WO2003101896A1 - Procede et dispositif de traitement des eaux usees - Google Patents

Procede et dispositif de traitement des eaux usees Download PDF

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Publication number
WO2003101896A1
WO2003101896A1 PCT/JP2003/006686 JP0306686W WO03101896A1 WO 2003101896 A1 WO2003101896 A1 WO 2003101896A1 JP 0306686 W JP0306686 W JP 0306686W WO 03101896 A1 WO03101896 A1 WO 03101896A1
Authority
WO
WIPO (PCT)
Prior art keywords
sludge
tank
aeration tank
aeration
wastewater treatment
Prior art date
Application number
PCT/JP2003/006686
Other languages
English (en)
Japanese (ja)
Inventor
Masanori Wakayama
Jiro Usui
Wataru Fujii
Minoru Okada
Naoya Tanakamaru
Original Assignee
Japan Sewage Works Agency
Mitsubishi Rayon Engineering Co., Ltd.
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
Publication date
Application filed by Japan Sewage Works Agency, Mitsubishi Rayon Engineering Co., Ltd. filed Critical Japan Sewage Works Agency
Priority to CNB038122286A priority Critical patent/CN1295164C/zh
Priority to KR20047019099A priority patent/KR100651092B1/ko
Publication of WO2003101896A1 publication Critical patent/WO2003101896A1/fr
Priority to HK05111611A priority patent/HK1077053A1/xx

