JPH10230295A - Water treating apparatus - Google Patents
Water treating apparatusInfo
- Publication number
- JPH10230295A JPH10230295A JP11802497A JP11802497A JPH10230295A JP H10230295 A JPH10230295 A JP H10230295A JP 11802497 A JP11802497 A JP 11802497A JP 11802497 A JP11802497 A JP 11802497A JP H10230295 A JPH10230295 A JP H10230295A
- Authority
- JP
- Japan
- Prior art keywords
- tank
- ozone
- water treatment
- treatment apparatus
- solubilization
- 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
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 24
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 90
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 65
- 239000007787 solid Substances 0.000 claims abstract description 52
- 238000006243 chemical reaction Methods 0.000 claims abstract description 49
- 239000002351 wastewater Substances 0.000 claims abstract description 28
- 238000000855 fermentation Methods 0.000 claims abstract description 26
- 230000004151 fermentation Effects 0.000 claims abstract description 26
- 230000003381 solubilizing effect Effects 0.000 claims abstract description 6
- 238000005063 solubilization Methods 0.000 claims description 37
- 230000007928 solubilization Effects 0.000 claims description 37
- 102000004190 Enzymes Human genes 0.000 claims description 23
- 108090000790 Enzymes Proteins 0.000 claims description 23
- 238000000926 separation method Methods 0.000 claims description 18
- 239000007788 liquid Substances 0.000 claims description 12
- 239000012528 membrane Substances 0.000 claims description 10
- 239000010802 sludge Substances 0.000 claims description 10
- 238000002156 mixing Methods 0.000 claims description 4
- 230000005484 gravity Effects 0.000 claims 1
- 229940088598 enzyme Drugs 0.000 description 22
- 241000894006 Bacteria Species 0.000 description 7
- 239000012295 chemical reaction liquid Substances 0.000 description 6
- 238000010586 diagram Methods 0.000 description 6
- 239000002253 acid Substances 0.000 description 5
- 244000005700 microbiome Species 0.000 description 3
- 210000000805 cytoplasm Anatomy 0.000 description 2
- 230000029087 digestion Effects 0.000 description 2
- 238000011038 discontinuous diafiltration by volume reduction Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 2
- 108010059892 Cellulase Proteins 0.000 description 1
- 108091005804 Peptidases Proteins 0.000 description 1
- 239000004365 Protease Substances 0.000 description 1
- 102100037486 Reverse transcriptase/ribonuclease H Human genes 0.000 description 1
- 238000005276 aerator Methods 0.000 description 1
- 210000004027 cell Anatomy 0.000 description 1
- 210000002421 cell wall Anatomy 0.000 description 1
- 229940106157 cellulase Drugs 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000007790 scraping Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Physical Water Treatments (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、有機性固形物を含
む廃水を適切に処理することができる水処理装置に関す
る。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a water treatment apparatus capable of appropriately treating wastewater containing organic solids.
【０００２】[0002]
【従来の技術】従来、下水の余剰汚泥等、有機性固形物
を含む廃水は、脱水後、その固形物が焼却、埋め立てな
どによって処分されたり、嫌気性菌の作用により消化・
減容後、脱水し、焼却、埋め立てされている。しかし、
処理場用地の不足による処理費用の高騰、海上投棄禁止
の動きなどから新たな処分方法の開発が望まれている。2. Description of the Related Art Conventionally, wastewater containing organic solids, such as excess sludge of sewage, is dewatered, then the solids are disposed of by incineration or landfill, or digested by the action of anaerobic bacteria.
After volume reduction, it is dehydrated, incinerated and landfilled. But,
Development of new disposal methods has been desired due to rising disposal costs due to shortage of land for treatment plants and the ban on marine dumping.
【０００３】また、廃水に対しては嫌気性菌の作用によ
る消化・減容が行なわれるが、この消化・減容作用は、
反応時間が長く、１００日程度の日数を要し、通常は大
型の処理施設が用いられている。[0003] Wastewater undergoes digestion and volume reduction by the action of anaerobic bacteria.
The reaction time is long, takes about 100 days, and usually a large-scale treatment facility is used.
【０００４】[0004]
【発明が解決しようとする課題】上述のように従来の廃
水は脱水され、その後焼却、埋め立て、消化されている
が、効果的かつ高速に廃水を処理することができれば、
処分場用地の不足を解消して迅速な処理を行なうことが
できて好ましい。As described above, conventional wastewater is dehydrated and then incinerated, landfilled and digested. However, if wastewater can be treated effectively and at high speed,
It is preferable because the shortage of the land for the disposal site can be resolved and quick processing can be performed.
