JP2001212587A - Method and apparatus for diffusing air of membrane separation activated sludge method - Google Patents

Method and apparatus for diffusing air of membrane separation activated sludge method

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Publication number
JP2001212587A
JP2001212587A JP2000026885A JP2000026885A JP2001212587A JP 2001212587 A JP2001212587 A JP 2001212587A JP 2000026885 A JP2000026885 A JP 2000026885A JP 2000026885 A JP2000026885 A JP 2000026885A JP 2001212587 A JP2001212587 A JP 2001212587A
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air
diffuser
bubbles
aeration
coarse
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Shinichi Fukuhara
Hirosuke Oi
裕亮 大井
真一 福原
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Kubota Corp
株式会社クボタ
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Priority to JP2000026885A priority Critical patent/JP2001212587A/en
Publication of JP2001212587A publication Critical patent/JP2001212587A/en
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    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02WCLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00Technologies for wastewater treatment
    • Y02W10/10Biological treatment of water, waste water, or sewage
    • Y02W10/15Aerobic processes

Abstract

PROBLEM TO BE SOLVED: To supply sufficient oxygen without damaging the membrane surface washing effect due to coarse air bubbles and accompanied by the diffusion of an excessive amount of air. SOLUTION: A predetermined amount of air is divided to be supplied to first and second air diffusers 8, 9 and a first aeration zone L3 is formed by fine air bubbles A diffused from the first air diffuser 8 arranged under an immersion type membrane separation apparatus 3 and a second aeration zone L2 is formed by coarse air bubbles B diffused from the second air diffuser 9 arranged above the first air diffuser 8 and finer air bubbles A diffused from the first air diffuser 8 and oxygen is supplied to the activated sludge mixed liquid in a tank with high dissolving efficiency by the independent aeration due to fine air bubbles A in the first aeration zone L3 and oxygen is supplied by the mixing aeration of coarse air bubbles B and fine air bubbles A in the second aeration zone L3 and the ascending streams of a gas-liquid mixed phase generated by the air lift action of coarse bubbles B and fine air bubbles A are allowed to act on the membrane surface of the immersion type membrane separation apparatus 3 as sweeping streams.

Description

【発明の詳細な説明】 DETAILED DESCRIPTION OF THE INVENTION

【0001】 [0001]

【発明の属する技術分野】本発明は、膜分離活性汚泥法の散気方法および散気装置に関し、有機性汚水を浸漬型の膜分離装置を使用して活性汚泥処理する膜分離活性汚泥処理技術に係るものである。 The present invention relates to a membrane separation active relates air diffusion method and an air diffuser of the sludge is activated sludge treatment using submerged membrane separator device organic sewage membrane separation activated sludge treatment techniques it relates to.

【0002】 [0002]

【従来の技術】従来、有機性汚水を処理する方法として活性汚泥処理があり、膜分離装置を併用して槽内の活性汚泥濃度を高く維持する膜分離活性汚泥処理がある。 Conventionally, there are activated sludge treatment as a method for processing organic sewage, there is a membrane separation activated sludge treatment to maintain a high concentration of activated sludge in the tank in combination with membrane separation device.

【0003】一般的な膜分離活性汚泥法においては、反応槽内に浸漬型膜分離装置を設置し、浸漬型膜分離装置の下方に散気装置を配置し、散気装置から散気する空気によって酸素供給を行なって活性汚泥処理を行なうとともに、空気のエアリフト作用によって生起する上昇流を浸漬型膜分離装置の膜面に掃流して作用させ、膜面に付着するケーキを連続的に洗浄している。 [0003] In a typical membrane bioreactor, reaction submerged membrane separator placed within a tank, placing a diffuser below the submerged membrane separator, to air diffusion from the air diffuser air by it performs a activated sludge process by performing oxygen supply, and purged the upflow occurs by air lift action of air on the membrane surface of the submerged membrane separator to act, washed sequentially cake adhering to the film surface ing.

