 of the second half side should be other than MABR.
  • the 2 tanks on the first half side be MABR and the 2 tanks on the second half side be other than MABR.
  • MABR treatment is effective when the pre-stage reaction tank is heavily loaded. Biofilm formation does not progress in the reaction tank on the downstream side where the processing is progressing and the load is low, so it is more effective to use a carrier method such as a floating method with high contact efficiency with aeration or a fluidized bed. is there.
  • plug flow type reaction vessel In the case of a plug flow type reaction vessel, if the ratio between the width and the length of the reaction vessel is 1:20 or more, plug flow is usually achieved.
  • the plug flow type reaction tank In general, the plug flow type reaction tank is not straight in the length direction, and is often folded back so as to reciprocate 3 or 5 times. Waste water flows in from one end and treated water flows out from the other end.
  • MABR is used for the drainage inflow side and another treatment system is used for the outflow part.
  • Other treatment methods include a carrier fluidized bed in which a sponge is introduced to a volume of 30 to 50% and a screen for preventing sponge outflow is provided in the treated water outflow portion, as described above.
  • FIG. 1 is a schematic longitudinal sectional view of an aerobic biological treatment apparatus 1 according to an example of the present invention.
  • An oxygen-dissolving membrane module 2 is installed in the first reaction tank 3.
  • One or a plurality of oxygen-dissolving membrane modules 2 are installed.
  • the oxygen-dissolving membrane module 2 may be installed in multiple upper and lower stages.
  • Raw water is supplied to the reaction tank 3 through the pipe 4, and the treated water flows through the trough 6 and flows out from the outlet 7.
  • the oxygen-dissolving membrane module 2 includes a non-porous oxygen-dissolving membrane, and oxygen that has permeated through the membrane is dissolved in the water to be treated in the reaction tank 3, so that no bubbles are generated in the reaction tank 3.
  • the air from the blower B is supplied to the oxygen-dissolving membrane module 2 through the pipe 8, and the exhaust gas flowing out from the oxygen-dissolving membrane module 2 is discharged through the pipe 9.
  • Air may flow from the top to the bottom of the oxygen-dissolving membrane module 2, may flow from the bottom to the top, or may flow in the lateral direction.
  • a plurality of oxygen-dissolving membranes When a plurality of oxygen-dissolving membranes are ventilated, they may be ventilated in series or in parallel.
  • a diffuser tube 5 is installed below the oxygen-dissolving membrane module 2, air is intermittently supplied via the pipe 10, and the reaction tank 3 is aerated.
  • the first treated water from the outlet 7 is introduced into the second reaction tank 12 that performs aerobic biological treatment other than MABR, and is further aerobically treated to become second treated water.
  • This second treated water is introduced into the solid-liquid separator 13 and separated into solid and liquid, and then taken out as final treated water. Part of the separated sludge is returned to the reaction tank 3 (or the reaction tanks 3 and 12) via the return pipe 13a.
  • the reaction tank may be a biological activated carbon reaction tank.
  • FIG. 2A is a longitudinal sectional view showing an example of a biological activated carbon treatment reaction tank
  • FIG. 2B is a perspective view of the nozzle.
  • a plurality of oxygen permeable membrane modules 2 are installed in the reaction tank 3 in multiple upper and lower stages.
  • the oxygen permeable membrane module 2 is installed in three stages, but the oxygen permeable membrane module 2 is preferably installed in 2 to 8 stages, particularly 2 to 4 stages.
  • Raw water is supplied to the bottom of the reaction tank 3 through the pipe 14 and the plurality of nozzles 14a to form a fluidized bed F of activated carbon.
  • the treated water that has passed through the fluidized bed F overflows the trough 6 and flows out from the outlet 7.
  • the oxygen permeable membrane module 2 includes a non-porous oxygen permeable membrane, and oxygen that has permeated through the membrane is dissolved in the water to be treated in the reaction tank 3, so that no bubbles are generated in the reaction tank 3.
  • oxygen-containing gas such as air from the blower B is supplied to the upper part of the lowermost oxygen permeable membrane module 2 c through the pipe 8, flows out from the lower part of the oxygen permeable membrane module 2 c, and passes through the pipe 19.
  • oxygen permeable membrane module 2b in the second stage flows out from the lower part of the oxygen permeable membrane module 2b, and is supplied to the upper part of the uppermost oxygen permeable membrane module 2a through the pipe 20.
