JP3111463B2 - Organic wastewater treatment equipment - Google Patents
Organic wastewater treatment equipmentInfo
- Publication number
- JP3111463B2 JP3111463B2 JP20094190A JP20094190A JP3111463B2 JP 3111463 B2 JP3111463 B2 JP 3111463B2 JP 20094190 A JP20094190 A JP 20094190A JP 20094190 A JP20094190 A JP 20094190A JP 3111463 B2 JP3111463 B2 JP 3111463B2
- Authority
- JP
- Japan
- Prior art keywords
- membrane
- aerobic biological
- biological reaction
- membrane module
- organic wastewater
- Prior art date
- Legal status (The legal status 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 status listed.)
- Expired - Lifetime
Links
Classifications
-
- 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
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Activated Sludge Processes (AREA)
Description
【発明の詳細な説明】 ［産業上の利用分野］ 本発明は有機性廃水処理装置に係り、特に、好気性生
物反応処理液を膜モジュールを用いて固液分離すること
により連続処理を行なう有機性廃水処理装置において、
膜分離におけるエネルギーを増大させることなく、膜透
過速度（フラックス）を高く維持し、かつ好気性生物反
応槽の酸素溶解効率を向上せしめる有機性廃水処理装置
に関する。Description: FIELD OF THE INVENTION The present invention relates to an organic wastewater treatment apparatus, and more particularly, to an organic wastewater treatment apparatus that performs continuous treatment by solid-liquid separation of an aerobic biological reaction treatment liquid using a membrane module. Wastewater treatment equipment,
The present invention relates to an organic wastewater treatment apparatus that maintains a high membrane permeation rate (flux) without increasing energy in membrane separation and improves oxygen dissolution efficiency of an aerobic biological reactor.
［従来の技術］ 従来、有機性廃水の連続的好気性生物反応処理法とし
て、好気性生物反応処理液を膜モジュールにより固液分
離する方法が知られている。この方法は、バルキング等
の生物相の変化に影響されることなく、濁質を含まない
良好な水質の処理水が得られることから、工業的に有利
な方法である。この方法は、例えば、第５図（ａ）に示
す如く、原水である有機性廃水を配管11より好気性生物
反応槽１に導入し、好気性生物反応処理液を配管12より
膜分離装置２に導入して膜分離処理し、透過水を処理水
として配管13より排出する一方、濃縮水を配管14より生
物反応槽１に循環する方法である。この方法において、
膜分離装置２の膜モジュール2Aとしては、SSを多く含む
生物懸濁液の好気性生物反応処理水を分離処理するため
に、SSによる目詰りの起こり難い、原水流路の大きい膜
モジュール、例えば平膜（プレート・アンド・フレー
ム）型膜モジュール、チューブラー型膜モジュール等が
用いられる。因みに、集水管の外周にネット状スペーサ
を介して分離膜を巻回してなる従来のスパイラル型膜モ
ジュールでは、目詰りのため、使用不可である。[Prior Art] Conventionally, as a continuous aerobic biological reaction treatment method of organic wastewater, a method of solid-liquid separation of an aerobic biological reaction treatment liquid using a membrane module is known. This method is industrially advantageous because treated water of good water quality without turbidity can be obtained without being affected by changes in biota such as bulking. In this method, for example, as shown in FIG. 5 (a), an organic wastewater as raw water is introduced into an aerobic biological reaction tank 1 through a pipe 11, and an aerobic biological reaction treatment liquid is introduced into a membrane separation device 2 through a pipe 12. And the permeated water is discharged from the pipe 13 as treated water, and the concentrated water is circulated to the biological reaction tank 1 through the pipe 14. In this method,
As the membrane module 2A of the membrane separation device 2, in order to separate and process the aerobic biological reaction water of the biological suspension containing a large amount of SS, clogging due to SS is unlikely to occur, and a membrane module having a large raw water flow path, for example, A flat membrane (plate and frame) membrane module, a tubular membrane module, or the like is used. Incidentally, a conventional spiral type membrane module in which a separation membrane is wound around the outer periphery of a water collecting pipe via a net-shaped spacer cannot be used because of clogging.