【０００５】本発明はこのような点を考慮してなされた
ものであり、大きな処分場用地を必要とせず、迅速な処
理を行なうことができる水処理装置を提供することを目
的とする。[0005] The present invention has been made in view of such a point, and an object of the present invention is to provide a water treatment apparatus capable of performing rapid treatment without requiring a large landfill site.
【０００６】[0006]
【課題を解決するための手段】本発明は、有機性固形分
を含む廃水とオゾンとを混合反応させて反応液を生成す
るオゾン反応槽と、オゾン反応槽からの反応液をメタン
発酵させるメタン発酵槽とを備えたことを特徴とする水
処理装置である。SUMMARY OF THE INVENTION The present invention provides an ozone reactor for producing a reaction solution by mixing and reacting wastewater containing organic solids with ozone, and a methane for methane fermenting the reaction solution from the ozone reactor. A water treatment apparatus comprising a fermenter.
【０００７】本発明によれば、有機性固形分を含む廃水
とオゾンとはオゾン反応槽内において混合反応し、オゾ
ン反応槽からの反応液はメタン発酵槽内でメタン発酵し
て浄化される。According to the present invention, waste water containing organic solids and ozone undergo a mixed reaction in the ozone reaction tank, and the reaction solution from the ozone reaction tank is purified by methane fermentation in the methane fermentation tank.
【０００８】[0008]
【発明の実施の形態】以下、図面を参照して本発明の実
施の形態について説明する。図１は本発明による水処理
装置の一実施の形態を示す図である。Embodiments of the present invention will be described below with reference to the drawings. FIG. 1 is a diagram showing an embodiment of a water treatment apparatus according to the present invention.
【０００９】図１に示すように、水処理装置はオゾンを
発生するオゾナイザ１と、有機性固形分を含む廃水とオ
ゾナイザ１からのオゾンとを混合反応させるオゾン反応
槽２とを備えている。またオゾン反応槽２の下流側に、
オゾン反応槽２からの反応液を可溶化反応させて低分子
化する可溶化槽３が配置されるとともに、可溶化槽３の
下流側に、低分子化した反応液をメタン発酵させるメタ
ン発酵槽４が配置されている。As shown in FIG. 1, the water treatment apparatus includes an ozonizer 1 for generating ozone, and an ozone reactor 2 for mixing and reacting wastewater containing organic solids and ozone from the ozonizer 1. Also, on the downstream side of the ozone reactor 2,
A solubilization tank 3 for solubilizing the reaction liquid from the ozone reaction tank 2 to reduce the molecular weight is disposed, and a methane fermentation tank for methane fermenting the reduced molecular weight reaction liquid downstream of the solubilization tank 3. 4 are arranged.
【００１０】次にこのような構成からなる本実施の形態
の作用について説明する。図１において有機性の固形物
を含む廃水は、オゾナイザ１から発生されるオゾンとオ
ゾン反応槽２において混合・反応される。Next, the operation of this embodiment having the above-described configuration will be described. In FIG. 1, wastewater containing organic solid matter is mixed and reacted with ozone generated from an ozonizer 1 in an ozone reaction tank 2.
【００１１】オゾン反応槽２において、廃水中の固形物
は、オゾンの作用をうけ、細胞壁などの原形質が直接破
壊され、低分子化しやすい状態に処理される。次いで、
オゾン処理された反応液は、可溶化槽３に送られ、ここ
で微生物や酵素などの作用により、可溶化され、更に、
酸発酵を受け、低分子化する。可溶化された反応液は、
メタン発酵槽４でメタン菌の作用により分解され、浄化
される。In the ozone reaction tank 2, the solids in the wastewater are subjected to the action of ozone, and the protoplasm such as the cell wall is directly destroyed, so that the solids are easily reduced to a low molecular weight. Then
The ozone-treated reaction solution is sent to the solubilization tank 3, where it is solubilized by the action of microorganisms, enzymes, and the like.
It undergoes acid fermentation and becomes low molecular. The solubilized reaction solution is
In the methane fermenter 4, it is decomposed and purified by the action of methane bacteria.
