WO2017098941A1 - 生物処理装置 - Google Patents

生物処理装置 Download PDF

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Publication number
WO2017098941A1
WO2017098941A1 PCT/JP2016/085143 JP2016085143W WO2017098941A1 WO 2017098941 A1 WO2017098941 A1 WO 2017098941A1 JP 2016085143 W JP2016085143 W JP 2016085143W WO 2017098941 A1 WO2017098941 A1 WO 2017098941A1
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WO
WIPO (PCT)
Prior art keywords
water
biological treatment
tank
membrane
side space
Prior art date
Application number
PCT/JP2016/085143
Other languages
English (en)
French (fr)
Japanese (ja)
Inventor
誠人 尾田
寿生 萩本
水谷　洋
Original Assignee
三菱重工環境・化学エンジニアリング株式会社
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
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Application filed by 三菱重工環境・化学エンジニアリング株式会社 filed Critical 三菱重工環境・化学エンジニアリング株式会社
Priority to MYPI2018700185A priority Critical patent/MY185893A/en
Priority to CN201680043796.6A priority patent/CN107848850A/zh
Priority to KR1020187001543A priority patent/KR102167816B1/ko
Priority to SG11201800356WA priority patent/SG11201800356WA/en
Publication of WO2017098941A1 publication Critical patent/WO2017098941A1/ja

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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
    • 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
    • B01D63/06—Tubular membrane modules
    • 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
    • C02F3/006—Regulation methods for biological treatment
    • 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
    • C02F3/28—Anaerobic digestion 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
    • C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/002—Construction details of the apparatus
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/03—Pressure
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/42—Liquid level
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • 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 biological treatment apparatus having a biological treatment water tank for treating organic substances contained in treated water such as human waste.
  • membrane separation such as MF (microfiltration) and UF (ultrafiltration) for solid-liquid separation.
  • MF microfiltration
  • UF ultrafiltration
  • the membrane separation device a plurality of membrane modules including a cylindrical casing and a plurality of tubular filtration membranes (hollow fiber membranes) accommodated in the casing are used, and raw water is circulated inside the tubular filtration membrane.
  • An apparatus using a filtration method is known (for example, see Patent Document 1).
  • the permeated water that has permeated through the tubular filtration membrane is sucked by a suction pump and stored in a storage tank, for example, and used as appropriate.
  • a membrane separation apparatus using a tubular filtration membrane suppresses sludge accumulation on the membrane, and in order to secure FLUX (permeate flow rate), the membrane surface flow rate (the rate at which the raw water flows inside the tubular filtration membrane) )
  • FLUX permeate flow rate
  • the membrane surface flow rate the rate at which the raw water flows inside the tubular filtration membrane
  • the membrane surface flow velocity is set to 2.5 m / s.
  • the flow rate of the circulating water that circulates through the water treatment system including the membrane separation device increases by increasing the membrane surface flow velocity, so that a tank for temporarily storing the circulating water is essential. It was.
  • This invention provides the biological treatment apparatus which can aim at reduction of installation cost by making the tank for storing circulating water unnecessary.
  • the biological treatment apparatus has a single-layer structure in which a biological treatment water tank for treating an organic substance contained in water to be treated, a casing, and a hydrophilic monomer are copolymerized, A membrane separator having a tubular filtration membrane that divides the casing into a concentrated side space to which effluent water flowing out from the biological treatment water tank is supplied and a permeate side space in which permeated water separated from the effluent water is accommodated.
  • a pressurizing pump that pressurizes the effluent water and supplies it to the concentrated side space, a suction pump that sucks the permeated water from the permeate side space, a pressure gauge that measures the pressure of the permeate side space, A return line for returning the concentrated water to the biological treatment water tank, and a control device for controlling a supply amount of the effluent by the pressurizing pump based on a measurement value of the pressure gauge.
  • the membrane surface flow velocity can be lowered because the tubular filtration membrane has hydrophilicity.
  • the circulating flow volume of to-be-processed water can be decreased, and the tank for temporarily storing a lot of circulating water becomes unnecessary.
  • the concentrated water (return sludge) can be stably supplied to the biological treatment water tank.
  • control device may increase the flow rate of the effluent water pressurized by the pressure pump when the absolute value of the measurement value of the pressure gauge is larger than a threshold value.
  • control device may control a flow rate of the permeated water sucked by the suction pump. According to such a configuration, the increased flow rate of the outflow water can be compensated.
  • the biological treatment apparatus includes an excess sludge discharge unit that draws excess sludge from the return line, and a water level measurement device that measures the water level of the biological treatment water tank, and the control device uses the measured value of the water level measurement device. Based on this, the amount of excess sludge drawn out from the excess sludge discharge section may be controlled.
  • the biological treatment apparatus includes a water level measurement device that measures a water level of the biological treatment water tank, and the control device determines a flow rate of water to be treated supplied to the biological treatment water tank based on a measurement value of the water level measurement device. You may control.
  • the biological treatment water tank may be a methane fermentation tank that decomposes organic matter contained in the water to be treated by microorganisms.
  • the energy of methane gas can be used for power generation and the like by efficiently recovering methane gas generated by methane fermentation.
  • the membrane surface flow rate can be lowered because the tubular filtration membrane has hydrophilicity.
  • the circulating flow volume of to-be-processed water can be decreased, and the tank for temporarily storing a lot of circulating water becomes unnecessary.
  • the concentrated water (return sludge) can be stably supplied to the biological treatment water tank.
  • the biological treatment apparatus 10 includes a biological treatment water tank 11 for treating organic substances contained in the water to be treated W1 (organic wastewater including human waste and septic tank sludge), and the biological treatment water tank 11.
  • a membrane separation device 13 that separates the outflow water W2 into the permeate water PW and the concentrated water W3, and a control device 12 are provided.