ところで、平膜型膜モジュールのように原水流路の大
きい膜モジュールを備える膜分離装置において、高いフ
ラックスを維持するためには、分離膜面上の原水流速を
高める必要がある。原水流速を高めることは、分離膜面
のゲル層の生成抑制のためにも有効である。例えば、平
膜型膜モジュールやチューブラー型膜モジュールでは、
一般に、２〜3m/s程度の高流速を必要とする。このた
め、膜分離装置を用いる方法では、好気性生物反応処理
液を単なる沈降分離槽で固液分離する場合に比べて、多
大なエネルギーを必要とするという不具合があった。Meanwhile, in a membrane separation apparatus including a membrane module having a large raw water flow path such as a flat membrane type membrane module, in order to maintain a high flux, it is necessary to increase the flow rate of the raw water on the separation membrane surface. Increasing the flow rate of raw water is also effective for suppressing the formation of a gel layer on the separation membrane surface. For example, in a flat membrane module or a tubular membrane module,
Generally, a high flow velocity of about 2 to 3 m / s is required. For this reason, the method using a membrane separation device has a problem that much energy is required as compared with the case where the aerobic biological reaction treatment liquid is subjected to solid-liquid separation in a simple sedimentation tank.
従来、このような方法において、エネルギーの有効利
用、回収を目的として、第５図（ｂ）に示す如く、膜分
離装置２への好気性生物反応処理液の導入配管12に、空
気供給管15を設ける方法、或いは、第５図（ｃ）に示す
如く、膜分離装置２の濃縮水を好気性生物反応槽１へ循
環する配管14に、減圧発生吸入装置（エゼクター）16を
取り付ける方法が提案されている。Conventionally, in such a method, for the purpose of effective use and recovery of energy, as shown in FIG. 5 (b), an air supply pipe 15 is introduced into a pipe 12 for introducing an aerobic biological reaction solution into the membrane separation device 2. Alternatively, as shown in FIG. 5 (c), a method of attaching a vacuum generating / suctioning device (ejector) 16 to a pipe 14 for circulating the concentrated water of the membrane separation device 2 to the aerobic biological reaction tank 1 is proposed. Have been.
［発明が解決しようとする課題］ 第５図（ｂ）に示す方法では、空気供給管15より比較
的多量（ガス：液容積比＝５〜30）の空気を供給するこ
とにより、分離膜2A面のゲル層の生成を抑制する効果は
多少期待できるが、平膜型やチューブ型の膜モジュール
の場合、供給された空気の液中への溶解効率が悪い。ま
た、高流速の原水中に多量のガスを供給するために、膜
モジュールや配管が振動するという欠点があった。[Problems to be Solved by the Invention] In the method shown in FIG. 5 (b), a relatively large amount of air (gas: liquid volume ratio = 5 to 30) is supplied from the air supply pipe 15 so that the separation membrane 2A The effect of suppressing the formation of a gel layer on the surface can be expected to some extent, but in the case of a flat membrane type or tube type membrane module, the efficiency of dissolving the supplied air in the liquid is poor. Further, there is a disadvantage that the membrane module and the piping vibrate in order to supply a large amount of gas into the raw water having a high flow rate.
一方、第５図（ｃ）に示す方法では、エゼクター16よ
り供給された空気を好気性生物反応槽で有効利用するこ
とができる反面、空気泡が膜分離装置２に流入せず、分
離膜2A面へのゲル層の生成を抑制することはできないと
いう問題がある。On the other hand, in the method shown in FIG. 5 (c), the air supplied from the ejector 16 can be effectively used in the aerobic biological reaction tank, but the air bubbles do not flow into the membrane separation device 2 and the separation membrane 2A There is a problem that generation of a gel layer on the surface cannot be suppressed.
本発明は上記従来の問題点を解決し、膜分離における
エネルギーを増大させることなく、フラックスを高く維
持し、かつ、好気性生物反応槽の酸素溶解効率を向上せ
しめる有機性廃水処理装置を提供することを目的とす
る。The present invention solves the above-mentioned conventional problems, and provides an organic wastewater treatment apparatus that maintains a high flux without increasing energy in membrane separation and improves oxygen dissolution efficiency of an aerobic biological reaction tank. The purpose is to:
［課題を解決するための手段］ 本発明の有機性廃水処理装置は、有機性廃水を好気性
生物反応処理する好気性生物反応槽と、該好気性生物反
応槽の処理液を膜分離処理する膜分離装置と、該好気性
生物反応槽の処理液を膜分離装置に導入するためのポン
プを有する導入用配管とを備え、該膜分離装置の濃縮水
を好気性生物反応槽に戻すようにした有機性廃水処理装
置において、該導入用配管のポンプの吸込み側に空気を
供給する空気供給手段を設け、かつ、前記膜分離装置の
膜モジュールとして、集水管の外周に波板形のスペーサ
を介して分離膜を巻回してなるスパイラル型膜モジュー
ルを用いたことを特徴とするものである。[Means for Solving the Problems] An organic wastewater treatment apparatus of the present invention performs an aerobic biological reaction tank for treating an organic wastewater with an aerobic biological reaction, and performs a membrane separation treatment on a treatment liquid in the aerobic biological reaction tank. A membrane separation device, and an introduction pipe having a pump for introducing a treatment liquid of the aerobic biological reaction tank to the membrane separation device, so that concentrated water of the membrane separation device is returned to the aerobic biological reaction tank. In the organic wastewater treatment apparatus, the air supply means for supplying air to the suction side of the pump of the introduction pipe is provided, and as a membrane module of the membrane separation apparatus, a corrugated spacer is provided on the outer periphery of the water collection pipe. Characterized in that a spiral-wound membrane module formed by winding a separation membrane through the membrane is used.