【0004】散気装置には、膜面洗浄効果の高かい粗大気泡を発生させるために、孔径6〜13mmの散気孔を有する多孔管を使用している。 [0004] air diffuser, in order to generate a high paddle coarse bubbles of membrane surface cleaning effect, using a perforated tube having a diffusing pores having a pore diameter of 6~13Mm.

【0005】 [0005]

【発明が解決しようとする課題】しかし、膜面洗浄効果を優先した多孔管式散気管は、酸素溶解効率が低く、酸素供給能が不足することがある。 [SUMMARY OF THE INVENTION] However, the porous tube type diffuser tube giving priority to the membrane surface washing effect, the oxygen dissolution efficiency is low, sometimes the oxygen supply capacity is insufficient. このため十分な酸素供給を行なうためには、膜面洗浄に必要な風量以上の過大な量の空気を散気する必要があり、曝気動力の増大につながる。 To order to perform an adequate oxygen supply this, it is necessary to air diffuser the amount of air air volume more excessive required membrane surface cleaning, leading to increased aeration power.

【0006】本発明は上記した課題を解決するものであり、粗大気泡による膜面洗浄効果を損なうことなく、かつ過大な空気量の散気を伴わずに、十分な酸素供給を行なうことができる膜分離活性汚泥法の散気方法および散気装置を提供することを目的とする。 [0006] The present invention has been made to solve the problems described above, without damaging the membrane surface cleaning effect by coarse bubbles, and without excessive amount of air aeration can be performed an adequate oxygen supply and to provide air diffusion method and an air diffuser of the membrane bioreactor.

【0007】 [0007]

【課題を解決するための手段】上記課題を解決するために、請求項1に係る本発明の膜分離活性汚泥法の散気方法は、浸漬型膜分離装置を配置した反応槽において、所定量の空気を第1散気装置と第2散気装置とに分けて供給し、浸漬型膜分離装置の下方に配置した第1散気装置から散気する微細気泡によって第1曝気ゾーンを形成し、第1散気装置の上方に配置した第2散気装置から散気する粗大気泡と第1散気装置から散気する微細気泡とによって第2曝気ゾーンを形成し、第1曝気ゾーンで微細気泡による単独曝気によって槽内の活性汚泥混合液に高い溶解効率の下で酸素供給し、第2曝気ゾーンで粗大気泡と微細気泡との混合曝気によって酸素供給し、粗大気泡と微細気泡のエアリフト作用によって生起する気液混相の上向流を掃流 In order to solve the above problems SUMMARY OF THE INVENTION, diffuser method of membrane bioreactor of the present invention according to claim 1, in a reaction vessel which was placed submerged membrane separator, a predetermined amount the air supply divided into a first air diffuser and a second diffuser, the first aeration zone formed by fine bubbles diffusers from the first air diffuser apparatus disposed below the submerged membrane separator and by the coarse bubbles and micro bubbles diffusers from the first diffusion device for the air diffuser from the second diffusion device disposed above the first diffusion device to form a second aeration zone, fine in the first aeration zone bubbles and the oxygen supply under a high dissolution efficiency activated sludge mixture in the tank by a single aeration by, by mixing aeration of coarse bubbles and micro-bubbles in the second aeration zone and oxygen supply, air lift action of coarse bubbles and micro bubbles It purged the upward flow of gas-liquid mixed phase that occurs by して浸漬型膜分離装置の膜面に作用させるものである。 It is intended to act on the membrane surface of the submerged membrane separator in.

【0008】請求項2に係る本発明の膜分離活性汚泥法の散気方法は、反応槽内に所定量の空気を曝気するに際して、粗大気泡として供給する空気量と微細気泡として供給する空気量の供給比を反応槽に流入する対象汚泥の性状に応じて調整するものである。 [0008] diffuser method of membrane bioreactor of the present invention according to claim 2, the amount of air supplied when aerating the predetermined amount of air into the reaction vessel, as the air amount and the fine bubbles supplied as coarse bubbles the supply ratio and adjusts according to the nature of the target sludge flowing into the reaction vessel.