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Classifications

    • 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
    • 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
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/308—Biological phosphorus removal
    • 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
    • C02F2209/04—Oxidation reduction potential [ORP]
    • 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
    • C02F2209/22—O2
    • 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 apparatus and a method for efficiently treating wastewater containing organic matter.
  • AO method As a dephosphorization method in the wastewater treatment method, there is a so-called AO method in which an anaerobic tank, an aeration tank, and a sedimentation tank are provided, and sludge in the sedimentation tank is returned to the anaerobic tank.
  • This method utilizes the fact that phosphorus storage bacteria accumulate phosphoric acid as polyphosphate in cells by continuously repeating a cycle in which activated sludge is put into an anaerobic state and then into an aerobic state.
  • dephosphorization was possible with this method, denitrification could not be performed.
  • the sludge in the anoxic tank and the aeration tank is circulated, the ammonia gas is oxidized to nitrate nitrogen in the aeration tank, and the nitrate nitrogen is reduced in the anoxic tank to reduce the nitrogen gas.
  • the activated sludge circulation method that discharges the wastewater from the system has been widely used. However, this method could remove nitrogen efficiently but did not remove phosphorus sufficiently. This is because dissolved oxygen, nitric acid nitrate, and nitrite nitrogen contained in the circulating water from the aerobic tank do not sufficiently increase the anaerobicity of the anoxic tank and do not sufficiently release phosphorus from phosphorus-accumulating bacteria. That's why.
  • an inorganic coagulant is added to the anoxic tank or aeration tank of the modified activated sludge circulation method to insolubilize phosphate ions and to remove excess sludge together with excess sludge.
  • the method of adding the coagulant has a problem that the cost of the coagulant is increased and the amount of excess sludge generated is increased, so that the processing cost of the excess sludge is also increased.
  • the A., ⁇ method requires a (complete) anaerobic tank compared to the activated sludge circulation method.
  • the present invention has been made to solve such a problem, and a wastewater treatment method capable of removing nitrogen and phosphorus without using a coagulant in only two treatment tanks, an anoxic tank and an aeration tank. And a wastewater treatment method. Disclosure of the invention
  • the present invention relates to a wastewater treatment apparatus configured to circulate sludge between an anoxic tank and an aeration tank to biologically treat wastewater.
  • a wastewater treatment apparatus configured to take out circulating fluid sludge from under an aeration device located at the lowest position in an aeration tank when sending circulating fluid sludge to an oxygen tank.
  • the wastewater treatment apparatus of the present invention can remove nitrogen and phosphorus in only two treatment tanks, an anoxic tank and an aeration tank, without using a coagulant.
  • the position for taking out the sludge, which is the circulating liquid be at least 20 cm below the lowest aeration device.
  • the present invention relates to a wastewater treatment method using activated sludge for biologically treating wastewater by circulating sludge between an anoxic tank and an aeration tank.
  • the dissolved oxygen concentration (hereinafter abbreviated as DOC) at the site where the sludge to be sent enters the anoxic tank is set to 0. SmgZL or less, and / or the DOC at the site where the sludge is removed from the aeration tank is set to 0.5.
  • DOC dissolved oxygen concentration
  • SmgZL or less SmgZL or less
  • / or the DOC at the site where the sludge is removed from the aeration tank is set to 0.5.
  • a wastewater treatment method characterized by being not more than mgZL. According to the wastewater treatment method of the present invention, nitrogen and phosphorus can be removed using only two treatment tanks, an anoxic tank and an aeration tank, without using a coagulant.
  • the oxygen utilization rate () of the sludge in the aeration tank is maintained at 15 mg / L -hour or more, more preferably 25 mgZL * hour or more. Thereby, phosphorus can be removed more efficiently.
  • MLSS concentration 500 OmgZL or more. This makes it possible to more reliably remove phosphorus.
  • the treatment method when circulating the sludge from the aeration tank to the oxygen-free tank, it is preferable to take out the sludge from the sludge accumulating portion in the aeration tank. Among them, it is preferable to take out the sludge from below the lowest position of the aeration device, and it is more preferable to take out the sludge from below at least 20 cm below the lowest position of the aeration device. This makes it possible to more reliably remove phosphorus.
  • the concentration of the soluble phosphate ion-form phosphorus in the oxygen-free tank it is preferable to maintain the concentration of the soluble phosphate ion-form phosphorus in the oxygen-free tank at 10 mg / L or more.
  • ORP oxidation-reduction potential
  • FIG. 1 is a schematic diagram showing an example of an embodiment of the present invention.
  • FIG. 2 is a schematic diagram showing an example of another embodiment of the present invention.
  • FIG. 3 is a schematic diagram showing an example of another embodiment of the present invention. BEST MODE FOR CARRYING OUT THE INVENTION
  • FIG. 1 is a schematic diagram showing an example of an embodiment of the present invention.
  • reference numeral 1 denotes an anoxic tank
  • reference numeral 2 denotes an aeration tank.
  • the wastewater (raw water) enters the anoxic tank 1 (arrow a), then enters the aeration tank 2 by overflow (arrow d), and is pumped from the pipe 9 through the pipe 9 at a location 6 below the aeration device 3 in the tank 2.