【００１２】本実施の形態によれば、廃水中の固形分を
オゾン反応槽２においてオゾンによって低分子化しやす
い状態にすることができ、可溶化槽３で可溶化して低分
子化することができる。さらにメタン発酵槽４において
反応液を分解、浄化するので、廃水を迅速に処理するこ
とができ、固形物量を減少させることができる。According to this embodiment, the solid content in the wastewater can be easily reduced to low molecular weight by ozone in the ozone reaction tank 2, and can be solubilized in the solubilization tank 3 to reduce the molecular weight. it can. Furthermore, since the reaction solution is decomposed and purified in the methane fermentation tank 4, the wastewater can be quickly treated, and the amount of solids can be reduced.
【００１３】ここで、オゾン反応槽２は、オゾンと廃水
中の有機性固形物が充分に混合、反応されれば、いかな
る型式の反応槽でも良い。また、可溶化槽３は、生物化
学的に有機性固形物の処理が可能であれば良く、いかな
るタイプの発酵槽でも良い。更に、メタン発酵槽４は、
メタン菌の作用により有機物を分解処理が可能であれば
良く、いかなるタイプのメタン発酵槽でも良い。Here, the ozone reactor 2 may be any type of reactor as long as ozone and organic solids in the wastewater are sufficiently mixed and reacted. The solubilization tank 3 may be any type of fermentation tank as long as it can biochemically treat organic solids. Further, the methane fermenter 4
Any type of methane fermentation tank may be used as long as organic substances can be decomposed by the action of methane bacteria.
【００１４】次に図２により本発明の第２の実施の形態
について説明する。図２に示す第２の実施の形態は、可
溶化槽３とメタン発酵槽４との間に反応液中の未分解固
形分を分離回収する固液分離槽５を設けたものであり、
他は図１に示す第１の実施の形態と略同一である。Next, a second embodiment of the present invention will be described with reference to FIG. In the second embodiment shown in FIG. 2, a solid-liquid separation tank 5 for separating and collecting undecomposed solid components in a reaction solution is provided between a solubilization tank 3 and a methane fermentation tank 4.
The other parts are substantially the same as the first embodiment shown in FIG.
【００１５】図２において、有機性の固形物を含む廃水
は、オゾナイザ１から発生するオゾンとオゾン反応槽２
において混合、反応される。オゾン反応槽２においてオ
ゾンにより低分子化されやすい状態にされた固形物は、
可溶化槽３に送られ、可溶化、酸発酵を受け低分子化さ
れる。可溶化された反応液は、メタン発酵槽４でメタン
菌の作用により分解され、浄化される。In FIG. 2, waste water containing organic solids is produced by mixing ozone generated from an ozonizer 1 with ozone reaction tank 2.
Are mixed and reacted. In the ozone reaction tank 2, the solid matter that is easily degraded by ozone is
It is sent to the solubilization tank 3 and subjected to solubilization and acid fermentation to be reduced in molecular weight. The solubilized reaction solution is decomposed and purified by the action of methane bacteria in the methane fermenter 4.
【００１６】この場合、可溶化槽２において固形物は、
低分子化されるが、一部未分解の状態で、メタン発酵槽
４に流入してしまうことがある。そのために、反応液の
浄化が不充分となってしまうことが生じ得る。そこで、
一部未分解の固形物をメタン発酵槽４の前段で、固液分
離槽５により回収し、可溶化槽３に戻して再度可溶化槽
３で処理する。このことにより固形物の処理効率が向上
し、これにより、固形物の処理効率を向上させることが
可能となる。In this case, the solid matter in the solubilization tank 2
Although it is reduced in molecular weight, it may flow into the methane fermentation tank 4 in a partially undecomposed state. Therefore, the purification of the reaction solution may be insufficient. Therefore,
Partially undecomposed solid matter is collected by a solid-liquid separation tank 5 before the methane fermentation tank 4, returned to the solubilization tank 3, and treated again in the solubilization tank 3. As a result, the processing efficiency of the solids is improved, and thereby the processing efficiency of the solids can be improved.
【００１７】ここで、この固液分離槽５は、固体と液体
とが分離できるものであれば、いかなる型式のものでも
良い。例えば、連続式遠心分離機などを用いることがで
きるが、使用する固液分離槽５の型式は、分離対象とな
る固形物の物理性状等によって決めることが望ましい。The solid-liquid separation tank 5 may be of any type as long as it can separate a solid and a liquid. For example, a continuous centrifugal separator or the like can be used, but the type of the solid-liquid separation tank 5 to be used is desirably determined according to the physical properties of the solid to be separated.