【0009】請求項3に係る本発明の膜分離活性汚泥法の散気方法は、微細気泡として供給する空気を定量供給して活性汚泥処理に必要な最低限の溶存酸素濃度を確保し、粗大気泡として供給する空気量を反応槽に流入する対象汚泥の性状に応じて調整するものである。 [0009] diffuser method of membrane bioreactor of the present invention according to claim 3, and dispensing the air supplied as fine bubbles ensuring minimum dissolved oxygen concentration required for activated sludge treatment, coarse the amount of air supplied as bubbles and adjusts according to the nature of the target sludge flowing into the reaction vessel.

【0010】請求項4に係る本発明の膜分離活性汚泥法の散気方法は、粗大気泡として供給する空気を定量供給して膜面洗浄に必要な最低限の空気量を確保し、微細気泡として供給する空気量を溶存酸素濃度に応じて調整するものである。 [0010] diffuser method of membrane bioreactor of the present invention according to claim 4 ensures a minimum amount of air necessary to the membrane surface cleaning by dispensing the air supplied as coarse bubbles, minute bubbles the air volume is to adjust in response to the dissolved oxygen concentration is supplied as.

【0011】請求項5に係る本発明の膜分離活性汚泥法の散気装置は、反応槽に浸漬型膜分離装置を配置し、浸漬型膜分離装置の下方に微細気泡を散気する第1散気装置と、粗大気泡を散気する第2散気装置とを配置し、反応槽内に散気する所定量の空気を第1散気装置と第2散気装置とに分けて供給する手段を設けたものである。 [0011] an air diffuser of the membrane bioreactor of the present invention according to claim 5, a submerged membrane separator in the reaction vessel was placed, first to aeration microbubbles below the submerged membrane separator and air diffuser, is arranged a second air diffuser to the air diffuser coarse bubbles, supplying a predetermined amount of air aeration in the reaction vessel is divided into a first air diffuser and a second diffuser it is provided with a means.

【0012】請求項6に係る本発明の膜分離活性汚泥法の散気装置は、下段に配置した第1散気装置から上方に所定距離を隔てた位置に上段の第2散気装置を配置したものである。 [0012] an air diffuser of the membrane bioreactor of the present invention according to claim 6, positioning a second air diffuser of the upper to a position separated a predetermined distance upwardly from the first diffusion device arranged in the lower part one in which the. 請求項7に係る本発明の膜分離活性汚泥法の散気装置は、第1散気装置が所定口径の小散気孔を有し、小散気孔から噴出する微細気泡が所定の酸素溶解効率を満たす気泡径となり、第2散気装置が小散気孔より大きな所定口径の大散気孔を有し、大散気孔から噴出する粗大気泡が所定の膜面洗浄効果を満たす気泡径となるものである。 Diffuser of membrane bioreactor of the present invention according to claim 7, the first diffusion device has a small aeration pores of a given diameter, the oxygen dissolution efficiency fine bubble jetting of predetermined from a small diffusing pores will bubble diameter to satisfy, in which the second diffusion device has a large aeration pores larger predetermined diameter than the small diffusing pores, coarse bubbles ejected is bubble diameter to satisfy a predetermined film surface cleaning effect from the large diffusing pores .

【0013】 [0013]

【発明の実施の形態】以下、本発明の実施の形態を図面に基づいて説明する。 BEST MODE FOR CARRYING OUT THE INVENTION Hereinafter, an embodiment of the present invention with reference to the accompanying drawings. 図1において、反応槽1には有機性汚水を供給する汚水供給系2が接続しており、反応槽1に浸漬型膜分離装置3を所定水深下(500〜150 1, the reaction tank 1 connects sewage supply system 2 supplies the organic wastewater, a predetermined depth under the submerged membrane separator 3 to reaction vessel 1 (500-150
0mm)L1に配置している。 They are arranged in 0 mm) L1.