  • the biological treatment water tank 11 is a device that decomposes and removes BOD, nitrogen compounds and the like in the liquid by the action of nitrifying bacteria and denitrifying bacteria.
  • the biological treatment water tank 11 is supplied with the treated water W ⁇ b> 1 through the treated water pipe 15.
  • the biological treatment water tank 11 of this embodiment uses a circulation type nitrification denitrification method.
  • the biological treatment water tank 11 has a configuration in which a denitrification tank 24, a nitrification tank 25, a secondary denitrification tank 26, and a re-aeration tank 27 are sequentially arranged in series.
  • the biological treatment water tank 11 has a circulation line 29 for circulating a part of the water to be treated W1 discharged from the nitrification tank 25 to the denitrification tank 24 as a circulation liquid.
  • the biological treatment water tank 11 includes a water level measuring device 56 that measures the water level of any of the tanks that constitute the biological treatment water tank 11.
  • the water level measuring device 56 of the present embodiment is provided in the re-aeration tank 27. Further, the water level measuring device 56 electrically transmits the measured water level value to the control device 12.
  • the denitrification tank 24 is an apparatus in which the inside of the tank is maintained in an anaerobic state, and in the presence of an organic carbon source, oxidized nitrogen such as nitrate nitrogen and nitrite nitrogen is reduced to nitrogen gas mainly by the action of denitrifying bacteria. is there. If necessary, an organic carbon source may be externally added.
  • the denitrification tank 24 includes an ORP measurement device 51 (51A) that measures an oxidation-reduction potential (ORP) of the water to be treated W1 flowing into the denitrification tank 24, and a hydrogen ion index (pH) of the water to be treated W1.
  • ORP oxidation-reduction potential
  • PH hydrogen ion index
  • the nitrification tank 25 is an apparatus that aerates air into the treatment liquid in the tank and oxidizes ammonia nitrogen in the treatment liquid to oxidized nitrogen mainly by the action of nitrate bacteria under aerobic conditions.
  • the nitrification tank 25 includes an aeration apparatus 57 (57B) that aerates air into the treatment liquid in the tank, and a DO measurement apparatus that measures the dissolved oxygen concentration (Dissolved Oxygen, DO) of the water to be treated W1 flowing into the nitrification tank 25.
  • 53 53
  • a pH measuring device 52 52B
  • the secondary denitrification tank 26 is an apparatus in which the inside of the tank is maintained in an anaerobic state and the oxidized nitrogen remaining in the treatment liquid is reduced to nitrogen gas by the addition of an organic carbon source such as methanol.
  • the secondary denitrification tank 26 has an ORP measurement device 51 (51C) and a pH measurement device 52 (52C). Further, the secondary denitrification tank 26 is provided with an organic carbon source supply device 54 for injecting an organic substance such as methanol, which becomes an organic carbon source for the denitrification reaction.
  • the re-aeration tank 27 is an apparatus that is maintained in an aerobic condition by aeration of air and mainly oxidizes ammonia nitrogen remaining in the treatment liquid to oxidized nitrogen.
  • the re-aeration tank 27 includes an aeration device 57 (57D) and a DO measurement device 53 (53D) that measures a dissolved oxygen concentration.
  • the control device 12 performs aeration based on the dissolved oxygen concentration value measured by the DO measurement device 53, the oxidation-reduction potential value measured by the ORP measurement device 51, and the pH value measured by the pH measurement device 52.
  • the device 57 is controlled. Specifically, the ORP measurement device 51, the pH measurement device 52, and the DO measurement device 53 transmit each measurement value as an electrical signal to the control device 12, and the control device 12 that has received these measurement values converts the measurement values into those measurement values. Based on this, the aeration air volume of the aeration device 57 is increased or decreased, and the dissolved oxygen concentration, oxidation-reduction potential, and pH values are adjusted within predetermined ranges.
  • control the oxidation-reduction potential it is preferable to control the oxidation-reduction potential to be 10 mV to 50 mV in order to suppress air lock (a phenomenon in which bubbles hinder the flow) in the tubular filtration membrane 3 which will be described later and sludge dismantling. Since the control device 12 also adjusts the pH, it is possible to prevent the nitrification / denitrification reaction from being hindered due to the low pH.
  • the membrane separation device 13 includes a plurality of membrane modules 1. As shown in FIG. 2, the membrane module 1 has a casing 2 and a plurality of tubular filtration membranes 3 arranged inside the casing 2.
  • the membrane separation device 13 is a device that takes out the permeated water PW from the effluent water W2 using a method of filtering while circulating the effluent water W2 inside the tubular filtration membrane 3.
  • the tubular filtration membrane 3 partitions the casing 2 into a concentrated side space S to which the effluent water W2 is supplied and a permeate side space P in which the permeated water PW separated from the effluent water W2 is accommodated.
  • the biological treatment water tank 11 and the membrane separation device 13 are connected by an effluent water supply pipe 17. That is, the effluent water W ⁇ b> 2 is introduced into the membrane separation device 13 through the effluent water supply pipe 17.
  • the effluent water supply pipe 17 is provided with a pressurizing pump 21.
  • the effluent water W2 flowing out from the biological treatment water tank 11 is supplied to the membrane separation device 13 while being pressurized by the pressurizing pump 21.
  • the permeated water PW separated from the membrane separation device 13 is introduced into the permeated water pipe 18.
  • the permeated water pipe 18 is connected to the storage tank 20. That is, the permeate outlet 9 (see FIG. 2) of the membrane module 1 is connected to the permeate pipe 18.
  • the permeate pipe 18 is provided with a suction pump 22 that makes the permeate side space P negative.
  • the permeate pipe 18 is provided with a pressure gauge 23 for measuring the pressure (water pressure) in the permeate side space P. The pressure value measured by the pressure gauge 23 is electrically transmitted to the control device 12 and processed as described later.