  • the gas flowing out from the lower part of the oxygen permeable membrane module 2b is discharged through the pipe 21.
  • the oxygen permeable membrane module 2 exists over substantially the entire vertical direction of the activated carbon fluidized bed F. Moreover, it is preferable that the oxygen permeable membrane module 2 is arranged evenly in the whole area in the reaction tank 3 in the plan view of the reaction tank 3.
  • raw water is discharged from the plurality of nozzles 14 a to the bottom of the reaction tank 3.
  • a water permeable plate 22 such as a punching metal is disposed at the bottom of the reaction tank 3.
  • the raw water flows out from the pipe 14 into the receiving chamber 25 below the water permeable plate 22 through the nozzle 26, passes through the water permeable plate 22, the large particle layer 23, and the small particle layer 24, and into the reaction tank 3 is a fluidized bed of activated carbon. F is formed. Note that a water-permeable plate such as punching metal is not necessary.
  • the oxygen-containing gas from the blower B is supplied to the upper part of the lowermost oxygen permeable membrane module 2c through the pipe 8, flows out from the lower part, and the second stage oxygen from the lower part. It is supplied to the lower part of the permeable membrane module 2b, flows out from the upper part thereof, is then supplied to the lower part of the uppermost oxygen permeable membrane module 2a, and is discharged from the upper part through the pipe 21.
  • the oxygen-containing gas from the blower B is supplied to the lower part of the lowermost oxygen permeable membrane module 2c through the pipe 8, flows out from the upper part, and the second stage oxygen from the lower part. It is supplied to the lower part of the permeable membrane module 2b, flows out from the upper part thereof, is then supplied to the lower part of the uppermost oxygen permeable membrane module 2a, and is discharged from the upper part through the pipe 21.
  • the oxygen-containing gas flows in parallel to the oxygen permeable membrane modules 2a to 2c. That is, the oxygen-containing gas from the blower B is supplied to the upper part of each oxygen permeable membrane module 2 a, 2 b, 2 c through the pipe 8, flows out from the lower part of each, and is discharged through the pipe 21.
  • the oxygen-containing gas is supplied to the upper part of the lowermost oxygen permeable membrane module 2c, flows out from the lower part of the oxygen permeable membrane module 2c, and then flows into the upper oxygen permeable membrane modules 2b and 2a.
  • the condensed water in the oxygen permeable membrane module 2c is easy to escape.
  • the condensed water in the oxygen permeable membrane module easily evaporates.
  • the condensed water is easily evaporated.
  • the oxygen supply amount according to the load can be obtained by increasing the oxygen-containing gas flow rate in the lower oxygen permeable membrane module.
  • the oxygen permeable membrane module on the upper side may have a smaller membrane area or lower membrane packing density.
  • the bottom structure having the water permeable plate 22, the large particle layer 23, and the small particle layer 24 may be used as shown in FIG.
  • the oxygen permeable membrane of the oxygen permeable membrane module 2 may be any of a hollow fiber membrane, a flat membrane, and a spiral membrane, but a hollow fiber membrane is preferable.
  • a hollow fiber membrane is preferable.
  • a composite film having a high strength and a porous hollow fiber coated with a nonporous polymer may be used.
  • the hollow fiber membrane preferably has an inner diameter of 0.05 to 4 mm, particularly 0.2 to 1 mm, and a thickness of 0.01 to 0.2 mm, particularly 0.02 to 0.1 mm. If the inner diameter is smaller than this, the aeration pressure loss is large, and if it is larger, the surface area becomes smaller and the oxygen dissolution rate decreases. When the thickness is smaller than the above range, the physical strength is reduced and the film is easily broken. On the other hand, when the thickness is larger than the above range, the oxygen permeation resistance increases and the oxygen dissolution efficiency decreases.
  • the length of the hollow fiber membrane is preferably about 0.5 to 3 m, particularly preferably about 1 to 2 m. If the hollow fiber membrane is too long, when a large amount of biofilm adheres, problems such as breakage, solidification into a dumpling, a decrease in surface area, a decrease in oxygen dissolution efficiency, and an increase in pressure loss occur. If the hollow fiber membrane is too short, the cost increases. For the same reason, the length of the flat membrane and the spiral membrane is preferably 0.5 to 1.5 m.
  • the required area of the membrane is sufficient to supply the amount of oxygen necessary for processing.
  • a hollow fiber membrane made of silicon having a thickness of 100 ⁇ m requires 240 m 2 or more per 1 m 3 of the volume of the activated carbon part flowing.