【0014】浸漬型膜分離装置3は、複数枚の平板状膜カートリッジ4をケース5の内部に鉛直方向に沿って配置し、かつ各平板状膜カートリッジ4を相互に所定間隙をあけて平行に配置したものであり、隣接する平板状膜カートリッジ4の間に、槽内の活性汚泥混合液をクロスフローで通液する流路を形成している。 [0014] submerged membrane separator 3 is disposed along the vertical direction a plurality of plate-like membrane cartridges 4 into the case 5, and each plate-like membrane cartridges 4 mutually parallel with a predetermined gap It is obtained by arrangement between the plate-like membrane cartridges 4 adjacent to form a flow path for passing fluid activated sludge mixture in the tank in cross-flow.

【0015】ケース5は平板状膜カートリッジ4を収納する上方の膜ケース6と下方の散気ケース7とに分割形成しており、散気ケース7は内部に第1散気装置8と第2散気装置9を上下二段に配置し、第1散気装置8と第2散気装置9より噴出する空気の全量が膜ケース6に入り込むように形成している。 [0015] Case 5 is flat membrane cartridges 4 are divided formed into an upper membrane casing 6 and the lower diffuser case 7 for accommodating a diffuser casing 7 and the first diffusion device 8 inside the second place the air diffuser 9 in upper and lower stages, the total amount of air ejected from the first air diffuser unit 8 from the second diffusion device 9 is formed so as to enter the film casing 6. 膜カートリッジ4は、AB Film cartridge 4, AB
S樹脂製の濾板の両表面に濾過膜を配置し、濾板に形成した透過液流路を透過液導出管10に連通させている。 The filtration membrane is disposed on both surfaces of the filtration plate made of S resin, and communicates the permeate passage formed filtration plate on the permeate outlet tube 10.

【0016】下段の第1散気装置8は反応槽1の底部から所定距離(0〜300mm)L4の位置に配置し、上段の第2散気装置9は第1散気装置8から所定距離(3 [0016] The first diffusion device 8 of the lower part disposed at a position a predetermined distance (0~300mm) L4 from the bottom of the reaction tank 1, the second diffusion device 9 of the upper a predetermined distance from the first diffusion device 8 (3
00〜800mm)L3を隔てた上方に位置し、浸漬型膜分離装置3の下方に所定距離(500〜800mm) Located upwardly across the 00~800mm) L3, a given distance below the submerged membrane separator 3 (500~800mm)
L2を隔てた位置に配置しており、第1散気装置8は微細気泡を散気し、第2散気装置9は粗大気泡を散気する。 Is disposed at a position across the L2, the 1 air diffuser 8 is air diffuser microbubbles, the second air diffuser 9 to the air diffuser coarse bubbles. 各散気装置8、9には個々にブロア11、12を接続しており、各ブロア11、12はその駆動を制御して空気量を調整することにより、反応槽1に散気する所定量の空気を第1散気装置8と第2散気装置9とに分けて供給する。 Each air diffuser 8,9 are connected individually blower 11, each blower 11, 12 by adjusting the air quantity by controlling the drive, a predetermined amount of aeration into the reaction vessel 1 supplying separately the air to the first air diffuser unit 8 and the second diffusion device 9.

【0017】この所定空気量は、浸漬型膜分離装置3の膜カートリッジ4の膜面を洗浄するに必要な空気量と、 [0017] The predetermined air amount, the amount of air required to clean the membrane surface of the membrane cartridge 4 of the submerged membrane separator 3,
槽内の活性汚泥処理に必要な酸素量を供給できる空気量との双方を満たすことができるものであり、流入する対象汚水の性状によって異なるものである。 Are those capable of satisfying both the air quantity which can supply oxygen amount necessary for the activated sludge process in the tank is different from the nature of the subject sewage flowing.