【００１８】次に図３により本発明の第３の実施の形態
について説明する。図３に示す第３の実施の形態は、固
液分離槽５が膜分離装置からなっている点が異なるのみ
であり、他は図２に示す第２の実施の形態と略同一であ
る。Next, a third embodiment of the present invention will be described with reference to FIG. The third embodiment shown in FIG. 3 is different from the second embodiment shown in FIG. 2 only in that the solid-liquid separation tank 5 is formed of a membrane separation device.
【００１９】図３において、有機性の固形物を含む廃水
は、オゾナイザ１から発生されるオゾンとオゾン反応槽
２において、混合、反応される。オゾン反応槽２で、オ
ゾンの作用で低分子化されやすい状態にされた固形物
は、可溶化槽３に送られ、この可溶化槽３において可溶
化、酸発酵を受け、低分子化される。可溶化された反応
液は、メタン発酵槽４でメタン菌の作用により分解さ
れ、浄化される。In FIG. 3, waste water containing organic solids is mixed and reacted in the ozone reaction tank 2 with ozone generated from the ozonizer 1. In the ozone reaction tank 2, the solid matter that is easily reduced to a low molecular weight by the action of ozone is sent to a solubilization tank 3, where the solid is subjected to solubilization and acid fermentation to reduce the molecular weight. . The solubilized reaction solution is decomposed and purified by the action of methane bacteria in the methane fermenter 4.
【００２０】ここで、可溶化槽２で固形物は、低分子化
されるが、一部未分解の状態で、メタン発酵槽４に流入
し、反応液の浄化が不充分となってしまうことが生じ得
る。また、可溶化槽３が、微生物作用によるものである
場合、微生物は、固形物を分解する酵素を多量に体外に
分泌する。この酵素を可溶化槽３に保持することは、反
応の高速化になるが、可溶化処理水とともに流出してし
まう。この現象は、可溶化槽３が酵素の作用によるもの
である場合も同様である。そこで、可溶化槽３の後段
に、膜分離装置５ａを有する固液分離槽５を設け、未分
解の固形物を回収するとともに、可溶化された反応液中
に含まれる酵素の回収を行ない、可溶化槽３に戻す。こ
れにより、固形物の分解率の向上を行なうことができ
る。Here, the solids are reduced in molecular weight in the solubilization tank 2, but flow into the methane fermentation tank 4 in a partially undecomposed state, resulting in insufficient purification of the reaction solution. Can occur. When the solubilization tank 3 is based on the action of a microorganism, the microorganism secretes a large amount of an enzyme that decomposes a solid substance outside the body. Holding the enzyme in the solubilization tank 3 speeds up the reaction, but flows out together with the solubilized water. This phenomenon is the same when the solubilization tank 3 is caused by the action of an enzyme. Therefore, a solid-liquid separation tank 5 having a membrane separation device 5a is provided at the subsequent stage of the solubilization tank 3 to collect undegraded solids and to collect enzymes contained in the solubilized reaction solution. Return to solubilization tank 3. Thereby, the decomposition rate of the solid can be improved.
【００２１】ここで、この膜分離装置５ａを有する固液
分離槽５は、固形物および酵素の分離回収が行なえれば
良く、膜材料、膜型式は問わない。使用する膜は、分離
回収の対象となる酵素の分子量などにより、予め、実験
により、決定することが望ましい。Here, the solid-liquid separation tank 5 having the membrane separation device 5a only needs to be capable of separating and recovering solids and enzymes, regardless of the membrane material and membrane type. It is desirable that the membrane to be used is determined in advance by an experiment based on the molecular weight of the enzyme to be separated and recovered.
【００２２】なお、図３において、可溶化槽３として、
嫌気性上向流式汚泥床型リアクタを用いてもよい。嫌気
性上向流式汚泥床型リアクタを用いた場合は、オゾン反
応槽２でオゾンの作用で低分子化されやすい状態にされ
た固形物は、嫌気性上向流式汚泥床型リアクタからなる
可溶化槽３に送られ、可溶化、酸発酵を受け、低分子化
される。この嫌気性上向流式汚泥型リアクタは、メタン
菌が粒状に造粒化されたグラニュールを多量に保持して
おり、反応液中の有機性固形物を速やかに可溶化する。
これは、メタン菌が体外に固形物を可溶化する酵素を多
量に分泌するためである。次いで、可溶化された固形物
を含む廃水は、メタン発酵槽４で、処理され、浄化され
る。このとき、嫌気性上向流式汚泥床型リアクタからな
る可溶化槽３から流出する未分解の固形物や固形物を分
解する酵素は、膜分離装置５ａで分離回収され、再び嫌
気性上向流式汚泥床型リアクタに戻され、可溶化され
る。In FIG. 3, as the solubilizing tank 3,
An anaerobic upward flow sludge bed type reactor may be used. When an anaerobic upward-flow sludge-bed reactor is used, the solids that have been made to be easily degraded by the action of ozone in the ozone reaction tank 2 are composed of an anaerobic upward-flow-type sludge-bed reactor. It is sent to the solubilization tank 3 and undergoes solubilization and acid fermentation to reduce the molecular weight. This anaerobic upward sludge reactor has a large amount of granules in which methane bacteria are granulated in granules, and rapidly solubilizes organic solids in the reaction solution.