  • the concentrated water W3 separated from the permeated water PW and discharged from the membrane separation device 13 is returned to the biological treatment water tank 11 through the return pipe 19 (return line) as the activated sludge, with the exception of excess sludge M. That is, the concentrated water discharge port 8 (see FIG. 2) of the membrane module 1 is connected to the return pipe 19. From the return pipe 19, an excess sludge pipe 28 (surplus sludge discharge part) for branching out a part of the concentrated water W3 (activated sludge) as excess sludge M is branched.
  • the excess sludge pipe 28 is provided with an excess sludge adjusting device 67 (for example, a pump or a valve) that adjusts the flow rate of the excess sludge M.
  • a flow meter 66 is arranged in the return pipe 19 between the branch point and the concentrated water discharge port 8.
  • the anemometer 66 electrically transmits the measured value of the flow rate of the concentrated water W3 to the control device 12.
  • the effluent water W2 flowing out from the biological treatment water tank 11 returns to the biological treatment water tank 11 via the membrane separator 13. That is, the to-be-processed water W1 circulates through the piping of the biological treatment apparatus 10.
  • the plurality of membrane modules 1 are arranged in parallel. Specifically, the effluent water supply pipe 17, the permeate water pipe 18, and the return pipe 19 are connected to each membrane module 1.
  • the membrane module 1 includes a cylindrical casing 2 and a plurality of tubular filtration membranes 3.
  • the casing 2 is formed above the casing body 4, the casing body 4 having a cylindrical shape, the first side wall 5 that closes the upper end of the casing body 4, the second side wall 6 that closes the lower end of the casing body 4, and the casing body 4. It has an effluent water introduction port 7, a concentrated water discharge port 8 formed below the casing body 4, and a permeate discharge port 9 formed in the casing body 4.
  • the membrane module 1 of the present embodiment is configured such that the effluent water W2 introduced into the tubular filtration membrane 3 from above flows downward in the tubular filtration membrane 3.
  • the membrane module 1 includes a first partition wall 30 and a second partition wall 31 that divide the inside of the casing 2 into three spaces.
  • a plurality of insertion holes 32 are formed in the first partition wall 30 and the second partition wall 31.
  • the insertion hole 32 is a hole that penetrates the first partition wall 30 and the second partition wall 31 in the plate thickness direction.
  • the inner diameter of the insertion hole 32 is slightly larger than the outer diameter of the tubular filtration membrane 3.
  • the plurality of tubular filtration membranes 3 extend in the axis A direction in the casing 2, in the vertical direction in the present embodiment, one end (first end) is connected to the first partition wall 30, and the other end (second end). ) Is connected to the second partition wall 31.
  • the first partition 30 is a plate-shaped member, and is fixed above the extending direction of the casing 2 (on the side of the first side wall 5).
  • a space surrounded by the casing body 4, the first partition wall 30, and the first side wall 5 is a first header space S1.
  • the first header space S1 is a space above the first partition wall 30 in the internal space of the casing 2.
  • the second partition wall 31 is a plate-shaped member, and is fixed below the extending direction of the casing 2 (on the second side wall 6 side).
  • a space surrounded by the casing body 4, the second partition wall 31, and the second side wall 6 is a second header space S2.
  • the second header space S ⁇ b> 2 is a space below the second partition wall 31 in the internal space of the casing 2.
  • the space surrounded by the casing body 4, the first partition wall 30, and the second partition wall 31 and on the outer peripheral side of the tubular filtration membrane 3 is a permeation side space P.
  • the permeated water PW taken out from the plurality of tubular filtration membranes 3 is discharged into the permeate side space P, and then introduced into the permeate water pipe 18 (see FIG. 1) through the permeate discharge port 9.
  • the effluent water introduction port 7 is an opening that allows communication between the outside of the casing 2 and the first header space S1.
  • the effluent water inlet 7 is formed in the casing body 4.
  • the effluent water introduction port 7 is provided between the first partition wall 30 and the first side wall 5 in the axis A direction of the casing 2.
  • the concentrated water discharge port 8 is an opening that allows communication between the outside of the casing 2 and the second header space S2.
  • the concentrated water discharge port 8 is formed in the casing body 4.
  • the concentrated water discharge port 8 is provided between the second partition wall 31 and the second side wall 6 in the axis A direction of the casing 2.
  • the permeate discharge port 9 is an opening that allows the outside of the casing 2 and the permeate side space P to communicate with each other.
  • the permeated water discharge port 9 is formed in the casing body 4.
  • the permeate discharge port 9 is provided between the first partition wall 30 and the second partition wall 31 in the axis A direction of the casing 2.
  • the permeate discharge port 9 is provided in the lower part of the permeate side space P. In other words, the permeated water discharge port 9 is provided slightly above the second partition wall 31.
  • the permeate discharge port 9 is preferably provided at the lower end of the permeate side space P.
  • the permeate discharge port 9 is formed at a position where the permeate PW that has permeated through the plurality of tubular filtration membranes 3 can be discharged as much as possible without staying in the permeate side space P. Moreover, the permeated water pipe 18 connected to the permeated water discharge port 9 is inclined downward. That is, the permeated water pipe 18 has a shape such that the permeated water PW discharged from the permeated water discharge port 9 does not return due to gravity.
  • the casing body 4 is provided with an openable / closable air vent 33 for communicating the outside of the casing 2 and the transmission side space P.
  • the air vent 33 is provided in the upper part of the transmission side space P.
  • the concentration side space S is a space into which the effluent water W2 is introduced, and is a first header space S1, a filtration membrane inner space S3 that is a space on the inner peripheral side of the tubular filtration membrane 3, and a second header space S2.
  • the permeate side space P is a space in which the permeate PW separated from the outflow water W2 is accommodated.