［作用］ 本発明の有機性廃水処理装置においては、膜分離装置
へ導入される好気性生物反応処理液に空気を供給し、好
気性生物反応処理液と空気との気液混合液を膜分離装置
の膜モジュールに導入する。この膜モジュールは、集水
管の外周に波板形のスペーサを介して分離膜を巻回して
なるスパイラル型膜モジュールであり、気液混合液がこ
のスパイラル型膜モジュール内を通過する過程におい
て、該液に含有される空気が効率良く液中に溶解する。
水中に溶解した空気は、透過水側に逃げることが殆どな
く、好気性生物反応に有効利用される。[Operation] In the organic wastewater treatment apparatus of the present invention, air is supplied to the aerobic biological reaction treatment liquid introduced into the membrane separation apparatus, and the gas-liquid mixture of the aerobic biological reaction treatment liquid and air is subjected to membrane separation. Introduce into the membrane module of the device. This membrane module is a spiral membrane module in which a separation membrane is wound around the outer periphery of a water collection pipe via a corrugated spacer, and in a process in which a gas-liquid mixture passes through the spiral membrane module, Air contained in the liquid is efficiently dissolved in the liquid.
The air dissolved in water hardly escapes to the permeated water side, and is effectively used for aerobic biological reactions.
即ち、生物処理液を膜分離するモジュールとして波板
形スペーサを有するスパイラル型膜モジュール（コルゲ
ートタイプのスパイラル型膜モジュール）を用いると、
該生物処理液中に供給された空気（気体）が効率良く液
中に溶け込む。そして、好気性生物反応処理のための空
気の溶解が、膜分離による固液分離処理と同時に行なわ
れるので、好気性生物反応のための空気溶解に要するエ
ネルギーが大幅に低減される。That is, when a spiral type membrane module (corrugated type spiral type membrane module) having a corrugated spacer is used as a module for membrane separation of a biological treatment liquid,
The air (gas) supplied into the biological treatment liquid efficiently dissolves into the liquid. Since the dissolution of air for the aerobic biological reaction is performed simultaneously with the solid-liquid separation treatment by membrane separation, the energy required for the air for the aerobic biological reaction is greatly reduced.
しかも、本発明で用いられるコルゲートタイプのスパ
イラル型膜モジュールでは、原水が通過する際に強い乱
流が起こり、SSによる目詰りのほか、膜面へのゲル層の
生成も抑制されるので、低流速域でもフラックスが高
い。加えて、本発明においては、気液混合液中の空気に
より、このゲル層生成抑制作用がより一層強められ、フ
ラックスがきわめて高く維持される。Moreover, in the corrugated spiral membrane module used in the present invention, strong turbulence occurs when raw water passes through, and clogging by SS, as well as formation of a gel layer on the membrane surface is suppressed. High flux even in flow velocity region. In addition, in the present invention, the action of suppressing the formation of the gel layer is further enhanced by the air in the gas-liquid mixture, and the flux is maintained at an extremely high level.
なお、コルゲートタイプのスパイラル型膜モジュール
は特願昭62−205809号にて公知である。A corrugated spiral type membrane module is known from Japanese Patent Application No. 62-205809.
［実施例］ 以下に図面を参照して本発明を詳細に説明する。EXAMPLES The present invention will be described below in detail with reference to the drawings.