This is because methane bacteria secrete a large amount of an enzyme that solubilizes solids outside the body. Next, the wastewater containing the solubilized solids is treated and purified in the methane fermenter 4. At this time, undecomposed solids and enzymes that decompose solids flowing out of the solubilization tank 3 composed of the anaerobic upward sludge bed type reactor are separated and collected by the membrane separation device 5a, and are again anaerobic upward. It is returned to the flow-type sludge bed type reactor and solubilized.
【００２３】また、図３において可溶化槽３として、酵
素を有する酵素リアクタを用いてもよい。酵素リアクタ
を用いた場合は、オゾン反応槽２でオゾンの作用により
低分子化されやすくなった固形物は、酵素リアクタ３に
送られ可溶化、酸発酵を受け、低分子化される。この酵
素リアクタ３は、固形物の成分により異なる種類の酵素
が添加されており、セルロースを含む固形物ならば酵素
としてセルラーゼが使用され、タンパク質を含む固形物
ならば酵素としてプロテアーゼが使用される。次いで、
可溶化された固形物を含む反応液は、メタン発酵槽４で
処理され、浄化される。このとき、酵素リアクタ３から
流出する未分解の固形物や酵素は、膜分離装置５で分離
回収され、再び酵素リアクタ３に戻されて可溶化され
る。ここで、酵素リアクタ３に添加される酵素の種類、
濃度などは、処理対象となる固形物の成分、濃度によっ
て決定されるもので、予め実験によって決定されるのが
望ましい。In FIG. 3, an enzyme reactor having an enzyme may be used as the solubilization tank 3. In the case where an enzyme reactor is used, solids that have been easily reduced in molecular weight by the action of ozone in the ozone reaction tank 2 are sent to the enzyme reactor 3 and subjected to solubilization and acid fermentation to reduce the molecular weight. In the enzyme reactor 3, different types of enzymes are added depending on the components of the solid. Cellulase is used as the enzyme in the case of a solid containing cellulose, and protease is used as the enzyme in the case of a solid containing protein. Then
The reaction solution containing the solubilized solid is treated and purified in the methane fermenter 4. At this time, undecomposed solids and enzymes flowing out of the enzyme reactor 3 are separated and recovered by the membrane separation device 5, and returned to the enzyme reactor 3 again to be solubilized. Here, the type of the enzyme added to the enzyme reactor 3,
The concentration and the like are determined by the components and concentrations of the solid to be treated, and are desirably determined in advance by experiments.
【００２４】次に図４により本発明の第４の実施の形態
について説明する。図４に示す第４の実施の形態はオゾ
ン反応槽２と可溶化槽３との間に濃縮槽６を設けたもの
であり、他は図３に示す第３の実施の形態と略同一であ
る。Next, a fourth embodiment of the present invention will be described with reference to FIG. In the fourth embodiment shown in FIG. 4, a concentrating tank 6 is provided between the ozone reaction tank 2 and the solubilizing tank 3, and the other parts are substantially the same as those in the third embodiment shown in FIG. is there.
【００２５】図４に示すように、廃水がオゾン反応槽２
内に流入すると、廃水中の固形物はオゾンの作用を受
け、細胞室など原形質が直接破壊され、低分子化しやす
い状態に処理される。オゾン処理を受けたオゾン反応槽
２からの反応液は、次に濃縮槽６において濃縮される
が、オゾン処理を受けた反応液は濃縮性が改善されるの
で、濃縮槽６において反応液を効率良く濃縮することが
できる。As shown in FIG.
When the solids flow into the wastewater, the solid matter in the wastewater is subjected to the action of ozone, and the protoplasm such as the cell compartment is directly destroyed, and the solid matter is processed into a state where the molecular weight is easily reduced. The reaction liquid from the ozone reaction tank 2 which has been subjected to the ozone treatment is then concentrated in the concentration tank 6, but the reaction liquid which has been subjected to the ozone treatment has an improved concentration property. It can be concentrated well.