【0018】第1散気装置8は所定口径の小散気孔を有し、小散気孔から噴出する微細気泡Aが所定の酸素溶解効率を満たす気泡径(例えば噴き出し口で0.5〜2m [0018] The first diffusion device 8 has a small aeration pores of a given diameter, in bubble size (e.g., ejection holes fine bubbles A injected from the small diffusing pores satisfies a predetermined oxygen dissolution efficiency 0.5~2m
m)となり、第2散気装置9は小散気孔より大きな所定口径の大散気孔を有し、大散気孔から噴出する粗大気泡Bが所定の膜面洗浄効果を満たす気泡径(例えば噴き出し口で0.8〜20mm)となるものである。 m), and the second diffusion device 9 has a large aeration pores larger predetermined diameter than the small diffusing pores bubble diameter is coarse bubble B to be ejected from the large diffusing pores satisfies a predetermined film surface cleaning effect (e.g. ejection holes it is in 0.8~20mm) to become one.

【0019】上記した構成における作用を説明する。 [0019] a description will be given of the operation in the configuration described above. ブロア11、12を駆動して所定量の空気(処理水量に対して25〜40倍)を第1散気装置8と第2散気装置9 A predetermined amount of air to drive the blower 11 (from 25 to 40 times the amount of water treated) and the first air diffuser 8 second diffusion device 9
とに分けて供給し、浸漬型膜分離装置3の下方領域に、 Supplied separately to the bets, the lower region of the submerged membrane separator 3,
第1散気装置8から散気する微細気泡Aによって第1曝気ゾーンL3を形成し、第2散気装置9から散気する粗大気泡Bと第1散気装置8の微細気泡Aとによって第2 The fine bubbles A to air diffusion from the first diffusion device 8 to form a first aeration zone L3, the by the coarse bubbles B to the air diffuser from the second diffusion device 9 and the fine bubbles A first diffusion device 8 2
曝気ゾーンL2を形成する。 To form the aeration zone L2.

【0020】第1曝気ゾーンL3では、微細気泡Aで単独曝気することによって、散気する単位空気当たりの気液接触面積が増加することで、槽内の活性汚泥混合液に高い溶解効率の下で酸素供給する。 [0020] In the first aeration zone L3, by solely aerated with fine gas bubbles A, by gas-liquid contact area per unit air aeration is increased under the high dissolution efficiency activated sludge mixture in the tank in oxygen supply.

【0021】第2曝気ゾーンL2では、粗大気泡Bと微細気泡Aとを混合曝気し、粗大気泡Bと微細気泡Aが合併と再分離を繰り返しながら槽内の活性汚泥混合液に酸素供給する。 [0021] In the second aeration zone L2, mixed aerated coarse bubble B and the fine bubbles A, oxygen is supplied to the activated sludge mixture in the tank while the coarse bubbles B and the fine bubble A is repeated merger and separated again. この粗大気泡Bと微細気泡Aのエアリフト作用によって生起する気液混相の上向流が隣接する平板状膜カートリッジ4の間の流路に流入し、活性汚泥混合液をクロスフローで浸漬型膜分離装置3に供給して固液分離し、上向流が掃流として浸漬型膜分離装置3の膜面に作用する。 This upflow of the gas-liquid mixed phase that occurs by air lift action of the coarse bubble B and the fine bubbles A flows in the flow path between the plate-like membrane cartridges 4 adjacent, submerged membrane separator activated sludge mixture in crossflow It is supplied to the device 3 and the solid-liquid separation, upward flow acts on the membrane surface of the submerged membrane separator 3 as bed load.

【0022】このとき、粗大気泡Bおよび微細気泡Aともに洗浄に寄与するが、特に粗大気泡Bは膜面間の流路を上昇していく際に膜面汚濁物質(ケーキ層)に対しての抵抗が大きく、膜面上で乱流を起こして洗浄効果を高める。 [0022] At this time, with respect to coarse bubble B and fine cells A are both contribute to cleaning, the film surface contaminants in particular coarse bubble B is going to increase the flow path between the film surface (cake layer) resistance is large, enhance the cleaning effect inducing turbulence on the membrane surface.