  • each tubular filtration membrane 3 is inserted into the insertion hole 32 of the first partition wall 30 and then fixed to the inner peripheral surface of the insertion hole 32.
  • a space between the inner peripheral surface of the insertion hole 32 and the outer peripheral surface of the tubular filtration membrane 3 is sealed with a sealing material (not shown).
  • a sealing material a material that has an initial viscosity and hardens with time, such as an epoxy resin or a urethane resin, is preferable.
  • the second end of each tubular filtration membrane 3 is fixed to the insertion hole 32 of the second partition wall 31 in the same manner as the first end of the tubular filtration membrane 3.
  • the tubular filtration membrane 3 has a cylindrical shape, and is formed of a polymer filtration membrane having a single layer structure in which a hydrophilic monomer is copolymerized on a single main constituent material. That is, the tubular filtration membrane 3 is formed of a single material as a main material. That the main material is formed of one kind of material means that one kind of resin accounts for 50% by mass or more in the material (for example, resin) forming the tubular filtration membrane 3. The fact that the main material is formed of one kind of material means that the nature of the one kind of material dominates the nature of the constituent material. Specifically, it means a material in which one kind of resin has 50 mass% to 99 mass%.
  • the main materials constituting the tubular filtration membrane 3 include polyolefin chlorides such as vinyl chloride resin, polysulfone (PS), polyvinylidene fluoride (PVDF), polyethylene (PE), polyacrylonitrile (PAN), and polyether.
  • Polymer materials such as sulfone, polyvinyl alcohol (PVA), and polyimide (PI) can be used.
  • a vinyl chloride resin is particularly preferable.
  • vinyl chloride resins include vinyl chloride homopolymer (vinyl chloride homopolymer), a copolymer of a monomer having an unsaturated bond copolymerizable with vinyl chloride monomer and vinyl chloride monomer, and vinyl chloride monomer in the polymer.
  • vinyl chloride resins include graft copolymers obtained by graft copolymerization, and (co) polymers composed of chlorinated vinyl chloride monomer units.
  • hydrophilic monomers examples include: (1) A cationic group-containing vinyl monomer such as an amino group, an ammonium group, a pyridyl group, an imino group or a betaine structure and / or a salt thereof, (2) Hydrophilic nonionic group-containing vinyl monomers such as hydroxyl groups, amide groups, ester structures, ether structures, (3) Anionic group-containing vinyl monomer such as carboxyl group, sulfonic acid group, phosphoric acid group and / or salt thereof, (4) Other monomers may be mentioned.
  • a cationic group-containing vinyl monomer such as an amino group, an ammonium group, a pyridyl group, an imino group or a betaine structure and / or a salt thereof
  • Hydrophilic nonionic group-containing vinyl monomers such as hydroxyl groups, amide groups, ester structures, ether structures
  • Anionic group-containing vinyl monomer such as carboxyl group, sulfonic acid group, phosphoric acid
  • the tube diameter of the tubular filtration membrane 3 can be selected as appropriate depending on the properties of the effluent water W2. For example, when the coarse fiber amount ⁇ is 200 mg / liter or less for the effluent water W2, the inner diameter of the tubular filtration membrane 3 is 5 mm.
  • the inner diameter of the tubular filtration membrane 3 is 5 mm-10 mm, and when the coarse fiber amount ⁇ is 500 mg / liter or more, the inner diameter of the tubular filtration membrane 3 is Can be 10 mm or more.
  • To-be-treated water W1 such as human waste is pretreated by a pretreatment facility (not shown) and then sent to the biologically treated water tank 11 through the to-be-treated water pipe 15.
  • the treated water W1 is treated in the biological treatment water tank 11.
  • the organic substance contained in the for-treatment water W1 is decomposed by microorganisms.
  • the effluent water W ⁇ b> 2 that has flowed out of the biological treatment water tank 11 is supplied to the membrane separation device 13 via the pressurizing pump 21.
  • the effluent water W ⁇ b> 2 supplied to the membrane separation device 13 is sent into the tubular filtration membrane 3 of the membrane module 1.
  • the operation of the pressurizing pump 21 is controlled by the control device 12 as described later.
  • the permeation side space P in the casing 2 of the membrane module 1 becomes negative pressure by the operation of the suction pump 22.
  • the suction pump 22 sucks in a direction substantially orthogonal to the flow of the effluent water W2 flowing through the tubular filtration membrane 3 through the permeate discharge port 9.
  • the operation of the suction pump 22 is controlled by the control device 12 as described later.
  • the permeated water PW permeated from the tubular filtration membrane 3 is stored in the storage tank 20 through the permeated water discharge port 9 and the permeated water pipe 18.
  • the air vent 33 is closed while the suction pump 22 is operating.
  • Concentrated water W3 (return sludge) discharged from the membrane separation device 13 is returned to the biological treatment water tank 11 through the return pipe 19 for the entire amount excluding the excess sludge M, and is processed again. Further, when the biological treatment apparatus 10 is stopped, the entire amount of the permeated water PW in the permeation side space P of the membrane module 1 is discharged out of the permeation side space P. In other words, the permeated water PW does not stay in the permeate-side space P even when the flow of the effluent W2 is stopped by the control device 12 stopping the pressurizing pump 21.
  • the control method of the biological treatment apparatus 10 of this embodiment is demonstrated.
  • the absolute value of the effluent water pressurizing step P1 for pressurizing W2, the permeated water suction step P2 for sucking the permeated water PW in the permeate side space P of the membrane separation device 13 using the suction pump 22, and the pressure in the permeate side space P The pressure determination step P3 in which the control device 12 determines whether or not the pressure is larger than the threshold value, and the effluent water that is pressurized by the pressure pump 21 when the absolute value of the pressure in the transmission side space P is larger than the threshold value.