【００２６】その後、反応液は可溶化槽３、固液分離槽
５およびメタン発酵槽４を順次続ていくが、濃縮槽６内
において効率良く反応液を濃縮することができるので、
その後可溶化槽３およびメタン発酵槽４における滞留時
間を延ばすことができ、処理効率の向上を図ることがで
きる。Thereafter, the reaction solution is successively passed through the solubilization tank 3, the solid-liquid separation tank 5 and the methane fermentation tank 4, but the reaction solution can be efficiently concentrated in the concentration tank 6.
Thereafter, the residence time in the solubilization tank 3 and the methane fermentation tank 4 can be extended, and the processing efficiency can be improved.
【００２７】次に図５により本発明の第５の実施の形態
について説明する。図５に示す第５の実施の形態はオゾ
ン反応槽２として濃縮機能を有するものを用いるととも
に濃縮槽６を取除いたものであり、他は図４に示す第４
の実施の形態と略同一である。Next, a fifth embodiment of the present invention will be described with reference to FIG. The fifth embodiment shown in FIG. 5 uses an ozone reaction tank 2 having a concentrating function and eliminates the concentrating tank 6, and the other is the fourth embodiment shown in FIG.
This is substantially the same as the embodiment.
【００２８】図５に示すように、オゾン反応槽２は槽本
体１１と、槽本体１１の下部に設けられオゾナイザ１に
連結されたオゾン散気用の散気装置１６とを有してい
る。また槽本体１１の略中央部には、廃水を流入させて
拡散させる流入部１５が配置され、流入部１５と散気装
置１６との間には濃縮汚泥を掻き寄せるレーキ１３が設
けられている。As shown in FIG. 5, the ozone reaction tank 2 has a tank body 11 and an air diffusion device 16 provided at a lower portion of the tank body 11 and connected to the ozonizer 1 for diffusing ozone. In addition, an inflow portion 15 for inflowing and diffusing wastewater is arranged at a substantially central portion of the tank body 11, and a rake 13 for scraping concentrated sludge is provided between the inflow portion 15 and the air diffuser 16. .
【００２９】さらに槽本体１１の底部には、濃縮汚泥を
排出して可溶化槽３へ送る排出部１７が設けられてい
る。また槽本体１１は、排気管１４ａを有する蓋１４に
よって密閉されている。Further, at the bottom of the tank body 11, there is provided a discharge section 17 for discharging the concentrated sludge and sending it to the solubilization tank 3. The tank body 11 is sealed by a lid 14 having an exhaust pipe 14a.
【００３０】図５において、流入部１５に流入する廃水
は流入部１５から槽本体１１内へ入る。この間、散気装
置１６からオゾンが槽本体１１内に流入し、廃水に対し
てオゾン処理を行なう。廃水に対してオゾン処理するこ
とにより反応液が生成され、この反応液はその後スムー
スに槽本体１１内で濃縮される。In FIG. 5, wastewater flowing into the inflow section 15 enters the tank body 11 from the inflow section 15. During this time, ozone flows from the air diffuser 16 into the tank body 11, and performs ozone treatment on the wastewater. A reaction liquid is generated by subjecting the wastewater to ozone treatment, and the reaction liquid is thereafter smoothly concentrated in the tank body 11.
【００３１】なお、図１乃至図５に示す各実施の形態に
おいて、メタン発酵槽４の前段に可溶化槽３を設けた例
を示したが、この可溶化槽３は必ずしも設ける必要はな
い。可溶化槽３を設けない場合は、オゾンの作用をうけ
て低分子化しやすい状態に処理された反応液は、メタン
発酵槽４においてメタン菌の作用により分解される。In each of the embodiments shown in FIGS. 1 to 5, an example is shown in which the solubilization tank 3 is provided before the methane fermentation tank 4, but the solubilization tank 3 is not necessarily provided. When the solubilization tank 3 is not provided, the reaction solution which has been subjected to the action of ozone and has been processed into a state in which it is likely to be reduced in molecular weight is decomposed in the methane fermentation tank 4 by the action of methane bacteria.
【００３２】[0032]
【実施例】次に本発明の具体的実施例について図６によ
り説明する。本実施例は、図１に示す第１の実施の形態
に対応するものである。図６にオゾン反応槽２における
オゾン濃度と、メタン発酵槽４におけるメタン発生効率
を示す。Next, a specific embodiment of the present invention will be described with reference to FIG. The present embodiment corresponds to the first embodiment shown in FIG. FIG. 6 shows the ozone concentration in the ozone reaction tank 2 and the methane generation efficiency in the methane fermentation tank 4.