第１図は本発明の実施例に係る有機性廃水処理装置の
系統図、第７図はコルゲートタイプの膜モジュールの組
立斜視図である。本実施例装置は、膜分離装置２の膜モ
ジュールとして、第７図の如く、集水管21の外周に波板
形のスペーサ22を介して分離膜23を巻回してなるスパイ
ラル型膜モジュールを用いている。第１図の装置のその
他の流路構成自体は第５図（ｂ）の従来例と同様であ
り、同一符号は同一部分を示している。FIG. 1 is a system diagram of an organic wastewater treatment apparatus according to an embodiment of the present invention, and FIG. 7 is an assembled perspective view of a corrugated type membrane module. The apparatus of this embodiment uses a spiral type membrane module in which a separation membrane 23 is wound around a water collecting pipe 21 via a corrugated spacer 22 as shown in FIG. 7 as a membrane module of the membrane separation apparatus 2. ing. The other flow path configuration itself of the apparatus of FIG. 1 is the same as that of the conventional example of FIG. 5 (b), and the same reference numerals indicate the same parts.
第１図は装置では、第５図（ｂ）の装置と同様に、原
水は配管11より好気性生物反応槽１に導入され好気性生
物反応処理される。処理液は導入用配管12を経て膜分離
装置２に導入されるが、その間に、供給用配管15より空
気が供給され、気液混合液となって膜分離装置２に導入
される。膜分離装置２の透過水は処理水として取り出さ
れ、一方、濃縮水は好気性生物反応槽１に戻される。In the apparatus shown in FIG. 1, as in the apparatus shown in FIG. 5 (b), raw water is introduced into the aerobic biological reaction tank 1 through a pipe 11 and subjected to an aerobic biological reaction treatment. The treatment liquid is introduced into the membrane separation device 2 through the introduction pipe 12, and during that time, air is supplied from the supply pipe 15, and is introduced into the membrane separation apparatus 2 as a gas-liquid mixture. The permeated water of the membrane separation device 2 is taken out as treated water, while the concentrated water is returned to the aerobic biological reaction tank 1.
本実施例装置で用いられているコルゲートタイプの膜
モジュール2Bでは、第７図に示した通り、分離膜23は両
長側辺部が封じられた長い袋状のものであり、袋状の分
離膜23の内部にネット状のスペーサ24が装填されてい
る。この膜モジュール2Bを組み立てる場合、袋状の分離
膜23の一方の短辺部が集水管21に係着される。（袋の内
部が集水管21の内部に連通するように、集水管21の管周
面に開口を設けてある。） 次いで、この袋状の分離膜23を集水管21の外周に巻回
し、この際、分離膜23の同志の間に波板状のスペーサ22
を介在させる。In the corrugated type membrane module 2B used in the apparatus of the present embodiment, as shown in FIG. 7, the separation membrane 23 is a long bag having both long sides sealed. A net-shaped spacer 24 is loaded inside the film 23. When assembling the membrane module 2B, one short side of the bag-shaped separation membrane 23 is engaged with the water collecting pipe 21. (An opening is provided in the peripheral surface of the water collecting tube 21 so that the inside of the bag communicates with the inside of the water collecting tube 21.) Next, the bag-shaped separation membrane 23 is wound around the outer periphery of the water collecting tube 21, At this time, a corrugated spacer 22 is placed between the separation membranes 23.
Intervene.
このようにして組み立てられた膜モジュール2Bにおい
ては、原水は第７図の矢印Ｌの如く巻回体の一方の端面
の部分からスペーサ22に沿って分離膜23同志の間に入り
込み、矢印Ｍの如く巻回体の他方の端面から流出する。
そして、原水がスペーサ22に沿って流れている間に液が
分離膜23を透過し、袋状の分離膜23の内部に入る。袋状
の分離膜23の内部において、透過水は、ネット状スペー
サ24に沿って集水管21に向って流れ、遂には該集水管21
内に流入し、透過水として膜モジュール2Bから取り出さ
れる。In the membrane module 2B assembled in this manner, the raw water enters between the separation membranes 23 along the spacer 22 from one end face of the wound body as shown by the arrow L in FIG. As described above, it flows out from the other end face of the wound body.
Then, the liquid permeates the separation membrane 23 while the raw water flows along the spacer 22, and enters the inside of the bag-shaped separation membrane 23. Inside the bag-shaped separation membrane 23, the permeated water flows along the net-shaped spacer 24 toward the water collecting pipe 21 and finally the water collecting pipe 21.
And is taken out from the membrane module 2B as permeated water.
かかるコルゲートタイプの膜モジュール2Bにおいて
は、気液混合液が波板状スペーサ22に沿う流路に流れ込
む際に、あるいは、このスペーサ22に沿う狭い流路を流
れる間に、該気液混合液中の気泡が細かく剪断され、微
小気泡化し、効率良く液中に溶解する。In the corrugated type membrane module 2B, when the gas-liquid mixture flows into the flow path along the corrugated spacer 22 or while flowing through the narrow flow path along the spacer 22, the gas-liquid mixture Bubbles are finely sheared, become microbubbles, and are efficiently dissolved in the liquid.
