JPS61287500A - Treatment of liquid containing organic substance - Google Patents
Treatment of liquid containing organic substanceInfo
- Publication number
- JPS61287500A JPS61287500A JP60127755A JP12775585A JPS61287500A JP S61287500 A JPS61287500 A JP S61287500A JP 60127755 A JP60127755 A JP 60127755A JP 12775585 A JP12775585 A JP 12775585A JP S61287500 A JPS61287500 A JP S61287500A
- Authority
- JP
- Japan
- Prior art keywords
- liq
- reaction tank
- membrane
- liquid
- vessel
- 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.)
- Pending
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
- Treatment Of Biological Wastes In General (AREA)
- Biological Treatment Of Waste Water (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【発明の詳細な説明】
[産業上の利用分野]
本発明は有機性物質含有液の処理方法に関し、詳細には
他の有価物質に変換し得る有機性基質を含む液体を処理
する方法に関するものである。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a method for treating a liquid containing an organic substance, and more particularly, to a method for treating a liquid containing an organic substrate that can be converted into other valuable substances. It is.
[従来の技術]
例えばパルプ廃液等の様な他の有価物質に変換し得る基
質を含む液体を処理する方法の一例として、該廃液中に
含まれている有機性物質を微生物によって分解する方法
が知られている。該方法では、新たに生成した有価物質
を母液から分離することの必要性から有価物質分離手段
を付加しなければならない。しかるに該有価物質は一般
に低分子液状物質であり、パルプ廃液の如き原料物質は
高分子液状乃至固形物質であるから、これらの分離手段
としては逆浸透法や限外濾過法等の膜分離技術の利用が
有効であると考えられる。[Prior Art] As an example of a method for treating a liquid containing a substrate that can be converted into other valuable substances, such as pulp waste liquid, there is a method in which organic substances contained in the waste liquid are decomposed by microorganisms. Are known. In this method, a means for separating valuable substances must be added because it is necessary to separate newly produced valuable substances from the mother liquor. However, these valuable substances are generally low-molecular liquid substances, and raw materials such as pulp waste liquid are high-molecular liquid or solid substances, so membrane separation techniques such as reverse osmosis and ultrafiltration are used as means for separating them. It is considered that its use is effective.
第2図は、従来の典型的処理システムAを示すフロー説
明図である。該システムAでは、処理されるべき原料は
管路5を介して反応槽lに導かれる。該原料としては、
例えばパルプ廃液に含まれるセルロースを糖化した後の
グルコース含有液が例示され、以下グルコース含有液を
原料とする場合を採り上げて説明する。反応槽1には、
管路12を介して空気が供給され、好気性条件となって
いるので、反応槽1内に導かれた原料は、反応槽l内の
担体(図示せず)に相持された酵母によって好気発酵さ
れエタノール等が生成する。生成したエタノール含有液
(未反応のグルコース等を含む)は、管路6を通って水
槽2に導入される。該水槽2には流量調整弁7によって
流量が調整された水が供給され、前記反応槽l内で生成
したエタノール等は水槽2内で木によって希釈され、エ
タノール等の有価物は膜分離が容易な状態となる。水槽
2からは高圧ポンプ8によってエタノール等が加圧状態
で引出され、管路9を介して膜分離装置3の濃縮液側に
導入される。膜分離装置3はエタノール等の低分子有価
物が透過液として分離され、該透過液は管路10を介し
て貯留槽4に貯留される。また膜分離装置3は、濃縮液
側の加圧液が廃水管11を介して大気圧下に取出され、
残圧を開放した状態で廃棄又はその他の適当な処分に付
される。FIG. 2 is a flow explanatory diagram showing a conventional typical processing system A. In said system A, the raw material to be treated is led via line 5 to reaction vessel l. The raw materials include:
For example, a glucose-containing liquid obtained by saccharifying cellulose contained in pulp waste liquid is exemplified, and the case where the glucose-containing liquid is used as a raw material will be explained below. In reaction tank 1,
Since air is supplied through the pipe line 12 and the conditions are aerobic, the raw materials introduced into the reaction tank 1 are subjected to aerobic conditions by the yeast supported on the carrier (not shown) in the reaction tank 1. It is fermented and ethanol etc. are produced. The generated ethanol-containing liquid (containing unreacted glucose, etc.) is introduced into the water tank 2 through the pipe 6. Water whose flow rate is adjusted by a flow rate regulating valve 7 is supplied to the water tank 2, and the ethanol etc. produced in the reaction tank 1 are diluted with wood in the water tank 2, and valuable substances such as ethanol can be easily separated by membrane. It becomes a state. Ethanol or the like is drawn out under pressure from the water tank 2 by a high-pressure pump 8 and introduced into the concentrate side of the membrane separation device 3 via a pipe 9. The membrane separator 3 separates low molecular weight substances such as ethanol as a permeated liquid, and the permeated liquid is stored in a storage tank 4 via a pipe line 10. Further, in the membrane separator 3, the pressurized liquid on the concentrate side is taken out under atmospheric pressure via the waste water pipe 11,
Disposed of or subjected to other appropriate disposal with the residual pressure released.