  • the area of the membrane is preferably 300 m 2 or more and 1000 m 2 / m 3 or less per tank volume. If the membrane area is large, the amount of oxygen supply increases and a high load is possible, but the membrane cost increases. If the membrane area per unit volume is too large, the membrane will be in a dumpling state and efficiency will be reduced.
  • the membrane is preferably installed in the flow direction. For example, in a tank with a water depth of 10 m, it is preferable to install a 2 m long membrane in four stages up and down.
  • the oxygen permeable membrane module 30 in FIG. 7 uses a hollow fiber membrane 27 as an oxygen permeable membrane.
  • the hollow fiber membranes 27 are arranged in the vertical direction, and the upper end of each hollow fiber membrane 27 is connected to the upper header 28 and the lower end is connected to the lower header 29.
  • the inside of the hollow fiber membrane 27 communicates with the upper header 28 and the lower header 29, respectively.
  • Each header 28, 29 is a hollow tube, and a plurality of headers 28, 29 are arranged in parallel in a substantially horizontal direction. Even when a flat film or a spiral film is used, they are arranged in the vertical direction.
  • each header 28 is connected to the manifold 28A, and one end or both ends of each header 29 are connected to the manifold 29A.
  • oxygen-containing gas is supplied to the upper part of the oxygen permeable membrane module 30 and discharged from the lower part of the oxygen permeable membrane module 30, the oxygen-containing gas flows from the upper header 28 through the hollow fiber membrane 27 to the lower header 29, Oxygen permeates through the hollow fiber membrane 27 and dissolves in the water in the reaction vessel 3.
  • oxygen-containing gas is supplied to the lower part of the oxygen permeable membrane module 30 and discharged from the upper part, the oxygen-containing gas is supplied to the lower header 29 and is discharged from the upper header 28 through the hollow fiber membrane 27.
  • FIG. 8 is a front view showing an example of the oxygen permeable membrane module 30 arranged in the frame 32.
  • the frame 32 has four pillars 32a erected at the four corners, an upper beam 32b erected between the upper ends of the pillars 32a, and a lower erection between lower parts of the pillars 32a. It has the beam 32c and the base plate 32d attached to the lower end surface of each pillar 32a.
  • the oxygen permeable membrane module 30 provided with the frame 32 can be easily installed in the reaction tank 3 in upper and lower stages. That is, the upper oxygen permeable membrane module 30 can be disposed on the frame 32 of the lower oxygen permeable membrane module 30 so that the bottom seat plate 32d of the upper oxygen permeable membrane module 30 is placed thereon.
  • a hollow fiber membrane module in which hollow fiber membranes are arranged in the vertical direction is a membrane module having a low height of about 1 to 2 m, and is laminated in two or more stages, preferably four or more stages. To do.
  • oxygen can be dissolved at a low pressure by stacking hollow fiber membrane modules in which the length of the hollow fiber membrane is shortened and the height is lowered in multiple stages.
  • the pressure of the oxygen-containing gas blown to the hollow fiber membrane is preferably a pressure slightly higher than the pressure loss of the hollow fiber membrane, for example, about 5 to 20% higher from the viewpoint of cost.
  • the pressure supplied to the hollow fiber membrane may be determined regardless of the water depth. Since a normal air diffuser requires a pressure higher than the water depth, the present invention is more advantageous as the water depth of the reaction vessel is deeper.
  • the hollow fiber membrane 27 is in the vertical direction, and the raw water (treated water) flows in the vertical direction along the hollow fiber membrane 27.
  • the oxygen permeable membrane module an oxygen permeable membrane module having a horizontal X-direction hollow fiber membrane 27b and a vertical (Z-direction) hollow fiber membrane 27a as shown in FIG. 9 may be used.
  • the hollow fiber membranes 27a and 27b may be braided into a plain weave.
  • FIG. 11 is a perspective view showing an example of an oxygen permeable membrane module including the hollow fiber membranes 27 (27a, 27b) in the X and Z directions.
  • the oxygen permeable membrane module 40 includes a pair of parallel headers 41, 41 extending in the Z direction, a pair of headers 42, 42 extending in the X direction orthogonal thereto, and the hollow fiber membrane 27.
  • the hollow fiber membrane 27 in the X direction is constructed between the headers 41 and 41
  • the hollow fiber membrane 27 in the Z direction is constructed between the headers 42 and 42.