  • the liquid is sent as a suction flow (arrow b), and enters the oxygen-free tank 1 from the discharge unit 5 and circulates (as indicated by the arrow).
  • the raw wastewater a is biologically purified by activated sludge in the anoxic tank 1 and the aeration tank 2.
  • Nitrogen is removed by circulating sludge between the anoxic tank 1 and the aeration tank 2 by a so-called nitrification denitrification reaction.
  • Organic substances converted into BOD are aerobically oxidized and decomposed mainly by air discharged from the air discharge part of the aeration device 3 disposed in the aeration tank 2.
  • the removal of phosphorus is carried out by being taken up as polyphosphoric acid into the microorganisms by the action of microorganisms (phosphorus accumulating bacteria) in the sludge.
  • microorganisms phosphorus accumulating bacteria
  • This microorganism takes up phosphorus in an aerobic state and releases phosphorus stored in the body in an anaerobic state.
  • Phosphorus-accumulating bacteria when repeatedly exposed to anaerobic and aerobic conditions, aerobically absorb more phosphorus than the amount released during anaerobic conditions.
  • the sludge is circulated between the anoxic tank 1 and the aeration tank 2 by using a pump 4 to send liquid from one tank to the other tank, and to flow in from the other tank by overflow.
  • a pump 4 it is not necessarily limited from which tank the liquid is sent using a pump, but sending the liquid from the aeration tank 2 to the oxygen-free tank 1 is preferable from the viewpoint of energy cost because the amount of the liquid sent can be reduced.
  • the DOC at the part 5 where the circulating fluid from the aeration tank 2 enters the anoxic tank 1 is set to 0.2 mg or less, and the DOC at the part 6 where the circulating fluid is removed from the aeration tank 2 is reduced to 0%.
  • the DOC at the site 5 where the circulating liquid (sludge) from the aeration tank 2 enters the anoxic tank 1 needs to be 0.2 mgZL or less, and if it is 0.1 mg / L or less, phosphorus is removed. Is more preferable because the stability is more stable, and further preferably 0.05 mg / L or less.
  • the DOC of the circulating fluid (sludge) from the aeration tank 2 at the part 5 entering the anoxic tank 1 is determined by the length of the pipe 9 from the part 6 taking out from the aeration tank 2 to the part 5 entering the anoxic tank 1.
  • the dissolved oxygen can be reduced in the piping by consuming it.
  • it can be reduced by providing a deaeration means in the piping.
  • DOC at the portion entering the anoxic tank 1 can be reduced with a simple device configuration .
  • the DOC at the part 6 for removing the circulating fluid from the aeration tank 2 should be 0.5 mgZL or less in order to reduce the DOC at the part 5 entering the anoxic tank 1 to 0.2 mg / L or less.
  • the DOC of the site 6 from which the circulating fluid is removed from the aeration tank 2 is set to 0.3 mgZL or less, since the removal of phosphorus is more stable.
  • the DOC can be measured using an ordinary D ⁇ meter based on the diaphragm electrode method.
  • the sludge accumulating part means a part that is not easily affected by sludge flow due to aeration. For example, if a space is provided between the aeration device 3 and the bottom of the aeration tank 2, the sludge present in the lower part of the aeration device 3 will not be sufficiently stirred, and will be a stagnant portion.
  • the DOC at the site 6 where the circulating fluid (sludge) is extracted from the aeration tank 2 can be reduced to 0.5 mg ZL or less.
  • a portion for extracting circulating fluid (sludge) is provided below the lowest aeration device.
  • the distance from the aeration device 3 to the site 6 to be taken out is preferably 20 cm or more downward, more preferably 30 cm or more.
  • the aeration liquid (sludge) is taken out from the aeration tank 2 by providing a partition plate 7 inside the aeration tank 2 and providing a part 6 where the sludge is not well stirred. You may make it take out sludge.
  • the flow of sludge in the aeration tank 2 is not aerated, mainly due to the rise of air bubbles from the air outlet at the aeration part by the aerator 3
  • the sludge descends in the part, whereby the whole is stirred.
  • the oxygen utilization rate ( ⁇ ⁇ ) of the sludge in the aeration tank 2 is maintained at a high level, the oxygen is rapidly consumed in the non-aerated area, so that the portion where the dissolved oxygen becomes low in the aeration tank 2 is reduced. It is easy to form.
  • the oxygen utilization rate () of the sludge in the aeration tank 2 refers to the i of the sludge taken from the aerated part of the aeration tank 2, and the measuring method is a sewer test method (1997, Japan Sewage Works Corporation). Association).
  • the MLSS concentration in the anoxic tank 1 and the aeration tank 2 can be controlled by SRT (solid matter retention time), but for more stable dephosphorization, the MLS S concentration must be increased. It is preferable to maintain. This is because if the MLSS concentration is high, oxygen is rapidly consumed in the non-aerated portion, so that it becomes easier to form a portion in the aeration tank 2 where the DOC becomes low. When the MLSS concentration is high, the number of denitrifying bacteria per unit volume is large, so that the denitrification rate is high and an anaerobic state free of dissolved oxygen and bound oxygen easily occurs in the anoxic tank 1.
  • the MLSS concentration in the aeration tank 2 is preferably maintained at 500 OmgZL or more, more preferably 800 OmgZL or more. If the MLSS concentration is too high, the dissolution efficiency of oxygen is extremely reduced due to a decrease in sludge fluidity. Therefore, the upper limit is preferably 2000 OmgZL or less.
  • the MLSS concentration can be measured according to a sewer test method (1997, Japan Sewer Association).