[発明が解決しようとする問題点]
上記した膜分離技術では水槽2内の被処理液を高圧ポン
プ8によって加圧した状態で膜分離装置3に導入するが
、透過を済ませた後の残圧保有濃縮液は該残圧をしない
ま覧で放棄しているのが現状である。この様な膜分離技
術については、従来から逆浸透法或は限外濾過法等と呼
ばれて区別されているが、それらの名称の間には本質的
な差異はなく、残圧放棄という面から把握するならば、
少なくとも定性的には全く同一・である。但し逆浸透膜
法では低分子溶質を高分子物質や塩類等と分離するのを
目的としている為著しい高圧を必要とするという特性が
あり、従って−に述した現状の欠点は、逆浸透膜法にお
いて特に顕著なものとして認識される。[Problems to be Solved by the Invention] In the membrane separation technology described above, the liquid to be treated in the water tank 2 is introduced into the membrane separation device 3 in a pressurized state by the high-pressure pump 8, but the residual pressure after permeation is Currently, the retained concentrate is discarded without checking the residual pressure. Such membrane separation technology has traditionally been distinguished by being called reverse osmosis or ultrafiltration, but there is no essential difference between these names; If you understand from
At least qualitatively, they are exactly the same. However, since the reverse osmosis membrane method aims to separate low-molecular solutes from high-molecular substances, salts, etc., it has the characteristic of requiring extremely high pressure. It is recognized as particularly remarkable.
更に反応槽lに関して述べると、反応槽1内に高濃度の
菌体を保持する方式として古くは浮遊方式が主流を占め
ていたが、菌体を担持した担体を反応槽l内で固定的に
保持する所謂固定床方式が近年に至って発達し、更に担
体と原料との接触機会を多くする目的で担体を反応槽1
内で流動させる所謂流動床方式等が提出されるに至って
いる。Furthermore, regarding the reaction tank 1, in the past, the floating method was the mainstream method for maintaining high concentration of bacterial cells in the reaction tank 1, but in the past, the carrier carrying the bacteria was fixed in the reaction tank 1. In recent years, the so-called fixed bed method of holding the carrier has developed, and in order to increase the chances of contact between the carrier and the raw material, the carrier is placed in a reaction tank 1.
So-called fluidized bed methods have been proposed.
該方式は従来の浮遊方式や固定床方式等と比べて反応槽
l内における反応が迅速に行なわれるという利点はある
けれども、担体を反応槽l内で流動させる為の循環ポン
プ(図示せず)等を動力源として使用する必要があり、
従来方式と比べて設備コストやエネルギーコストが大き
いという新たな問題が生じる。Although this method has the advantage that the reaction in the reaction tank 1 can be carried out quickly compared to the conventional floating method or fixed bed method, etc., it requires a circulation pump (not shown) to flow the carrier in the reaction tank 1. etc. must be used as a power source,
A new problem arises in that equipment costs and energy costs are higher than in conventional methods.
本発明は上記現状に鑑みなされたものであって、従来で
は利用されないままで廃棄されていた残圧を有効に利用
することにより、今まで必要とされていた動力の低減を
図ることのできる有機性物質含有液の処理方法を提供す
ることをその目的とするものである。The present invention was made in view of the above-mentioned current situation, and is an organic material that can reduce the power required up until now by effectively utilizing the residual pressure that was conventionally discarded without being utilized. The object of the present invention is to provide a method for treating a liquid containing a sexual substance.
[問題点を解決する為の手段]
本発明は、反応槽と膜分離装置とが該記載順序で配置さ
れ、有機性物質含有液を上記反応槽に導いて生化学的反
応を行ない、1;記反応槽から取出される反応処理液を
」;記数分離装置に加圧状態で導いて低分子有価物を透
過液側に膜分離することにより有機性物質を処理する方
法において、上記反応槽内には菌体を担持した担体が流
動可能に装入されると共に、上記膜分離装置の濃縮液側
から回収される加圧濃縮液を上記反応槽に返還する点に
要旨を有するものである。[Means for Solving the Problems] According to the present invention, a reaction tank and a membrane separation device are arranged in the above described order, and an organic substance-containing liquid is introduced into the reaction tank to perform a biochemical reaction, 1; In a method for treating organic substances by introducing the reaction treated liquid taken out from the reaction tank under pressure into a separation device and separating low-molecular valuables into the permeate side with a membrane, The main feature is that a carrier carrying bacterial cells is charged in a fluidized manner, and the pressurized concentrated liquid recovered from the concentrated liquid side of the membrane separation device is returned to the reaction tank. .