  • An effluent water flow rate increasing step P4 for increasing the flow rate of W2 and an effluent water flow rate adjusting step P5 for adjusting the flow rate of the effluent water W2 by the control device 12 are provided.
  • the control device 12 satisfies the planned values of the membrane surface flow velocity and FLUX (outflow amount of the permeate water PW) based on the value of the flow velocity received from the velocimeter 66.
  • the pressurization pump 21 and the suction pump 22 are controlled so as to be in the range.
  • the membrane surface flow rate is a speed at which the effluent water W2 flows inside the tubular filtration membrane 3.
  • the film surface flow velocity is, for example, 0.15 m / s-0.30 m / s.
  • the control device 12 determines whether or not the value of the pressure (water pressure) in the transmission side space P measured by the pressure gauge 23 is larger than the threshold value.
  • the permeated water PW does not sufficiently pass through the tubular filtration membrane 3.
  • the absolute value of the pressure in the permeate-side space P which is set to a negative pressure by the operation of the suction pump 22, increases due to the fact that the permeate PW does not pass sufficiently, and becomes larger than the threshold value.
  • the threshold value of the pressure in the transmission side space P can be appropriately determined by, for example, a prior experiment.
  • the control device 12 controls the pressurizing pump 21 to increase the flow rate of the outflow water W2 supplied to the concentration side space S.
  • the control device 12 normally operates the suction pump 22 similarly to the permeated water suction step P2, and does not perform control to increase power.
  • the flow rate of the effluent water W2 increases (the pressure of the effluent water W2 increases)
  • the foreign matter accumulated inside the tubular filtration membrane 3 is washed away downstream. Thereby, the function of the tubular filtration membrane 3 is restored, and the permeated water PW flows into the permeate side space P.
  • the pressure value transmitted from the pressure gauge 23 to the control device 12 becomes equal to or less than the threshold value.
  • control is performed to adjust the flow rate of the effluent water W2 increased in the effluent water flow rate increase step P4.
  • the control device 12 controls the pressurizing pump 21 to return the flow rate of the effluent water W2 when the pressure value received from the pressure gauge 23 is equal to or less than the threshold value.
  • the control device 12 controls the excess sludge adjusting device 67 (for example, a pump or a valve) to increase the amount of excess sludge M pulled out from the excess sludge pipe 28, and the value of the water level measured by the water level measuring device 56. Is adjusted to a predetermined value.
  • the excess sludge adjusting device 67 for example, a pump or a valve
  • control device 12 can control the flow rate of the water to be treated W1 supplied to the biological treatment water tank 11 based on the measurement value of the water level measurement device 56.
  • the membrane surface flow velocity can be lowered by forming the tubular filtration membrane 3 with a hydrophilic material.
  • the membrane surface flow velocity can be set to, for example, 0.15 m / s-0.30 m / s.
  • the biological treatment apparatus 10 of the present embodiment can reduce the membrane surface flow velocity, the circulation flow rate can be reduced. Thereby, the power of the pressurizing pump 21 can be reduced. Moreover, the tank for temporarily storing circulating water and the piping for introducing circulating water into this tank become unnecessary. Further, the diameter of the pipe can be reduced by reducing the flow rate of the circulating water.
  • the control device 12 may perform control to increase or decrease the suction force of the suction pump 22 to vibrate the tubular filtration membrane 3. This is because the foreign matter is promoted by the vibration.
  • the membrane module 1 of the present embodiment is vertically arranged, and the effluent water W2 flowing through the tubular filtration membrane 3 flows from the top to the bottom. With such a configuration, the amount of permeated water at the outlet can be supplemented by the head difference. That is, the entire tubular filtration membrane 3 can be used effectively, and the power of the pressurizing pump 21 can be reduced.
  • the inner diameter of the tubular filtration membrane 3 according to the amount of coarse fibers in the effluent water W2, it is possible to suppress the tubular filtration membrane 3 from being blocked by the coarse fibers.
  • the membrane module 1 in which the tubular filtration membranes 3 are arranged in parallel is adopted as the membrane module 1, but the present invention is not limited to this.
  • a plurality of tubular filtration membranes 3 may be connected in series. That is, the first ends of the plurality of tubular filtration membranes 3 and the second ends of the tubular filtration membranes 3 are connected so that the plurality of tubular filtration membranes 3 are connected in series. It is good also as a structure which has the one connection member 46.
  • the plurality of tubular filtration membranes 3 connected in series and the effluent introduction port 7 are directly connected by the tubular second connection member 59, and the plurality of tubular filtration membranes 3 connected in series are concentrated.
  • the water discharge port 8 may be directly connected by the tubular third connection member 60.
  • the first header space S1 and the second header space S2 may be omitted. Therefore, you may change the structure of the casing 2, such as eliminating the 1st side wall 5 and the 2nd side wall 6.
  • the membrane module 1 of the above embodiment is configured such that a pressurized pump with low power can be adopted because the effluent water W2 introduced into the tubular filtration membrane 3 from above flows downward in the tubular filtration membrane 3.
  • a pressurized pump with low power can be adopted because the effluent water W2 introduced into the tubular filtration membrane 3 from above flows downward in the tubular filtration membrane 3.
  • a high-pressure pressurizing pump is adopted, an effluent inlet 7 is provided at the lower part of the casing 2 and a concentrated water outlet 8 is provided at the upper part of the casing 2 so that the effluent W2 moves upward in the tubular filtration membrane 3. It is good also as a structure which flows toward.
  • the biological treatment water tank 11B of this embodiment uses the activated sludge method.
  • the biological treatment water tank 11B includes an aerobic tank 62 that mixes the water to be treated W1 and the return sludge.
  • the aerobic tank 62 includes an ORP measurement device 51 (51E), a pH measurement device 52 (52E), and a DO measurement device 53 (53E).
  • the aerobic tank 62 includes an aeration device 57 (57E).