  • the end portions of the headers 41 and 42 are connected to each other, so that the headers 41 and 42 have a rectangular frame shape.
  • closing members such as end plugs are provided inside both ends of the headers 41 and 42, and the headers 41 and 42 are blocked.
  • the oxygen-containing gas is supplied to one header 41, passes through the hollow fiber membrane 27, and flows into the other header 41.
  • the oxygen-containing gas is supplied to one header 42, passes through the hollow fiber membrane 27, and flows into the other header 42.
  • one one header 41 and one one header 42 communicate with each other.
  • the other one header 41 and the other one header 42 communicate with each other.
  • a closing member such as an end plug is provided inside the connecting portion of the one header 41, 42 and the other header 41, 42, and the one header 41, 42 and the other header 41, 42 are connected to each other.
  • the headers 41 and 42 are blocked.
  • the oxygen-containing gas is supplied to the one header 41, 42, passes through the hollow fiber membrane 27, and flows into the other header 41, 42.
  • These hollow fiber membranes are one by one in FIGS. 7 to 11, but may be bundles of several to 100.
  • An aeration device may be installed in the lower part of the reaction tank.
  • Activated carbon is suitable as the biological carrier.
  • the filling amount of the activated carbon is preferably about 40 to 60%, particularly about 50% of the volume of the reaction tank.
  • the larger the filling amount the greater the amount of biomass and the higher the activity. Accordingly, it is preferable to pass water through an LV in which the activated carbon phase expands by about 20 to 50% when the filling amount is about 50%.
  • the water flow LV is about 7 to 15 m / hr with 0.5 mm activated carbon.
  • Gels other than activated carbon, porous materials, non-porous materials, and the like can be used under similar conditions. For example, polyvinyl alcohol gel, polyacrylamide gel, polyurethane foam, calcium alginate gel, zeolite, plastic and the like can also be used.
  • activated carbon when activated carbon is used as the carrier, it is possible to remove a wide range of pollutants by the interaction between the activated carbon adsorption and biodegradation.
  • the average particle diameter of the activated carbon is preferably about 0.2 to 3 mm.
  • the average particle size is large, it is possible to achieve a high LV, and the amount of circulation can be increased, so that a high load is possible.
  • the surface area is small, the biomass is reduced. If the average particle size is small, the pump power can be reduced because it can flow at a low LV. And since the surface area is large, the amount of attached organisms increases.
  • the optimum particle size is determined by the concentration of waste water, and is preferably about 0.2 to 0.4 mm when TOC is 50 mg / L, and about 0.6 to 1.2 mm when TOC is 10 mg / L.
  • the expansion ratio of activated carbon is preferably about 20 to 50%. If the expansion rate is lower than 20%, there is a possibility of clogging and short circuit. If the expansion rate is higher than 50%, there is a risk of outflow and the pump power cost becomes high.
  • the expansion rate of the activated carbon fluidized bed is about 10 to 20%.
  • the membrane installed at the same time is rubbed by activated carbon and worn out.
  • the activated carbon needs to flow sufficiently, and the expansion rate is desirably 20% or more.
  • the particle size of the activated carbon is preferably smaller than that of normal biological activated carbon.
  • the activated carbon may be anything from coconut charcoal, coal, charcoal and the like.
  • the shape is preferably spherical charcoal, but may be ordinary granular charcoal or crushed charcoal.
  • the oxygen-containing gas may be a gas containing oxygen, such as air, oxygen-enriched air, or pure oxygen. It is desirable that the gas to be vented pass through a filter to remove fine particles.
  • the aeration rate is preferably about twice the amount of oxygen required for biological reactions. If it is less than this, BOD and ammonia will remain in the treated water due to insufficient oxygen, and if it is greater, the air flow will be unnecessarily increased and the pressure loss will be increased, so the economy will be impaired.
  • the aeration pressure is slightly higher than the pressure loss of the hollow fiber generated at a predetermined aeration amount.
  • Flow rate of treated water It is preferable that the flow rate of the water to be treated is LV10 m / hr or more, and the treatment water is not circulated and treated in one pass.
  • the oxygen dissolution rate is increased proportionally.
  • oxygen dissolves about twice as much as 10 m / hr.
  • the optimum LV range is about 10 to 30 m / hr.
  • the residence time is preferably set so that the tank load is 1 to 2 kg-TOC / m 3 / day.