この結果、膜分離装置２内に流れ込んだ気泡混合液中
の空気は、膜モジュール2Bを液と共に流れる間に液中に
十分に溶け込む。空気が十分に溶け込んだ液は、膜モジ
ュール2Bを通過した後、好気性生物反応処理装置に戻さ
れ、きわめて効率良く生物処理される。As a result, the air in the mixed bubble liquid flowing into the membrane separation device 2 is sufficiently dissolved in the liquid while flowing through the membrane module 2B together with the liquid. The liquid in which the air is sufficiently dissolved passes through the membrane module 2B, and is returned to the aerobic biological reaction processing device, where the biological treatment is performed very efficiently.
第２図及び第３図は本発明の有機性廃水処理装置の別
の実施例を示す系統図である。第２図及び第３図におい
て、濃縮水配管14の途中から余剰汚泥の排出用配管17が
分岐している。その他の構成は第１図の装置と同様であ
り、第１図と同一機能を有する部材には同一符号を付し
てある。FIG. 2 and FIG. 3 are system diagrams showing another embodiment of the organic wastewater treatment apparatus of the present invention. 2 and 3, a pipe 17 for discharging excess sludge branches off from the middle of the concentrated water pipe 14. Other configurations are the same as those of the apparatus of FIG. 1, and members having the same functions as those of FIG. 1 are denoted by the same reference numerals.
第２図に示す有機性廃水処理装置と第３図に示す有機
性廃水処理装置とでは、好気性生物反応処理槽（曝気
槽）１への、膜分離装置２の濃縮水の循環用配管14の接
続位置が異なるのみで、その他の構成は同様である。こ
のように、本発明において、循環用配管14の接続位置に
は制限はなく、好気性生物反応槽１の上層部であっても
下層部であっても良い。In the organic wastewater treatment apparatus shown in FIG. 2 and the organic wastewater treatment apparatus shown in FIG. 3, a pipe 14 for circulating the concentrated water of the membrane separation device 2 to the aerobic biological reaction treatment tank (aeration tank) 1 Only the connection position is different, and the other configuration is the same. Thus, in the present invention, the connection position of the circulation pipe 14 is not limited, and may be the upper layer or the lower layer of the aerobic biological reaction tank 1.
なお、本発明においては、好気性生物反応槽１の処理
液を膜分離装置２へ導入する導入用配管12のポンプＰの
吸込み側（上流側）にブロワ等により空気を配管15を経
て供給しているが、このようにポンプＰの入口側に空気
を供給することにより、極く低圧の押込み圧にて空気を
導入することができ、また、ポンプを通過する過程でも
空気の溶解を促進することができ、極めて有利である。In the present invention, air is supplied from a blower or the like to the suction side (upstream side) of the pump P of the introduction pipe 12 for introducing the treatment liquid in the aerobic biological reaction tank 1 into the membrane separation device 2 via the pipe 15. However, by supplying air to the inlet side of the pump P in this way, air can be introduced at an extremely low pressure, and the dissolution of air is promoted in the process of passing through the pump. Can be very advantageous.
この空気供給手段はブロワによる空気圧送方式に限ら
ず、第４図に示す如く、空気供給部をエゼクター形状と
して大気を自吸するように構成したものであっても良
い。エゼクター方式の場合には、空気供給管15の空気取
り入れ用開放端を好気性生物反応槽１の水位よりも高い
位置に設けて、ポンプＰ停止時の液の逆流を防ぐように
する。This air supply means is not limited to the air supply method using a blower, but may be configured such that the air supply section is formed as an ejector and self-absorbs the atmosphere, as shown in FIG. In the case of the ejector system, the open end for taking in air of the air supply pipe 15 is provided at a position higher than the water level of the aerobic biological reaction tank 1 so as to prevent the liquid from flowing backward when the pump P is stopped.
また、第１〜３図に示す如く、ポンプＰの吸込み側に
空気供給管15を接続する場合、ポンプＰとしては、空気
を吸い込んでも運転可能なポンプを選ぶ必要がある。こ
のようなポンプとしては、例えば、うず巻ポンプ等を用
いることができる。When the air supply pipe 15 is connected to the suction side of the pump P as shown in FIGS. 1 to 3, it is necessary to select a pump that can be operated even if air is sucked. For example, a centrifugal pump or the like can be used as such a pump.