  • the treated water W1 is purified by being mixed with activated sludge and aerated.
  • the biological treatment water tank 11C of this embodiment uses methane fermentation.
  • the biologically treated water tank 11C includes a methane fermentation tank 63 that is a sealed container.
  • the methane fermenter 63 is a facility for generating methane gas (biogas) by decomposing macromolecular organic matter into anaerobic bacteria (microorganisms) in the methane fermenter 63.
  • the biological treatment water tank 11 ⁇ / b> C includes an alkaline agent supply device 68 that supplies an alkaline agent into the methane fermentation tank 63.
  • the methane fermentation tank 63 includes a gas circulation line 64 that circulates methane gas to the lower part of the methane fermentation tank 63.
  • the gas circulation line 64 has a gas branch line 65 for taking out part of the methane gas flowing through the gas circulation line 64. Further, when the measured value of the pH measuring device 52 (52F) becomes excessively acidic than the predetermined value, the control device 12 supplies the alkaline agent from the alkaline agent supplying device 68, and the pH measuring device 52 (52F) Control is performed so that the measured value becomes the predetermined value.
  • the methane gas taken out through the gas branch line 65 can be sent to a power generator or the like for use.
  • FIG. 1 You may send the whole quantity of methane gas to a power generation device etc., without providing the gas circulation line 64.
  • FIG. You may provide the stirring apparatus which stirs the to-be-processed water W1 stored in the methane fermentation tank 63 in the methane fermentation tank 63.
  • FIG. 1 You may provide the stirring apparatus which stirs the to-be-processed water W1 stored in the methane fermentation tank 63 in the methane fermentation tank 63.
  • the biological treatment apparatus 10 of the first embodiment employs a membrane separation apparatus 13D shown in FIG. 7 instead of the membrane separation apparatus 13.
  • the membrane separation device 13D of the present embodiment the plurality of membrane modules 1D are disposed sideways in the housing 14 of the membrane separation device 13D. That is, unlike the first embodiment, the axis A (see FIG. 8) of the cylindrical casing 2 of the membrane module 1D extends in the horizontal direction.
  • the membrane module 1 ⁇ / b> D includes a cylindrical casing 2, a plurality of tubular filtration membranes 3, and a reinforcing member 34 that reinforces the tubular filtration membrane 3.
  • the membrane module 1D of this embodiment includes a reinforcing member 34 that reinforces each tubular filtration membrane 3.
  • the reinforcing member 34 is a cylindrical member that covers each tubular filtration membrane 3 from the outer peripheral side.
  • the tubular filtration membrane 3 is inserted through the inner peripheral side of the reinforcing member 34.
  • the reinforcing member 34 includes a cylindrical main body 35 disposed on the outer peripheral side of the tubular filtration membrane 3, and a plurality of support portions 36 provided on the inner peripheral surface 35 a of the cylindrical main body 35. And a plurality of through holes 37 formed in the cylindrical main body 35.
  • the cylindrical main body 35 has a cylindrical shape. As shown in FIG. 10, the inner diameter of the cylindrical main body 35 (the diameter of the inner peripheral surface 35 a) is larger than the outer diameter of the tubular filtration membrane 3. A gap G is formed between the inner peripheral surface 35 a of the cylindrical main body 35 and the outer peripheral surface of the tubular filtration membrane 3.
  • the inner diameter of the cylindrical main body 35 can be 7 mm, for example.
  • the gap G between the inner peripheral surface 35a of the tubular main body 35 and the outer peripheral surface of the tubular filtration membrane 3 is 2 mm.
  • the cylindrical main body 35 is formed such that the gap G between the tubular main body 35 and the tubular filtration membrane 3 is constant.
  • the length of the cylindrical main body portion 35 is the same as the distance between the first partition wall 30 and the second partition wall 31. That is, the length of the cylindrical main body 35 is the same as the length of the tubular filtration membrane 3 exposed in the permeation side space P.
  • the cylindrical main body 35 can be formed of, for example, a lightweight metal such as titanium or aluminum, or a plastic such as polyacetal resin.
  • the plate thickness of the cylindrical main body 35 is preferably as thin as possible within a range that does not impair the strength of the reinforcing member 34.
  • the support part 36 is a protrusion extending in the direction of the axis A (extending direction) of the cylindrical main body part 35.
  • a plurality of support portions 36 are formed in the circumferential direction of the cylindrical main body portion 35 at intervals.
  • the height of each support portion 36 is substantially the same as the width of the gap G between the inner peripheral surface 35 a of the cylindrical main body portion 35 and the outer peripheral surface of the tubular filtration membrane 3.
  • the reinforcement member 34 of this embodiment has the eight support parts 36, if it can support the tubular filtration membrane 3, it will not restrict to this. In order to secure a wider space between the tubular main body 35 and the tubular filtration membrane 3, that is, a space where the permeated water PW is discharged, the number of support portions 36 should be as small as three. Is preferred.
  • the support part 36 is continuously formed in the axis line A direction of the cylindrical main-body part 35, it is not restricted to this. The support part 36 should just be able to support the tubular filtration membrane 3, ensuring this space as much as possible, without filling the space between the cylindrical main-body part 35 and the tubular filtration membrane 3.
  • the support part 36 may be intermittently formed in the axis A direction.
  • the tubular filtration membrane 3 may be point-supported by a plurality of support protrusions that are separated from each other.
  • the through-hole 37 is an opening that allows communication between the outer peripheral side of the cylindrical main body 35 and the inner peripheral side of the cylindrical main body 35.
  • the plurality of through holes 37 are regularly (equally) arranged on the entire outer surface of the cylindrical main body 35. It is preferable to form as many through holes 37 as possible as long as the strength of the reinforcing member 34 is not impaired.
  • the position of the through hole 37 in the circumferential direction of the cylindrical main body portion 35 is preferably different from that of the support portion 36.