[作用1
有機性物質含有液に菌体を作用させて生成した反応生成
物を利用する各種技術は、第2図に示したように従来か
ら開発されている。本発明の基本的構成は従来システム
A(第2図)と特に変わる所はないが、本発明者等は循
環ポンプ等を駆動さ 1せるための動力費を低減すると
いう目的を、従来廃棄されていた濃縮液側の残圧を利用
するという技術的手段によって達成するという指針を立
て、これに基づいて種々検討を行ない本発明を完成する
に至った。[Action 1 Various techniques have been developed in the past, as shown in FIG. 2, that utilize reaction products produced by the action of bacterial cells on an organic substance-containing liquid. Although the basic configuration of the present invention is not particularly different from the conventional system A (Fig. 2), the inventors of the present invention aimed to reduce the power cost for driving circulation pumps, etc., which was previously abandoned. Based on this guideline, the present invention was completed after conducting various studies.
本発明では、上述の如き構成を採用することによって、
従来利用されずに廃棄されていた濃縮液側の残圧を有効
に利用することができると共に、反応槽を流動床式にす
る為に必要とされていた動力の低減を図ることが可能と
なった。In the present invention, by adopting the above configuration,
It is now possible to effectively utilize the residual pressure on the concentrate side, which was previously unused and discarded, and it is also possible to reduce the power required to make the reaction tank a fluidized bed type. Ta.
以下、本発明を第1図を用いて更に詳細に説明する。Hereinafter, the present invention will be explained in more detail using FIG.
[実施例]
第1図は、本発明の実施態様の一例を示すフロー説明図
である。本システムBの基本的構成は従来システムAと
同様であり、対応する部分に同一の参照符号を付すこと
により重複説明を回避する。第1図において注目すべき
点は、本システムBは膜分離装置3の濃縮液側から排出
された加圧液を反応槽lに返還するための返送路15を
設けた点である。該返送路15は膜分離装置3の濃縮液
側と反応槽lとを連結しており、濃縮液側の加圧液は残
圧を保持した状態で反応槽1に返還される。このことに
よって、従来利用されずに廃棄されていた残圧を有効に
利用することができると共に、反応槽1内に流動床を形
成するために必要とされていた循環ポンプ等の動力源を
別途設ける必要がなくなり、従って動力費の低減を図る
ことができるようになる。[Example] FIG. 1 is a flow explanatory diagram showing an example of an embodiment of the present invention. The basic configuration of the present system B is the same as that of the conventional system A, and corresponding parts are given the same reference numerals to avoid redundant explanation. What should be noted in FIG. 1 is that this system B is provided with a return path 15 for returning the pressurized liquid discharged from the concentrated liquid side of the membrane separation device 3 to the reaction tank 1. The return path 15 connects the concentrate side of the membrane separation device 3 and the reaction tank 1, and the pressurized liquid on the concentrate side is returned to the reaction tank 1 while maintaining residual pressure. This makes it possible to effectively utilize the residual pressure that was previously unused and wasted, and to separate the power source for the circulation pump, etc. that was required to form the fluidized bed in the reaction tank 1. There is no need to provide one, so it is possible to reduce power costs.
返送路15には流量調整弁18が介在されており、反応
槽lに返還される加圧液の流量は、この流量調整弁18
によって調整される。また返送路15から分岐するバイ
パス管17を設け、前記水槽2に濃縮側の加圧液を供給
するようにしてもよい。該バイパス管17には、流量調
整弁16が介在され、該流量調整弁16によって水槽2
に返還される加圧液の流量が調整される。該バイパス管
17は、膜分離装置3の膜表面における線速度を増加し
て該膜表面への固形分付着を防止する目的で設けられる
ものであり、水槽2から膜分離装置3に供給される水量
を調整することによって上記目的を達成する。A flow rate adjustment valve 18 is interposed in the return path 15, and the flow rate of the pressurized liquid returned to the reaction tank l is controlled by this flow rate adjustment valve 18.
adjusted by. Further, a bypass pipe 17 branching from the return path 15 may be provided to supply pressurized liquid on the concentration side to the water tank 2. A flow rate adjustment valve 16 is interposed in the bypass pipe 17, and the water tank 2 is controlled by the flow rate adjustment valve 16.