本発明において、処理液中への空気供給量は、好気性
生物反応処理液の送水量の５〜10％（体積比）とするの
が望ましい。本発明に係る膜分離装置２のスパイラル型
膜モジュール2Bは、このような通常の膜モジュールより
も少ない空気供給量にて十分に高いフラックスを確保す
ることができる。なお、空気供給量が10％を超えてもフ
ラックスの向上にさほどの効果はなく、むしろ、空気供
給のためのエネルギーコストが向上する上に、導入用配
管12の振動等により好ましい運転状態を維持できなくな
るなどの不具合が生じる場合がある。In the present invention, the amount of air supplied to the treatment liquid is desirably 5 to 10% (volume ratio) of the water supply amount of the treatment liquid for the aerobic biological reaction. The spiral-type membrane module 2B of the membrane separation device 2 according to the present invention can secure a sufficiently high flux with a smaller air supply than such a normal membrane module. It should be noted that even if the air supply amount exceeds 10%, there is not much effect on the improvement of the flux. Rather, the energy cost for air supply is improved, and the preferable operation state is maintained by the vibration of the introduction pipe 12 and the like. In some cases, inconveniences such as inability to do so may occur.
本発明において、スパイラル型膜モジュールとして
は、第７図に示す如く、波板形スペーサ22が連続して延
在しかつ蛇行する波条を有することが好ましい。このよ
うなスパイラル型膜モジュールであれば、蛇行する波条
により膜面に沿う流れが攪乱される。これにより濃度分
極が解消されるようになってフラックスがより一層増大
される。しかも、原水流路は途切れることなく連続して
おり、SSも引掛かりにくく、原水流路の閉塞も防止され
る。このようなことから、比較的低い膜面流速、例えば
0.5〜1.0m/sでも、高いフラックスを維持することが可
能とされる。しかも、このような乱流促進機能を有する
波板形スペーサを備えるスパイラル型膜モジュールによ
れば、より一層高い空気の溶解効率が得られる。In the present invention, as the spiral-type membrane module, as shown in FIG. 7, it is preferable that the corrugated spacer 22 has a continuous extending and meandering wave. In such a spiral type membrane module, the flow along the membrane surface is disturbed by the meandering ripples. As a result, concentration polarization is eliminated and the flux is further increased. In addition, the raw water flow path is continuous without interruption, the SS is hardly caught, and the blockage of the raw water flow path is prevented. For this reason, a relatively low film surface velocity, for example,
Even at 0.5 to 1.0 m / s, it is possible to maintain a high flux. Moreover, according to the spiral membrane module including the corrugated spacer having the turbulence promoting function, a higher air dissolving efficiency can be obtained.
本発明の有機性廃水処理装置においては、空気の供給
と膜分離とを同時に行なうことができることから、別
途、空気の供給系路を設ける必要はないが、これを設け
ても良いことは言うまでもない。In the organic wastewater treatment apparatus of the present invention, since air supply and membrane separation can be performed simultaneously, there is no need to separately provide an air supply system, but it goes without saying that this may be provided. .
以下に具体的な実施例を挙げて、本発明をより詳細に
説明する。Hereinafter, the present invention will be described in more detail with reference to specific examples.
実施例1,比較例１ 好気性生物反応槽及び膜分離装置を用いて、酸素溶解
効率の測定を行なった。なお、各装置の仕様は下記の通
りである。Example 1, Comparative Example 1 The oxygen dissolution efficiency was measured using an aerobic biological reaction tank and a membrane separation device. The specifications of each device are as follows.
好気性生物反応槽 水深:2m 有効水量:350 膜分離装置 膜モジュール： 直径100mm、長さ1000mmのスパイラル型膜モジュー
ル。Aerobic reaction tank Water depth: 2m Effective water volume: 350 Membrane separation device Membrane module: Spiral type membrane module with diameter of 100mm and length of 1000mm.
波板形スペーサによる有効流路高さは2.5mm。 The effective flow path height of the corrugated plate spacer is 2.5mm.