  • the membrane module 1D can be easily replaced even when a plurality of membrane modules 1D are arranged by placing the membrane module 1D horizontally, that is, by arranging the casing 2 so as to extend in the horizontal direction. It can be. Thereby, the maintenance of the membrane separation apparatus 13D including the plurality of membrane modules 1D can be facilitated.
  • the plurality of tubular filtration membranes 3 are reinforced by the reinforcing member 34, thereby preventing the tubular filtration membrane 3 from being bent even when the tubular filtration membrane 3 is arranged to extend in the horizontal direction. Can do.
  • the permeated water PW permeated from the tubular filtration membrane 3 is formed by forming a gap G between the inner circumferential surface 35 a of the reinforcement member 34 and the outer circumferential surface of the tubular filtration membrane 3 by the support portion 36 of the reinforcement member 34. It is possible to support the tubular filtration membrane 3 so as not to bend without impeding the flow.
  • the membrane module 1D when the membrane module 1D is placed vertically, the head difference (resistance) between the first end and the second end of the tubular filtration membrane 3 increases.
  • the membrane module 1D When the membrane module 1D is placed horizontally, the head difference is reduced and the FLUX (outflow amount) distribution can be reduced as compared with the case where the membrane module 1D is placed vertically.
  • the membrane module 1D by placing the membrane module 1D horizontally, it becomes easy to connect the plurality of membrane modules 1D in series. Even when the arrangement method of the plurality of membrane modules 1D constituting the membrane separation device 13D is arranged in series, it is easy to cope with it.
  • the length of the reinforcing member 34 is the same as the distance between the first partition wall 30 and the second partition wall 31, but is not limited thereto.
  • the length of the reinforcing member 34 is made longer than the distance between the first partition wall 30 and the second partition wall 31, and the reinforcing member 34 is inserted into the insertion holes 32 of the first partition wall 30 and the second partition wall 31. Also good. By setting it as such a form, the burden concerning the tubular filtration membrane 3 can be reduced more.
  • the reinforcing member 34 may have a cylindrical shape, and may be a mesh-like network structure disposed on the outer peripheral side of the tubular filtration membrane 3 so as to be in contact with the tubular filtration membrane 3.
  • the net-like structure can be, for example, a plastic tube formed by combining a plurality of linear plastics in a lattice shape.
  • linear plastic for example, a wire formed of a metal such as stainless steel can be employed. Moreover, you may employ
  • the reinforcing member 34 ⁇ / b> E of the present embodiment includes a plate-like main body portion 48 having a circular plate shape, and a plurality of film insertion holes 49 formed in the plate-like main body portion 48. .
  • the tubular filtration membrane 3 is inserted through the plurality of membrane insertion holes 49.
  • Three reinforcing members 34E are provided at intervals in the direction of the axis A of the casing 2.
  • the outer peripheral surface 48a of the plate-like main body 48 of the reinforcing member 34E is in contact with the inner peripheral surface of the casing 2.
  • the reinforcing member 34E is supported by the lower part of the reinforcing member 34E coming into contact with the inner peripheral surface of the casing 2.
  • the lower outer peripheral surface 48a of the reinforcing member 34E functions as a reinforcing member support portion that supports the reinforcing member 34E. Further, it is desirable that the cutout 55 exists in a part of the reinforcing member 34E, for example, so that the permeated water PW flows in the permeate side space P.
  • the plurality of tubular filtration membranes 3 are mechanically connected by the reinforcing member 34E.
  • the reinforcing member 34E of the present embodiment supports the tubular filtration membrane 3 only at three points in the extending direction, the permeated water PW can be further permeated as compared with the reinforcing member 34E of the second embodiment. it can.
  • the outer peripheral surface 48a of the reinforcing member 34E is in contact with the inner peripheral surface of the casing 2, but the present invention is not limited to this. That is, if the reinforcing member 34 ⁇ / b> E is supported by the inner peripheral surface of the casing 2, the upper portion of the reinforcing member 34 ⁇ / b> E does not need to be in contact with the inner peripheral surface of the casing 2. Moreover, the shape which a part of outer periphery contact
  • the membrane filtration rate can be lowered because the tubular filtration membrane has hydrophilicity.
  • the circulating flow volume of to-be-processed water can be decreased, and the tank for temporarily storing a lot of circulating water becomes unnecessary.
  • the concentrated water (return sludge) can be stably supplied to the biological treatment water tank.