  • the blower it is sufficient that the discharge wind pressure is equal to or lower than the water pressure coming from the water depth. However, it is necessary to be more than the pressure loss of piping. Usually, the pipe resistance is about 1 to 2 kPa.
  • a general purpose blower having a pressure of 0.5 MPa or less can be used even at a water depth of 5 m or more, and a low pressure blower of 0.1 MPa or less is preferably used.
  • the supply pressure of the oxygen-containing gas is higher than the pressure loss of the hollow fiber membrane, lower than the water depth pressure, and that the membrane is not crushed by water pressure. Since the pressure loss of the flat membrane and the spiral membrane is negligible compared to the water pressure, the pressure is very low, about 5 kPa or more, water pressure or less, preferably 20 kPa or less.
  • the pressure loss varies depending on the inner diameter and length. Since the amount of air to be vented is 20 mL to 100 mL / day per m 2 of membrane, the amount of air doubles when the membrane length is doubled, and the amount of air is only doubled even when the membrane diameter is doubled. Don't be. Therefore, the pressure loss of the membrane is directly proportional to the membrane length and inversely proportional to the diameter.
  • the value of pressure loss is about 3 to 20 kPa for hollow fibers having an inner diameter of 50 ⁇ m and a length of 2 m.
  • the oxygen dissolution efficiency is preferably 30 to 100%, particularly 40 to 60%.
  • the fluidized bed F of the carrier is formed, but the carrier may be suspended.
  • the carrier is preferably suspended or fluidized by one or more of aeration of the liquid in the reaction vessel, flow of the liquid, and mechanical operation.
  • the MLSS concentration in the reaction tank is preferably maintained at 10,000 to 50,000 mg / L, particularly preferably 20,000 to 30,000 mg / L.
  • a filtration membrane in the treatment liquid in the reaction tank and take out the permeated water of this filtration membrane as the treatment water.
  • Example 1 Semiconductor cleaning wastewater containing DMSO 3.2% was passed through with a TOC tank load of 1.2 kg / m 3 / D, a water tank capacity of 10 L, and a residence time of 24 hours.
  • Odor (DMS) measurement was carried out 10 days, 20 days and 21 days after water flow. In any measurement, it was below the DMS lower limit (0.25 mg / L) of the detection tube. In addition, by performing biological treatment (standard activated sludge treatment method) at the subsequent stage, it was possible to further reduce low-load organic matter. The odor measurement was performed using a gas tube pyrotube detector tube.

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  • Chemical & Material Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Microbiology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Dispersion Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Activated Sludge Processes (AREA)
  • Aeration Devices For Treatment Of Activated Polluted Sludge (AREA)
  • Biological Treatment Of Waste Water (AREA)

Abstract

L'invention concerne un dispositif de traitement biologique aérobie qui comprend un premier réservoir de réaction 3 et un second réservoir de réaction 12 qui sont connectés en série, un traitement biologique aérobie étant effectué dans chacun des réservoirs de réaction 3, 12, le premier réservoir de réaction 3 étant un réservoir de réaction MABR dans lequel de l'oxygène est dissous dans de l'eau de traitement par un module de membrane de dissolution d'oxygène 2 disposé à l'intérieur du réservoir de réaction 3, et le second réservoir de réaction 12 étant un réservoir de réaction d'un type différent du MABR.
PCT/JP2017/033545 2017-03-16 2017-09-15 Dispositif de traitement biologique aérobie WO2018168022A1 (fr)

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JP2019141783A (ja) * 2018-02-20 2019-08-29 栗田工業株式会社 好気性生物処理装置
JP2021000607A (ja) * 2019-06-21 2021-01-07 栗田工業株式会社 生物処理装置の運転方法

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JP7437139B2 (ja) * 2019-11-19 2024-02-22 住友重機械エンバイロメント株式会社 水処理装置及び水処理方法
CN112142192B (zh) * 2020-09-08 2021-12-21 同济大学 一种膜载生物除臭反应器及除臭方法

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JP2019141783A (ja) * 2018-02-20 2019-08-29 栗田工業株式会社 好気性生物処理装置
WO2019163426A1 (fr) * 2018-02-20 2019-08-29 栗田工業株式会社 Dispositif de traitement d'organisme aérobie
JP2021000607A (ja) * 2019-06-21 2021-01-07 栗田工業株式会社 生物処理装置の運転方法
JP7283253B2 (ja) 2019-06-21 2023-05-30 栗田工業株式会社 生物処理装置の運転方法

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