【0023】また、粗大気泡Bおよび微細気泡Aの全量が膜ケース6に入り込むことにより、浸漬型膜分離装置3の内部に生起する上昇流と浸漬型膜分離装置3の周囲に生起する下降流とが明確に分離されるので、反応槽1 Further, by the total amount of coarse bubbles B and the fine bubble A enters the film casing 6, downward flow that occurs around the rising flow with submerged membrane separator 3 that occurs in the interior of the submerged membrane separator 3 since bets are clearly separated, the reaction vessel 1
の内部に循環流が支障なく起こり、槽内の攪拌を円滑に行なうことができる。 Internal circulation occurs without hindrance, it is possible to perform agitation in the tank smoothly in.

【0024】ところで、季節もしくは水温により対象汚泥を活性汚泥処理するに必要な酸素量は変動する。 [0024] By the way, the amount of oxygen required to be activated sludge process the target sludge according to the season or water temperature fluctuates. このため、反応槽1に所定量(総合曝気風量)の空気を曝気するに際して、粗大気泡Bとして供給する空気量と微細気泡Aとして供給する空気量の供給比を反応槽1に流入する対象汚泥の性状に応じて調整する。 Therefore, the target sludge flowing when aerating the air of a predetermined amount into the reaction vessel 1 (total aeration volume), the supply ratio of the supply air volume as the air amount and the fine bubble A supplied as coarse bubble B to the reaction vessel 1 It is adjusted according to the properties.

【0025】例えば、酸素消費量の増える高水温時には微細気泡Aの空気量を増加させ、粗大気泡Bの空気量を低減する。 [0025] For example, at the time of high temperature to increase the oxygen consumption increases the air quantity of fine bubbles A, to reduce the air quantity of coarse bubbles B. 逆に酸素消費量の少ない低水温時には粗大気泡Bの空気量を増大させ、微細気泡Aの空気量を低減する。 During less low temperature oxygen consumption Conversely increasing the air quantity of coarse bubbles B, and reduce the amount of air micro-bubbles A.

【0026】このことにより、常に極小の総合曝気風量とすることができ、ブロア11、12の曝気動力を低減することができる。 [0026] In this way, can be always made to have a comprehensive aeration air volume of minimum, it is possible to reduce the aeration power of the blower 11 and 12. また、微細気泡Aとして供給する空気を定量供給して活性汚泥処理に必要な最低限の溶存酸素濃度を確保する状態で、粗大気泡Bとして供給する空気量を反応槽1に流入する対象汚泥の性状に応じて調整することも可能である。 Further, in a state of securing a minimum dissolved oxygen concentration required air activated sludge process by metering the supply of fine bubbles A, the target sludge flowing amount of air supplied to the reaction vessel 1 as a coarse bubble B it is also possible to adjust according to nature.

【0027】また、粗大気泡Bとして供給する空気を定量供給して膜面洗浄に必要な最低限の空気量を確保し、 Further, to ensure the minimum amount of air necessary to the membrane surface cleaning by dispensing the air supplied as coarse bubble B,
微細気泡Aとして供給する空気量を溶存酸素濃度に応じて調整することも可能である。 It is also possible to adjust according to the dissolved oxygen concentration of air quantity supplied as fine bubbles A.

