JP2003164856A - Method for separating and decomposing volatile organic compound in waste water and device therefor - Google Patents
Method for separating and decomposing volatile organic compound in waste water and device thereforInfo
- Publication number
- JP2003164856A JP2003164856A JP2001364994A JP2001364994A JP2003164856A JP 2003164856 A JP2003164856 A JP 2003164856A JP 2001364994 A JP2001364994 A JP 2001364994A JP 2001364994 A JP2001364994 A JP 2001364994A JP 2003164856 A JP2003164856 A JP 2003164856A
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- Japan
- Prior art keywords
- volatile organic
- waste water
- gas
- exhaust gas
- organic compound
- 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.)
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Classifications
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- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Treating Waste Gases (AREA)
- Degasification And Air Bubble Elimination (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Physical Water Treatments (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、地下水又は産業廃
水等の廃水にトリクロロエチレン又はテトラクロロエチ
レン等のような揮発性有機化合物を含んでいる場合に、
この揮発性有機化合物を、廃水から分離したのち無害な
状態に分解処理するための方法とその装置とに関するも
のである。TECHNICAL FIELD The present invention relates to a case where wastewater such as groundwater or industrial wastewater contains a volatile organic compound such as trichlorethylene or tetrachloroethylene,
The present invention relates to a method and an apparatus for decomposing this volatile organic compound into a harmless state after separating it from wastewater.
【０００２】[0002]
【従来の技術】従来、地下水又は産業廃水等の廃水の処
理に際して、これに含まれているトリクロロエチレン又
はテトラクロロエチレン等のような揮発性有機化合物
を、前記廃水から分離したのち分解処理するには、この
廃水に対して空気等の気体を多量に吹き込むというバブ
リング（曝気）を行い、廃水中における揮発性有機化合
物を、この廃水に吹き込んだ気体中に揮発させることに
より、廃水から分離し、次いで、この揮発性有機化合物
を含む排出ガスをガス浄化装置に導くことにより、有害
な揮発性有機化合物を活性炭に吸着させるか、揮発性有
機化合物を紫外線の照射にて酸化分解するとか、或い
は、高温加熱にて揮発性有機化合物を分解するという方
法が採用されている。2. Description of the Related Art Conventionally, when treating wastewater such as groundwater or industrial wastewater, volatile organic compounds such as trichlorethylene or tetrachlorethylene contained therein are separated from the wastewater and then decomposed. Bubbling (aeration) is performed by blowing a large amount of gas such as air into the wastewater, and volatile organic compounds in the wastewater are volatilized into the gas blown into the wastewater to separate it from the wastewater. By introducing the exhaust gas containing volatile organic compounds to the gas purifier, the harmful volatile organic compounds are adsorbed on the activated carbon, or the volatile organic compounds are oxidatively decomposed by irradiation of ultraviolet rays, or they are heated at high temperature. The method of decomposing volatile organic compounds is adopted.
【０００３】[0003]
【発明が解決しようとする課題】しかし、このバブリン
グ方法においては、廃水に対して揮発性有機化合物を分
離することのために吹き込んだ多量の空気が、揮発性有
機化合物を含む排出ガスとして多量に排出されることに
加えて、この排気ガスにおける揮発性有機化合物の濃度
が極めて低いから、この排出ガスの浄化処理に際して
は、多量の排出ガスを取り扱うことのために、その浄化
装置が著しく大型化になるという問題がある。However, in this bubbling method, a large amount of air blown for separating the volatile organic compounds from the wastewater becomes a large amount of exhaust gas containing the volatile organic compounds. In addition to being discharged, the concentration of volatile organic compounds in this exhaust gas is extremely low, so during the purification process of this exhaust gas, the purification device has to be remarkably large in size because a large amount of exhaust gas is handled. There is a problem that becomes.
【０００４】これに加えて、前記した各浄化方法のうち
活性炭に吸着させる方法は、吸着した後の活性炭の廃棄
処分が厄介であるという問題があり、また、紫外線の照
射にて酸化分解する方法は、ハロゲン化酢酸等が生成
し、これを処理するための、エアーレーションタンクを
含んだ生物処理装置等の新たな処理装置が必要となり、
装置が複雑・高価になるという問題があり、更にまた、
高温加熱する方法は、多量の排出ガスを均一に加熱する
ことができず、加熱温度むらができるから、有害な二次
生成物が発生するばかりか、安定して分解処理できず、
しかも、排出ガスの加熱に多量の熱源を必要とし、ラン
ニングコストが大幅に嵩むという問題がある。In addition to the above, among the above-mentioned purification methods, the method of adsorbing on activated carbon has a problem that disposal of activated carbon after adsorption is troublesome, and the method of oxidative decomposition by irradiation of ultraviolet rays. Produces halogenated acetic acid, etc., and requires a new treatment device such as a biological treatment device including an aeration tank for treating this.
There is a problem that the device becomes complicated and expensive, and furthermore,
The method of heating at a high temperature cannot uniformly heat a large amount of exhaust gas, and since the heating temperature can be uneven, not only harmful secondary products are generated, but also stable decomposition cannot be performed,
In addition, there is a problem that a large amount of heat source is required to heat the exhaust gas, which significantly increases running cost.