即ち、第１図（実施例１）又は第４図（比較例１）に
示す如く、好気性生物反応槽１からの液をポンプＰを備
える導入用配管12を経て膜分離装置２に導入し、膜分離
装置の濃縮水を循環用配管14を経て好気性生物反応槽１
に循環させる系において、好気性生物反応槽１に市水を
投入し、N2ガスにより脱酸素した後、膜面流速1m/sで膜
分離装置２に導入するにあたり、通気倍率2VVh（好気性
生物反応槽あたりの通気倍率）で、下記第１表に示す如
く、配管15又は16（第４図ではエゼクター）より空気の
供給を行ない、溶存酸素の上昇カーブよりKLa（酸素溶
解容量係数）を求めることにより、酸素溶解効率を求め
た。That is, as shown in FIG. 1 (Example 1) or FIG. 4 (Comparative Example 1), the liquid from the aerobic biological reaction tank 1 is introduced into the membrane separation device 2 through the introduction pipe 12 having the pump P. Aerobic biological reactor 1 through the circulation pipe 14
In a system for circulating water, city water is introduced into the aerobic biological reaction tank 1, deoxygenated with N 2 gas, and then introduced into the membrane separation device 2 at a membrane surface flow rate of 1 m / s. As shown in Table 1 below, air was supplied from piping 15 or 16 (ejector in FIG. 4), and K La (oxygen dissolution capacity coefficient) was obtained from the rise curve of dissolved oxygen. To determine the oxygen dissolution efficiency.
実施例2,比較例２ 実施例１及び比較例１の装置を用いて、合成下水（ペ
プトン、グルコース基質）（BOD＝1200mg/）の連続処
理を行なった。なお、膜面流速は0.5m/sとしたこと以外
は、同条件で処理を行なった。得られたフラックスを第
２表にに示す。 Example 2, Comparative Example 2 Using the apparatus of Example 1 and Comparative Example 1, continuous treatment of synthetic sewage (peptone, glucose substrate) (BOD = 1200 mg /) was performed. The treatment was performed under the same conditions except that the membrane surface flow rate was 0.5 m / s. Table 2 shows the obtained flux.
比較例３ 実施例２において、膜分離装置の膜モジュールとし
て、集水管の外周にネット状スペーサを介して分離膜を
巻回してなる通常のスパイラル型膜モジュールを用いた
こと以外は同様にして処理を行なったところ、SSによる
目詰りで運転を継続することができなかった。 Comparative Example 3 Processing was performed in the same manner as in Example 2 except that a normal spiral-type membrane module in which a separation membrane was wound around a water collecting pipe with a net-shaped spacer interposed therebetween was used as the membrane module of the membrane separation device. The operation could not be continued because of clogging by SS.
以上の結果から、本発明の有機性廃水処理装置によれ
ば、フラックスの増大と同時に好気性生物処理への酸素
の有効利用が図れることが明らかである。From the above results, it is clear that according to the organic wastewater treatment apparatus of the present invention, it is possible to effectively utilize oxygen for aerobic biological treatment while increasing the flux.
実施例３ 実施例２において、通気量を変えて連続処理を行な
い、通気量とフラックスとの関係を調べ、結果を第６図
に示した。Example 3 In Example 2, continuous processing was performed by changing the air flow rate, and the relationship between the air flow rate and the flux was examined. The results are shown in FIG.
なお、好気性生物反応槽には別途過剰量の通気を行な
い、ポンプ吸込み側の通気量を変えても溶存酸素濃度等
に影響がでないようにして行なった。The aerobic biological reaction tank was separately ventilated with an excessive amount of gas so that the concentration of dissolved oxygen and the like were not affected even if the amount of ventilation on the pump suction side was changed.
第６図より明らかなように、（通気量／送水量）×10
0の割合（体積比）が５〜10％の範囲でフラックスの良
好な回復効果が認められる。なお、この割合が10％を超
えてもフラックスの著しい回復効果は認められず、一
方、配管等の振動等が増加し、好ましい運転状態を維持
できないことが判明した。As is clear from FIG. 6, (aeration amount / water supply amount) × 10
When the ratio of 0 (volume ratio) is in the range of 5 to 10%, a good effect of recovering the flux is observed. Note that even if this ratio exceeds 10%, no remarkable effect of flux recovery was observed, while on the other hand, the vibrations of the pipes and the like increased, and it was found that a favorable operation state could not be maintained.
［発明の効果 以上詳述した通り、本発明の有機性廃水処理装置によ
れば、装置全体のエネルギー効率の向上、好気性生物反
応処理への空気の有効利用、酸素溶解効率の向上、膜分
離装置のフラックスの向上、膜面へのゲル層の生成抑制
及び目詰り防止が達成される。従って、有機性廃水の処
理をより一層低コストにかつ効率的に行なうことが可能
とされる。[Effects of the Invention As described in detail above, according to the organic wastewater treatment apparatus of the present invention, the energy efficiency of the entire apparatus can be improved, the air can be effectively used for aerobic biological reaction treatment, the oxygen dissolution efficiency can be improved, and the membrane separation can be performed. Improvement of the flux of the apparatus, suppression of formation of a gel layer on the film surface, and prevention of clogging are achieved. Therefore, the treatment of the organic wastewater can be performed at a lower cost and more efficiently.