  • D ⁇ C in the aeration section in the aeration tank 2 needs to be maintained at a concentration higher than that required for the organic matter decomposition treatment and the nitrification treatment, and is preferably maintained at lmg / L or more. However, if the concentration is too high, the phosphorus removal performance is reduced, so it is preferable to keep the concentration at 3 mgZL or less. D ⁇ C in the aeration section can be adjusted by adjusting the amount of aeration, changing the dissolving efficiency of the aeration apparatus 3, and the like. If the phosphate-accumulating bacteria release more phosphorus in the anoxic tank 1, more phosphorus can be taken up in the aeration tank 2.
  • the concentration of the soluble phosphate ion form phosphorus in the anoxic tank 1 is preferably maintained at 10 mg ZL or more, more preferably at 15 mg ZL or more.
  • the ORP of the oxygen-free tank 1 is preferably maintained at -150 mV (based on silver-silver chloride), more preferably at 120 OmV or less.
  • ORP is an indicator of whether a substance is easy to oxidize or reduce another substance. The larger the number, the more it is likely to participate in other substances. This means that the more the other substances are, the more easily they can be reduced.
  • the ORP is measured by a metal electrode method using a saturated silver chloride electrode as a reference electrode.
  • a part of the sludge treated in the aeration tank 2 by the wastewater treatment method of the present invention is solid-liquid separated, disinfected if necessary, and then discharged.
  • the solid-liquid separation means is not particularly limited, and a conventional precipitation separation method can be used.However, when the membrane separation device 8 is immersed in the aeration tank 2 as shown in FIG. This is preferable because high-quality treated water that is substantially not contained can be obtained. When solid-liquid separation is performed using the membrane separation device 8, the MLSS concentration can be easily maintained at a high level, and the efficiency of phosphorus removal can be increased.
  • the membrane separation device 8 is not particularly limited, and a known device such as a flat membrane, a hollow fiber membrane, a tubular ceramic membrane, and a rotating disk membrane can be used.
  • the treated water separated by the membrane is discharged out of the system by the arrow e.
  • the membrane separation device 8 may not be provided.
  • a microorganism-immobilized carrier can be added to the oxygen-free tank 1, the aeration tank 2, or both.
  • the actual MLSS concentration increases, and in the aeration tank 2, nitrifying bacteria having a low growth rate are fixed to the carrier, so that the nitrification rate in the tank is increased, and the nitrogen removal treatment can be performed in a short time. Will be able to do so.
  • the carrier used is not particularly limited, and a polyolefin hollow foam, a urethane foam carrier, or the like can be used. Add carrier In this case, a screen, mesh, etc. should be provided at the sludge discharge port, overflow port, etc. from each tank so that the carrier does not flow out. Further, the specific gravity of the carrier is preferably 1 or less in order to avoid sedimentation or the like in the stagnant portion.
  • a coagulant may be added to the raw water, the oxygen-free tank 1, or the aeration tank 2 to reduce the phosphorus concentration in the treated water.
  • Aeration device Installed at a height of 60 cm from the bottom of the aeration tank
  • Circulating fluid outlet from aeration tank 2 Installed at a height of 20 cm from the bottom of the aeration tank
  • a membrane separation device 8 using a hollow fiber membrane (membrane area: 126 m 2 ; manufactured by Mitsubishi Rayon Co., Ltd .; using a polyethylene hollow fiber membrane; product name: EX 540 V) was installed at a position 50 cm above the aeration device. The filtrate was taken out as treated water.
  • Table 1 shows the raw water quality and sludge properties
  • Table 2 shows the treated water quality.
  • each measurement method was performed as follows according to the sewer test method (1997, Japan Sewerage Association).
  • BOD was measured without adding a nitrification inhibitor.
  • C ⁇ D COD was measured by the so-called Mangan method determined from the consumption of potassium permanganate.
  • Total phosphorus was measured by a complete degradation assay.
  • DOC was measured using a dissolved oxygen meter (a dissolved oxygen sensor (model number: DO30G) and a dissolved oxygen converter (model number: DO402G) manufactured by Yokogawa Electric Corporation).
  • ORP silver-silver chloride standard
  • ORP sensor model number: OR8 EFG
  • ORP converter model number: OR400G
  • Use Measured As the electrode, a saturated silver chloride electrode was used, and a direct reading value was used.
  • Soluble phosphate ion phosphorus concentration The concentration of soluble phosphate ion phosphorus is determined by filtering a non-oxygen tank sludge sample with dry filter paper Type 5 B and then filtering the filtrate with molybdenum blue (ascorbic acid reduction). It was measured using the method.
  • Solid content and MLSS concentration Measured by centrifugation. That is, take an appropriate amount of sludge sample in a sedimentation tube, perform centrifugation for 2 to 3 minutes at "3000 to 4000]" 13171, discard the supernatant, add water to the sedimentation tube, stir, and centrifuge again in the same manner. The liquid was discarded, the precipitate was washed in an evaporating dish, dried at 105 to 110 ° C for 2 hours, the mass was measured, and calculated by the following formula.
  • a part of the sensor (Central Chemical Co., UC 101) was inserted and the decrease in oxygen concentration was recorded.
  • the oxygen utilization rate was calculated from the following equation using the initial linear part of the recorded decrease curve.
  • Oxygen utilization rate (r r ) (mgZL ') oxygen reduction (mgZL) Z elapsed time (time)
  • r r oxygen utilization rate
  • phosphorus can be removed in addition to removing nitrogen and BOD using only two tanks, an anoxic tank and an aeration tank. You. Furthermore, since no coagulant is added, the amount of excess sludge generated can be kept low.