The flow rate of the pressurized fluid returned to is adjusted. The bypass pipe 17 is provided for the purpose of increasing the linear velocity on the membrane surface of the membrane separator 3 to prevent solid content from adhering to the membrane surface, and is used to supply water from the water tank 2 to the membrane separator 3. The above objective is achieved by adjusting the amount of water.
−L述の実施例では、パルプ廃液を糖化した後のグルコ
ース等を含む液体をエタノール含有液等に変換させる場
合に関して述べたけれども、本発明の精神に従えば、本
発明パルプ廃液を処理する場合に限らず、し尿などの都
市廃水を処理する場合等においても好適に実施すること
ができる。従って前述した実施例では、反応槽lは好気
的反応を行なうものとして説明したが、管路12を設け
ずに反応槽1内で嫌気的反応が行なわれるように構成さ
れても良いのは勿論である。- In the embodiment described above, the case was described in which a liquid containing glucose etc. after saccharification of pulp waste liquid was converted into an ethanol-containing liquid etc. However, according to the spirit of the present invention, when treating the pulp waste liquid of the present invention It can be suitably implemented not only when treating urban wastewater such as human waste, but also when treating urban wastewater such as human waste. Therefore, in the above-mentioned embodiment, the reaction tank 1 was described as one that performs an aerobic reaction, but it is also possible to configure the reaction tank 1 so that an anaerobic reaction is performed without providing the pipe line 12. Of course.
[発明の効果]
以−に述べた如く本発明によれば、従来利用されずに廃
棄されていた濃縮液側に残存する圧力を有効に利用する
ことができると共に、流動床を形成する一Lで必要とさ
れていた動力費の低減を図ることが可能となった[Effects of the Invention] As described above, according to the present invention, it is possible to effectively utilize the pressure remaining on the concentrated liquid side, which was conventionally unused and discarded, and to reduce the pressure of one liter to form a fluidized bed. It became possible to reduce the power costs that were required in
第1図は本発明の実施態様の一例を示すフロー説明図、
第2図は従来の典型的処理システムAを示すフロー説明
図である。FIG. 1 is a flow explanatory diagram showing an example of an embodiment of the present invention,
FIG. 2 is a flow explanatory diagram showing a conventional typical processing system A.
Claims (1)
物質含有液を上記反応槽に導いて生化学的反応を行ない
、上記反応槽から取出された反応処理液を上記膜分離装
置に加圧状態で導いて低分子有価物を透過液側に膜分離
することにより有機性物質含有液を処理する方法におい
て、上記反応槽内には菌体を担持した担体が流動可能に
装入されると共に、上記膜分離装置の濃縮液側から回収
される加圧濃縮液を上記反応槽に返還することを特徴と
する有機性物質含有液の処理方法。A reaction tank and a membrane separation device are arranged in the stated order, an organic substance-containing liquid is introduced into the reaction tank to perform a biochemical reaction, and a reaction-treated liquid taken out from the reaction tank is transferred to the membrane separation device. In a method of treating an organic substance-containing liquid by introducing it under pressure and separating low-molecular-weight valuables into the permeate side through a membrane, a carrier carrying bacterial cells is charged into the reaction tank in a flowable manner. A method for treating an organic substance-containing liquid, characterized in that the pressurized concentrated liquid recovered from the concentrated liquid side of the membrane separation device is returned to the reaction tank.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP60127755A JPS61287500A (en) | 1985-06-12 | 1985-06-12 | Treatment of liquid containing organic substance |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP60127755A JPS61287500A (en) | 1985-06-12 | 1985-06-12 | Treatment of liquid containing organic substance |
Publications (1)
Publication Number | Publication Date |
---|---|
JPS61287500A true JPS61287500A (en) | 1986-12-17 |
Family
ID=14967887
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP60127755A Pending JPS61287500A (en) | 1985-06-12 | 1985-06-12 | Treatment of liquid containing organic substance |
Country Status (1)
Country | Link |
---|---|
JP (1) | JPS61287500A (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0861808A2 (en) * | 1997-02-28 | 1998-09-02 | Kuraray Co., Ltd. | Waste water treatment apparatus |
-
1985
- 1985-06-12 JP JP60127755A patent/JPS61287500A/en active Pending
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0861808A2 (en) * | 1997-02-28 | 1998-09-02 | Kuraray Co., Ltd. | Waste water treatment apparatus |
US6007712A (en) * | 1997-02-28 | 1999-12-28 | Kuraray Co., Ltd. | Waste water treatment apparatus |
EP0861808A3 (en) * | 1997-02-28 | 2001-06-20 | Kuraray Co., Ltd. | Waste water treatment apparatus |
KR100496722B1 (en) * | 1997-02-28 | 2005-09-13 | 가부시키가이샤 구라레 | Wastewater treatment unit |
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