【0028】 [0028]

【発明の効果】以上のように、本発明によれば、微細気泡による単独曝気を行なう第1曝気ゾーンで高い溶解効率の下で酸素供給し、粗大気泡と微細気泡との混合曝気を行なう第2曝気ゾーンで酸素供給するとともに、粗大気泡と微細気泡のエアリフト作用によって生起する気液混相の上向流の全量を掃流として浸漬型膜分離装置の膜面に作用させることにより、粗大気泡による膜面洗浄効果を損なうことなく、かつ過大な空気量の散気を伴わずに、反応槽内に十分な酸素供給を行なうことができる。 As it is evident from the foregoing description, according to the present invention, oxygen supply under high dissolution efficiency in the first aeration zone to perform a single aeration by fine bubbles, performs mixing aeration of coarse bubbles and micro bubbles first with oxygen supplied at 2 aeration zone, by applying a total amount of upward flow of the gas-liquid mixed phase to the membrane surface of the submerged membrane separator as purged that occurs by air lift action of coarse bubbles and micro bubbles, by coarse bubbles without damaging the film surface cleaning effect, and without excessive amount of air aeration can be performed an adequate oxygen supply to the reaction vessel.
また、反応槽に所定量(総合曝気風量)の空気を曝気するに際して、粗大気泡として供給する空気量と微細気泡として供給する空気量の供給比を反応槽に流入する対象汚泥の性状に応じて調整することにより、常に極小の総合曝気風量とすることができ、曝気動力を低減することができる。 Further, when aerating the air of a predetermined amount (total aeration volume) in the reactor, depending on the nature of the target sludge flowing amount of air supply ratio to be supplied to the reaction vessel as air quantity and the fine bubbles supplied as coarse bubbles by adjusting, always be a total aeration amount of minimum, it is possible to reduce the aeration power.

【図面の簡単な説明】 BRIEF DESCRIPTION OF THE DRAWINGS

【図1】本発明の実施の形態における汚水の処理装置を示す模式図である。 1 is a schematic view showing a wastewater treatment device in the embodiment of the present invention.

【符号の説明】 DESCRIPTION OF SYMBOLS

1 反応槽 2 汚水供給系 3 浸漬型膜分離装置 4 平板状膜カートリッジ 5 ケース 6 膜ケース 7 散気ケース 8 第1散気装置 9 第2散気装置 10 透過液導出管 11、12 ブロア 1 reaction vessel 2 sewage supply system 3 submerged membrane separator 4 flat membrane cartridges 5 Case 6 film case 7 air diffuser case 8 first diffusion device 9 second diffusion device 10 permeate outlet tube 11 Blower

Claims (7)