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  • Life Sciences & Earth Sciences (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Chemical & Material Sciences (AREA)
  • Microbiology (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Molecular Biology (AREA)
  • Health & Medical Sciences (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

L'invention concerne un appareil pour traiter des eaux usées, les boues circulant entre un bassin anaérobie et un bassin d'aération et les eaux usées étant ainsi traitées biologiquement. L'invention est caractérisée en ce que, lorsque les boues passent du bassin d'aération au bassin anaérobie, elles sont extraites à un niveau inférieur à celui d'un dispositif d'aération disposé au niveau le plus bas parmi les dispositifs montés dans le bassin d'aération. L'appareil permet, par exemple, d'extraire à la fois l'azote et le phosphore au moyen de seulement deux bassins de traitement, un bassin anaérobie et un bassin d'aération, sans utiliser d'agent coagulant.
PCT/JP2003/006686 2002-05-31 2003-05-28 Procede et dispositif de traitement des eaux usees WO2003101896A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
CNB038122286A CN1295164C (zh) 2002-05-31 2003-05-28 排水处理装置及排水处理方法
KR20047019099A KR100651092B1 (ko) 2002-05-31 2003-05-28 폐수 처리 장치 및 폐수 처리 방법
HK05111611A HK1077053A1 (en) 2002-05-31 2005-12-15 Apparatus and method for waste water treatment

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2002-159466 2002-05-31
JP2002159466A JP3962284B2 (ja) 2002-05-31 2002-05-31 排水処理装置及び排水の処理方法

Publications (1)

Publication Number Publication Date
WO2003101896A1 true WO2003101896A1 (fr) 2003-12-11

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PCT/JP2003/006686 WO2003101896A1 (fr) 2002-05-31 2003-05-28 Procede et dispositif de traitement des eaux usees