【００３３】図１において、廃水として、図示しない活
性汚泥処理装置からの余剰汚泥（ＴＳ濃度２．２％）が
オゾン反応槽２内に流入した。この時、オゾン反応槽２
内におけるオゾン濃度（ｇ／Ｎｍ3 ）を種々変化させ
た。この場合におけるメタン発酵槽４内のメタン発生効
率（％）を図６に示す。In FIG. 1, surplus sludge (TS concentration: 2.2%) from an activated sludge treatment device (not shown) flowed into the ozone reaction tank 2 as wastewater. At this time, the ozone reaction tank 2
The ozone concentration (g / Nm 3 ) in the chamber was variously changed. FIG. 6 shows the methane generation efficiency (%) in the methane fermenter 4 in this case.
【００３４】図６に示すように、オゾン濃度７０ｇ／Ｎ
ｍ3 以上のとき、メタン発生効率が最高値１００％をと
ることがわかる。As shown in FIG. 6, the ozone concentration is 70 g / N
It can be seen that the methane generation efficiency takes the maximum value of 100% when m 3 or more.
【００３５】なお、図６においてメタン発生効率は、メ
タン発生効率の最高値を１００％としたものである。In FIG. 6, the methane generation efficiency is obtained by setting the maximum value of the methane generation efficiency to 100%.
【００３６】[0036]
【発明の効果】以上説明したように、本発明によれば、
有機性固形物を含む廃水を容易かつ簡単に浄化処理する
ことができる。そのため、従来、消化期間が長期にわた
るとともに大きな施設が必要であったが、小さな施設で
迅速に処理することができ、施設建設のイニシャルコス
ト、ランニングコストの低減を図ることができる。As described above, according to the present invention,
Wastewater containing organic solids can be easily and easily purified. For this reason, conventionally, the digestion period has been long and a large facility has been required. However, the treatment can be quickly performed in a small facility, and the initial cost and running cost of the facility construction can be reduced.
【図１】発明による水処理装置の第１の実施の形態を示
す構成図。FIG. 1 is a configuration diagram showing a first embodiment of a water treatment apparatus according to the present invention.
【図２】発明による水処理装置の第２の実施の形態を示
す構成図。FIG. 2 is a configuration diagram showing a second embodiment of the water treatment apparatus according to the present invention.
【図３】発明による水処理装置の第３の実施の形態を示
す構成図。FIG. 3 is a configuration diagram showing a third embodiment of the water treatment apparatus according to the present invention.
【図４】発明による水処理装置の第４の実施の形態を示
す構成図。FIG. 4 is a configuration diagram showing a fourth embodiment of the water treatment apparatus according to the present invention.
【図５】発明による水処理装置の第５の実施の形態を示
す構成図。FIG. 5 is a configuration diagram showing a fifth embodiment of the water treatment apparatus according to the present invention.
【図６】オゾン濃度とメタン発生効率との関係を示す
図。FIG. 6 is a graph showing the relationship between ozone concentration and methane generation efficiency.
１ オゾナイザ ２ オゾン反応槽 ３ 可溶化槽 ４ メタン発酵槽 ５ 固液分離槽 ５ａ 膜分離装置 ６ 濃縮槽 １１ 槽本体 １３ レーキ １６ 散気装置 DESCRIPTION OF SYMBOLS 1 Ozonizer 2 Ozone reaction tank 3 Solubilization tank 4 Methane fermentation tank 5 Solid-liquid separation tank 5a Membrane separation device 6 Concentration tank 11 Tank body 13 Rake 16 Aerator
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 ＦＩ Ｃ０２Ｆ 3/28 Ｃ０２Ｆ 3/28 Ｚ (72)発明者 毛 受 卓 神奈川県横浜市鶴見区末広町２丁目４番地 株式会社東芝京浜事業所内──────────────────────────────────────────────────続 き Continued on the front page (51) Int.Cl. 6 Identification symbol FI C02F 3/28 C02F 3/28 Z (72) Inventor Mamoru Taku 2-4 Suehirocho, Tsurumi-ku, Yokohama-shi, Kanagawa Toshiba Keihin Office
Claims (11)
反応させて反応液を生成するオゾン反応槽と、 オゾン反応槽からの反応液をメタン発酵させるメタン発
酵槽とを備えたことを特徴とする水処理装置。1. An ozone reactor for mixing and reacting wastewater containing organic solids and ozone to produce a reaction solution, and a methane fermenter for methane fermenting the reaction solution from the ozone reactor. Characterized water treatment equipment.