    【特許請求の範囲】 [The claims]
  1. 【請求項1】 浸漬型膜分離装置を配置した反応槽において、所定量の空気を第1散気装置と第2散気装置とに分けて供給し、浸漬型膜分離装置の下方に配置した第1 1. A reaction vessel was placed a submerged membrane separator, fed separately a predetermined amount of air into the first air diffuser and a second diffuser, arranged below the submerged membrane separator first
    散気装置から散気する微細気泡によって第1曝気ゾーンを形成し、第1散気装置の上方に配置した第2散気装置から散気する粗大気泡と第1散気装置から散気する微細気泡とによって第2曝気ゾーンを形成し、第1曝気ゾーンで微細気泡による単独曝気によって槽内の活性汚泥混合液に高い溶解効率の下で酸素供給し、第2曝気ゾーンで粗大気泡と微細気泡との混合曝気によって酸素供給し、粗大気泡と微細気泡のエアリフト作用によって生起する気液混相の上向流を掃流として浸漬型膜分離装置の膜面に作用させることを特徴とする膜分離活性汚泥法の散気方法。 A first aeration zone formed by fine bubbles diffuser from the air diffuser apparatus, fine for air diffusion from coarse bubble and first diffuser to the air diffuser from the second diffusion device disposed above the first diffusion device a second aeration zone formed by the bubble, by a single aeration by fine bubbles in the first aeration zone and oxygen supply under a high dissolution efficiency activated sludge mixture in the tank, coarse bubbles and micro-bubbles in the second aeration zone mixed aeration by oxygen supply, coarse bubbles and submerged membrane, characterized in that the action on the film surface of the separator membrane separation active as sweep the upward flow of the gas-liquid mixed phase that occurs by air lift action of fine bubbles with aeration method of sludge method.
  2. 【請求項2】 反応槽内に所定量の空気を曝気するに際して、粗大気泡として供給する空気量と微細気泡として供給する空気量の供給比を反応槽に流入する対象汚泥の性状に応じて調整することを特徴とする請求項1に記載の膜分離活性汚泥法の散気方法。 Upon wherein aerating a predetermined amount of air into the reaction vessel, adjusted in accordance with the nature of the target sludge flowing into the reaction vessel supply ratio of supply air volume as the air amount and the fine bubbles supplied as coarse bubbles diffuser method of membrane bioreactor according to claim 1, characterized in that.
  3. 【請求項3】 微細気泡として供給する空気を定量供給して活性汚泥処理に必要な最低限の溶存酸素濃度を確保し、粗大気泡として供給する空気量を反応槽に流入する対象汚泥の性状に応じて調整することを特徴とする請求項1に記載の膜分離活性汚泥法の散気方法。 3. A quantitatively supplying air supplied as fine bubbles ensuring minimum dissolved oxygen concentration required for activated sludge treatment, the nature of the target sludge flowing into the reaction tank for supplying air amount as the coarse bubbles diffuser method of membrane bioreactor according to claim 1, wherein the adjusting according to.
  4. 【請求項4】 粗大気泡として供給する空気を定量供給して膜面洗浄に必要な最低限の空気量を確保し、微細気泡として供給する空気量を溶存酸素濃度に応じて調整することを特徴とする請求項1に記載の膜分離活性汚泥法の散気方法。 4. ensuring minimum amount of air necessary to the membrane surface cleaning by dispensing the air supplied as coarse bubbles, characterized in that adjusted according to the dissolved oxygen concentration of air quantity supplied as fine bubbles diffuser method of membrane bioreactor according to claim 1,.
  5. 【請求項5】 反応槽に浸漬型膜分離装置を配置し、浸漬型膜分離装置の下方に微細気泡を散気する第1散気装置と、粗大気泡を散気する第2散気装置とを配置し、反応槽内に散気する所定量の空気を第1散気装置と第2散気装置とに分けて供給する手段を設けたことを特徴とする膜分離活性汚泥法の散気装置。 5. Place the submerged membrane separator in the reaction vessel, a first air diffuser for aeration microbubbles below the submerged membrane separator, a second air diffuser to the air diffuser coarse bubbles was placed, the air diffuser of a predetermined amount of air aeration in the reaction vessel first diffusion device and the membrane bioreactor, characterized in that a means for supplying divided into a second diffusion device apparatus.
  6. 【請求項6】 下段に配置した第1散気装置から上方に所定距離を隔てた位置に上段の第2散気装置を配置したことを特徴とする請求項5に記載の膜分離活性汚泥法の散気装置。 6. A membrane bioreactor according to claim 5, characterized in that a second diffuser in the upper from the first diffusion device disposed in the lower the position spaced a predetermined distance above of air diffuser.
  7. 【請求項7】 第1散気装置が所定口径の小散気孔を有し、小散気孔から噴出する微細気泡が所定の酸素溶解効率を満たす気泡径となり、第2散気装置が小散気孔より大きな所定口径の大散気孔を有し、大散気孔から噴出する粗大気泡が所定の膜面洗浄効果を満たす気泡径となることを特徴とする請求項5又は6に記載の膜分離活性汚泥法の散気装置。 7. a first diffusion device is a small diffusing pores of a given diameter, fine bubbles jetted from the small diffusing pores become bubble diameter to satisfy the predetermined oxygen dissolution efficiency, the second air diffuser small diffusing pores has a larger diffusing pores larger predetermined diameter, membrane bioreactor according to claim 5 or 6 coarse bubbles jetted from the large diffusing pores are characterized in that the bubble diameter to satisfy a predetermined film surface cleaning effect air diffuser of the law.
JP2000026885A 2000-02-04 2000-02-04 Method and apparatus for diffusing air of membrane separation activated sludge method Pending JP2001212587A (en)

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