第１図は本発明の有機性廃水処理装置の概略を示す系統
図、第２図及び第３図は本発明の有機性廃水処理装置の
実施例を示す系統図、第４図はエゼクター構造の一例を
示す断面図、第５図は従来例を示す系統図、第６図は実
施例３の結果を示すグラフ、第７図はスパイラル型膜モ
ジュールの一例を示す組立斜視図である。 １……好気性生物反応槽、 ２……膜分離装置、 2B……スパイラル型膜モジュール。FIG. 1 is a system diagram showing an outline of an organic wastewater treatment apparatus of the present invention, FIGS. 2 and 3 are system diagrams showing an embodiment of an organic wastewater treatment apparatus of the present invention, and FIG. FIG. 5 is a sectional view showing an example, FIG. 5 is a system diagram showing a conventional example, FIG. 6 is a graph showing the results of Example 3, and FIG. 7 is an assembly perspective view showing an example of a spiral membrane module. 1 ... aerobic biological reactor, 2 ... membrane separation device, 2B ... spiral type membrane module.
───────────────────────────────────────────────────── フロントページの続き (58)調査した分野(Int.Cl.7，ＤＢ名) C02F 3/12 B01D 63/10 C02F 1/44 C02F 9/00 501 ──────────────────────────────────────────────────続 き Continued on the front page (58) Field surveyed (Int. Cl. 7 , DB name) C02F 3/12 B01D 63/10 C02F 1/44 C02F 9/00 501
Claims (1)
性生物反応槽と、該好気性生物反応槽の処理液を膜分離
処理する膜分離装置と、該好気性生物反応槽の処理液を
膜分離装置に導入するためのポンプを有する導入用配管
とを備え、該膜分離装置の濃縮水を好気性生物反応槽に
戻すようにした有機性廃水処理装置において、該導入用
配管のポンプの吸込み側に空気を供給する空気供給手段
を設け、かつ、前記膜分離装置の膜モジュールとして、
集水管の外周に波板形のスペーサを介して分離膜を巻回
してなるスパイラル型膜モジュールを用いたことを特徴
とする有機性廃水処理装置。An aerobic biological reaction tank for treating an organic wastewater with an aerobic biological reaction, a membrane separation device for performing a membrane separation treatment of a treatment liquid in the aerobic biological reaction tank, and a treatment liquid for the aerobic biological reaction tank An introduction pipe having a pump for introducing the water into the membrane separation apparatus, wherein the concentrated water of the membrane separation apparatus is returned to the aerobic biological reaction tank. Air supply means for supplying air to the suction side of, and, as a membrane module of the membrane separation device,
An organic wastewater treatment apparatus characterized by using a spiral-wound membrane module in which a separation membrane is wound around the outer periphery of a water collecting pipe via a corrugated spacer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP20094190A JP3111463B2 (en) | 1990-07-27 | 1990-07-27 | Organic wastewater treatment equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP20094190A JP3111463B2 (en) | 1990-07-27 | 1990-07-27 | Organic wastewater treatment equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0487695A JPH0487695A (en) | 1992-03-19 |
| JP3111463B2 true JP3111463B2 (en) | 2000-11-20 |
Family
ID=16432845
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP20094190A Expired - Lifetime JP3111463B2 (en) | 1990-07-27 | 1990-07-27 | Organic wastewater treatment equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3111463B2 (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TWI222895B (en) * | 1998-09-25 | 2004-11-01 | Usf Filtration & Separations | Apparatus and method for cleaning membrane filtration modules |
| JP4599633B2 (en) * | 1999-04-15 | 2010-12-15 | 栗田工業株式会社 | Membrane separator |
| JP2007136387A (en) * | 2005-11-21 | 2007-06-07 | Ngk Insulators Ltd | Membrane separation activated sludge treatment system for waste water |
| JP4911730B2 (en) * | 2008-12-22 | 2012-04-04 | 旭化成ケミカルズ株式会社 | Organic wastewater treatment method |
| CN111732186B (en) * | 2020-08-27 | 2020-11-06 | 湖南叶之能科技有限公司 | Roll type membrane aeration bioreactor and preparation method thereof |
-
1990
- 1990-07-27 JP JP20094190A patent/JP3111463B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0487695A (en) | 1992-03-19 |
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