応液を濃縮する濃縮槽を設けたことを特徴とする請求項
１記載の水処理装置。2. The water treatment apparatus according to claim 1, wherein a concentration tank for concentrating the reaction solution is provided between the ozone reaction tank and the methane fermentation tank.
させて低分子化する可溶化槽を設けたことを特徴とする
請求項１または２のいずれか記載の水処理装置。3. The water treatment apparatus according to claim 1, wherein a solubilization tank for solubilizing the reaction solution to reduce the molecular weight is provided in a stage preceding the methane fermentation tank.
中の未分解固形分を分離回収して可溶化槽に戻す固液分
離槽を設けたことを特徴とする請求項１記載の水処理装
置。4. A solid-liquid separation tank is provided between the solubilization tank and the methane fermentation tank to separate and recover undecomposed solids in the reaction solution and return the solid to the solubilization tank. A water treatment apparatus as described in the above.
徴とする請求項４記載の水処理装置。5. The water treatment apparatus according to claim 4, wherein the solid-liquid separation tank has a membrane separation device.
を特徴とする請求項３記載の水処理装置。6. The water treatment apparatus according to claim 3, wherein the solubilization tank comprises a sludge bed type reactor.
ことを特徴とする請求項３記載の水処理装置。7. The water treatment apparatus according to claim 3, wherein the solubilization tank comprises a reactor having an enzyme.
を特徴とする請求項３記載の水処理装置。8. The water treatment apparatus according to claim 3, wherein the solubilization tank comprises a fixed bed type reactor.
ｇ／Ｎｍ3 以上としたことを特徴とする請求項１記載の
水処理装置。9. An ozone concentration of 70 in an ozone reaction tank.
The water treatment apparatus according to claim 1, characterized in that a g / Nm 3 or more.
らなることを特徴とする請求項２記載の水処理装置。10. The water treatment apparatus according to claim 2, wherein the concentration tank comprises a gravity concentration tank or a centrifugal concentration tank.
設けられたオゾン散気用の散気装置と、槽本体内に設け
られたレーキとを有し、濃縮機能をもつことを特徴とす
る請求項２記載の水処理装置。11. The ozone treatment tank has a tank main body, an ozone diffusing device provided at a lower portion of the tank main body, and a rake provided in the tank main body, and has an enrichment function. The water treatment apparatus according to claim 2, wherein
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11802497A JPH10230295A (en) | 1996-12-19 | 1997-05-08 | Water treating apparatus |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP33981196 | 1996-12-19 | ||
| JP8-339811 | 1996-12-19 | ||
| JP11802497A JPH10230295A (en) | 1996-12-19 | 1997-05-08 | Water treating apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH10230295A true JPH10230295A (en) | 1998-09-02 |
Family
ID=26456037
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP11802497A Pending JPH10230295A (en) | 1996-12-19 | 1997-05-08 | Water treating apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH10230295A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001000985A (en) * | 1999-06-22 | 2001-01-09 | Toshiba Corp | Method and apparatus for treating organic solid- containing wastewater |
| JP2009022955A (en) * | 2008-11-04 | 2009-02-05 | Toshiba Corp | Method for treating organic solid-containing waste water, and treatment method therefor |
| US20120080374A1 (en) * | 2010-10-04 | 2012-04-05 | Pacific Advanced Civil Engineering, Inc. | Ozone and anaerobic biological pretreatment for a desalination process |
| JP2013184107A (en) * | 2012-03-07 | 2013-09-19 | Osaka Gas Co Ltd | Method for solubilizing wastewater containing used tea leaf |
-
1997
- 1997-05-08 JP JP11802497A patent/JPH10230295A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001000985A (en) * | 1999-06-22 | 2001-01-09 | Toshiba Corp | Method and apparatus for treating organic solid- containing wastewater |
| JP2009022955A (en) * | 2008-11-04 | 2009-02-05 | Toshiba Corp | Method for treating organic solid-containing waste water, and treatment method therefor |
| US20120080374A1 (en) * | 2010-10-04 | 2012-04-05 | Pacific Advanced Civil Engineering, Inc. | Ozone and anaerobic biological pretreatment for a desalination process |
| JP2013184107A (en) * | 2012-03-07 | 2013-09-19 | Osaka Gas Co Ltd | Method for solubilizing wastewater containing used tea leaf |
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