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  • Life Sciences & Earth Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Microbiology (AREA)
  • Water Supply & Treatment (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Hydrology & Water Resources (AREA)
  • Organic Chemistry (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Molecular Biology (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Activated Sludge Processes (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
PCT/JP2016/085143 2015-12-11 2016-11-28 生物処理装置 WO2017098941A1 (ja)

Priority Applications (4)

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MYPI2018700185A MY185893A (en) 2015-12-11 2016-11-28 Biological treatment device
CN201680043796.6A CN107848850A (zh) 2015-12-11 2016-11-28 生物处理装置
KR1020187001543A KR102167816B1 (ko) 2015-12-11 2016-11-28 생물 처리 장치
SG11201800356WA SG11201800356WA (en) 2015-12-11 2016-11-28 Biological treatment device

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Families Citing this family (1)

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Publication number Priority date Publication date Assignee Title
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Citations (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5044656A (zh) * 1973-08-27 1975-04-22
JPH034994A (ja) * 1989-05-31 1991-01-10 Meidensha Corp 廃水処理装置
JPH0760287A (ja) * 1993-08-24 1995-03-07 Sumitomo Heavy Ind Ltd 汚水の脱窒処理方法およびその脱窒処理装置
JPH10150973A (ja) * 1996-11-26 1998-06-09 Nec Environment Eng Ltd メタン発酵装置
JPH11300168A (ja) * 1998-04-24 1999-11-02 Mitsui Zosen Engineering Kk 膜処理方法及び膜処理装置
JP2000271581A (ja) * 1999-03-26 2000-10-03 Matsushita Electric Works Ltd 膜処理型浄化槽
JP2000279984A (ja) * 1999-03-31 2000-10-10 Sumitomo Heavy Ind Ltd 生物処理装置
JP2002113484A (ja) * 2000-10-10 2002-04-16 Hitachi Zosen Corp 浄水処理方法および装置
JP2003126874A (ja) * 2001-10-29 2003-05-07 Hitachi Plant Eng & Constr Co Ltd 砒素含有水の処理方法及びその装置
JP2006015335A (ja) * 2004-06-01 2006-01-19 Kubota Corp 膜型メタン発酵処理方法および装置
JP2006297376A (ja) * 2005-03-24 2006-11-02 Ngk Insulators Ltd 分離膜の洗浄方法
JP2010012434A (ja) * 2008-07-04 2010-01-21 Hitachi Plant Technologies Ltd Ｍｂｒ＋ｒｏシステムの構造および運転方法。
JP2010234226A (ja) * 2009-03-31 2010-10-21 Kubota Corp メタン発酵処理装置
WO2010150405A1 (ja) * 2009-06-26 2010-12-29 旭化成ケミカルズ株式会社 ろ過方法及び膜ろ過装置
JP2011218246A (ja) * 2010-04-05 2011-11-04 Sumitomo Electric Ind Ltd 濾過膜評価装置および濾過膜評価方法
JP2012179019A (ja) * 2011-03-02 2012-09-20 Toray Ind Inc 連続発酵による化学品の製造方法
JP2013248607A (ja) * 2012-05-01 2013-12-12 Sumitomo Heavy Ind Ltd 膜分離装置及び膜分離方法
JP2014034003A (ja) * 2012-08-09 2014-02-24 Meidensha Corp 膜分離メタン発酵処理装置及び膜分離メタン発酵処理方法

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP3208053B2 (ja) * 1995-10-09 2001-09-10 明久 湊 精製水製造装置
JP4832393B2 (ja) * 2007-09-20 2011-12-07 月島環境エンジニアリング株式会社 膜を用いたポリグリセリンの分離方法及び分離装置
CN101734794B (zh) * 2008-11-19 2012-01-11 北京渭黄天安环保科技有限公司 利用侧流式膜生物反应器装置及利用其的污水处理方法
JP5757089B2 (ja) * 2011-01-05 2015-07-29 栗田工業株式会社 有機物含有水の処理方法及び処理装置
JP5960401B2 (ja) 2011-09-02 2016-08-02 積水化学工業株式会社 水処理装置及び水処理方法
CN102642926B (zh) * 2012-04-28 2013-07-03 哈尔滨工业大学水资源国家工程研究中心有限公司 厌氧流化床-微氧膜生物反应器的污水处理系统及方法
CN103922468B (zh) * 2014-03-17 2015-06-10 大连民族学院 一种低能耗无曝气生活污水再利用装置

Patent Citations (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5044656A (zh) * 1973-08-27 1975-04-22
JPH034994A (ja) * 1989-05-31 1991-01-10 Meidensha Corp 廃水処理装置
JPH0760287A (ja) * 1993-08-24 1995-03-07 Sumitomo Heavy Ind Ltd 汚水の脱窒処理方法およびその脱窒処理装置
JPH10150973A (ja) * 1996-11-26 1998-06-09 Nec Environment Eng Ltd メタン発酵装置
JPH11300168A (ja) * 1998-04-24 1999-11-02 Mitsui Zosen Engineering Kk 膜処理方法及び膜処理装置
JP2000271581A (ja) * 1999-03-26 2000-10-03 Matsushita Electric Works Ltd 膜処理型浄化槽
JP2000279984A (ja) * 1999-03-31 2000-10-10 Sumitomo Heavy Ind Ltd 生物処理装置
JP2002113484A (ja) * 2000-10-10 2002-04-16 Hitachi Zosen Corp 浄水処理方法および装置
JP2003126874A (ja) * 2001-10-29 2003-05-07 Hitachi Plant Eng & Constr Co Ltd 砒素含有水の処理方法及びその装置
JP2006015335A (ja) * 2004-06-01 2006-01-19 Kubota Corp 膜型メタン発酵処理方法および装置
JP2006297376A (ja) * 2005-03-24 2006-11-02 Ngk Insulators Ltd 分離膜の洗浄方法
JP2010012434A (ja) * 2008-07-04 2010-01-21 Hitachi Plant Technologies Ltd Ｍｂｒ＋ｒｏシステムの構造および運転方法。
JP2010234226A (ja) * 2009-03-31 2010-10-21 Kubota Corp メタン発酵処理装置
WO2010150405A1 (ja) * 2009-06-26 2010-12-29 旭化成ケミカルズ株式会社 ろ過方法及び膜ろ過装置
JP2011218246A (ja) * 2010-04-05 2011-11-04 Sumitomo Electric Ind Ltd 濾過膜評価装置および濾過膜評価方法
JP2012179019A (ja) * 2011-03-02 2012-09-20 Toray Ind Inc 連続発酵による化学品の製造方法
JP2013248607A (ja) * 2012-05-01 2013-12-12 Sumitomo Heavy Ind Ltd 膜分離装置及び膜分離方法
JP2014034003A (ja) * 2012-08-09 2014-02-24 Meidensha Corp 膜分離メタン発酵処理装置及び膜分離メタン発酵処理方法

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SG11201800356WA (en) 2018-02-27
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JP6264698B2 (ja) 2018-01-24
TW201726238A (zh) 2017-08-01
KR102167816B1 (ko) 2020-10-20
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JP2017104833A (ja) 2017-06-15
MY185893A (en) 2021-06-14

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