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JP (1) JP3962284B2 (fr)
KR (1) KR100651092B1 (fr)
CN (1) CN1295164C (fr)
HK (1) HK1077053A1 (fr)
WO (1) WO2003101896A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2007190488A (ja) * 2006-01-19 2007-08-02 Mitsubishi Rayon Eng Co Ltd 膜分離活性汚泥処理装置
WO2008139617A1 (fr) 2007-05-14 2008-11-20 Mitsubishi Rayon Engineering Co., Ltd. Ensemble filtre à membrane
JP2013255919A (ja) * 2013-08-14 2013-12-26 Mitsubishi Rayon Co Ltd 膜ろ過ユニット

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JP4603307B2 (ja) * 2004-07-27 2010-12-22 株式会社神鋼環境ソリューション 活性汚泥処理装置およびその運転方法
JP5448285B2 (ja) * 2005-12-07 2014-03-19 三菱レイヨン株式会社 膜分離活性汚泥処理方法
US7378023B2 (en) * 2006-09-13 2008-05-27 Nalco Company Method of improving membrane bioreactor performance
JP2010253428A (ja) * 2009-04-28 2010-11-11 Asahi Kasei Chemicals Corp 排水処理装置及び排水処理方法
CN103663695B (zh) * 2013-12-09 2015-11-04 北京威力尔德科贸有限公司 一种去除废水中氮磷的方法

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JPH06343992A (ja) * 1993-06-07 1994-12-20 Shimizu Corp 廃水処理装置
JP2001029991A (ja) * 1999-07-23 2001-02-06 Nissin Electric Co Ltd 水処理方法
WO2001066475A1 (fr) * 2000-03-08 2001-09-13 Kyong-Ho Engineering & Architects Co., Ltd. Appareil et procede d'epuration des eaux usees

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JP2000197892A (ja) * 1999-01-08 2000-07-18 Kubota Corp 浄化槽およびその運転方法
JP3872302B2 (ja) * 2001-02-02 2007-01-24 住友重機械工業株式会社 排水処理装置
JP2003019496A (ja) * 2001-07-09 2003-01-21 Kubota Corp 窒素除去を行う水処理装置
JP3744425B2 (ja) * 2002-01-15 2006-02-08 日立プラント建設株式会社 膜分離廃水処理装置

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Publication number Priority date Publication date Assignee Title
JPH06343992A (ja) * 1993-06-07 1994-12-20 Shimizu Corp 廃水処理装置
JP2001029991A (ja) * 1999-07-23 2001-02-06 Nissin Electric Co Ltd 水処理方法
WO2001066475A1 (fr) * 2000-03-08 2001-09-13 Kyong-Ho Engineering & Architects Co., Ltd. Appareil et procede d'epuration des eaux usees

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2007190488A (ja) * 2006-01-19 2007-08-02 Mitsubishi Rayon Eng Co Ltd 膜分離活性汚泥処理装置
WO2008139617A1 (fr) 2007-05-14 2008-11-20 Mitsubishi Rayon Engineering Co., Ltd. Ensemble filtre à membrane
US20100200481A1 (en) * 2007-05-14 2010-08-12 Yoshihito Nakahara Membrane Filter Unit
EP2147714A4 (fr) * 2007-05-14 2012-05-30 Mitsubishi Rayon Co Ensemble filtre à membrane
JP5456253B2 (ja) * 2007-05-14 2014-03-26 三菱レイヨン株式会社 活性汚泥処理装置
US8728316B2 (en) 2007-05-14 2014-05-20 Mitsubishi Rayon Co., Ltd. Membrane filter unit
JP2013255919A (ja) * 2013-08-14 2013-12-26 Mitsubishi Rayon Co Ltd 膜ろ過ユニット

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CN1295164C (zh) 2007-01-17
KR20050028916A (ko) 2005-03-23
CN1656026A (zh) 2005-08-17
JP3962284B2 (ja) 2007-08-22
HK1077053A1 (en) 2006-02-03
KR100651092B1 (ko) 2006-11-30
JP2004000835A (ja) 2004-01-08

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