【０００５】本発明は、廃水に含まれている揮発性有機
化合物を廃水から分離したのち分解処理することを、ラ
ンニングコストのアップ及び装置の大型化等を招来する
ことなく、安定して確実にできるようにした方法と、そ
の装置とを提供することを技術的課題とするものであ
る。The present invention stably and reliably separates volatile organic compounds contained in wastewater from the wastewater and then decomposes the wastewater without increasing running costs and increasing the size of the apparatus. It is a technical object to provide a method and an apparatus therefor.
【０００６】[0006]
【課題を解決するための手段】この技術的課題を達成す
るため本発明の方法は、第１に、「揮発性有機化合物を
含む廃水を、大気圧以下の減圧に保持した蒸発缶内に導
いて沸騰・蒸発し、その水蒸気を凝縮し、凝縮水を除い
た排出ガスを、９００℃以上の温度に加熱し、この加熱
した排出ガスを、アルカリ水溶液と直接的に接触す
る。」することを特徴としている。In order to achieve this technical object, the method of the present invention is as follows. First, "Waste water containing a volatile organic compound is introduced into an evaporator which is kept at a reduced pressure below atmospheric pressure. It is boiled and evaporated to condense the water vapor, and the exhaust gas from which condensed water has been removed is heated to a temperature of 900 ° C. or higher, and the heated exhaust gas is brought into direct contact with the alkaline aqueous solution. ” It has a feature.
【０００７】また、本発明の方法は、第２に、「揮発性
有機化合物を含む廃水に空気等のガスを吸収させ、この
廃水を、大気圧以下の減圧に保持した脱気容器内に導い
て脱気し、脱気した排出ガスを、９００℃以上の温度に
加熱し、この加熱した排出ガスを、アルカリ水溶液と直
接的に接触する。」することを特徴としている。Secondly, in the method of the present invention, "a waste water containing a volatile organic compound is allowed to absorb a gas such as air, and the waste water is introduced into a deaeration container maintained at a reduced pressure below atmospheric pressure. Degassing is performed, the degassed exhaust gas is heated to a temperature of 900 ° C. or higher, and the heated exhaust gas is brought into direct contact with the alkaline aqueous solution. ”
【０００８】次に、本発明の装置は、第１に、「揮発性
有機化合物を含む廃水を大気圧以下の減圧状態で沸騰・
蒸発する蒸発缶と、この蒸発缶で発生した水蒸気に対す
る凝縮器とからなり、更に、前記凝縮器からの排出ガス
に対する加熱手段と、この加熱した排出ガスをアルカリ
水溶液に直接的に接触する手段とを備えている。」こと
を特徴としている。Next, in the apparatus of the present invention, firstly, "the waste water containing a volatile organic compound is boiled under reduced pressure below atmospheric pressure.
It comprises an evaporator that evaporates and a condenser for water vapor generated in the evaporator, and a heating means for the exhaust gas from the condenser, and a means for directly contacting the heated exhaust gas with an alkaline aqueous solution. Is equipped with. It is characterized by
【０００９】また、本発明の装置は、第２に、「揮発性
有機化合物を含む廃水に対するガス吸収容器と、このガ
ス吸収容器からの廃水を大気圧以下の減圧状態で脱気す
る脱気容器とからなり、更に、前記脱気容器からの排出
ガスに対する加熱手段と、この加熱した排出ガスをアル
カリ水溶液に直接的に接触する手段とを備えている。」
ことを特徴としている。Secondly, the apparatus of the present invention includes: "a gas absorption container for waste water containing a volatile organic compound, and a degassing container for degassing the waste water from this gas absorption container under a reduced pressure below atmospheric pressure. And a means for heating the exhaust gas from the degassing container and a means for directly contacting the heated exhaust gas with the alkaline aqueous solution. "
It is characterized by that.
【００１０】[0010]
【発明の実施の形態】以下、本発明の実施の形態を図面
について説明する。BEST MODE FOR CARRYING OUT THE INVENTION Embodiments of the present invention will be described below with reference to the drawings.
【００１１】図１は、第１の実施の形態を示す。FIG. 1 shows a first embodiment.
【００１２】この図において、符号１は、廃水に含まれ
ている揮発性有機化合物を廃水から分離するための蒸発
式の分離装置を示し、この分離装置１は、減圧式の蒸発
缶２を備え、廃水供給管路３より送られて来るトリクロ
ロエチレン又はテトラクロロエチレン等のような揮発性
有機化合物を含む廃水を、前記蒸発缶２内の底部に流入
し、この蒸発缶２内の適宜液深さＨ１に溜めたのち、排
出口４から流出するように構成する。In the figure, reference numeral 1 indicates an evaporative separator for separating volatile organic compounds contained in wastewater from the wastewater, and the separator 1 comprises a depressurizing evaporator 2 Waste water containing a volatile organic compound such as trichloroethylene or tetrachloroethylene sent from the wastewater supply pipe 3 flows into the bottom of the evaporator 2 to a suitable liquid depth H1 in the evaporator 2. After being stored, it is configured to flow out from the discharge port 4.
【００１３】前記廃水供給管路３の途中には、凝縮器を
兼ねた間接熱交換式の給水加熱器５が設けられ、この給
水加熱器５に、前記蒸発缶２内での沸騰・蒸発で発生し
た水蒸気及び不凝縮性のガスを、電動モータにて回転駆
動されるブロワー等の圧縮機６に吸引して圧縮したのち
導入することにより、前記廃水供給管路３を通って蒸発
缶２に送られる廃水を加熱（給水加熱）する一方、この
給水加熱器５における凝縮水及び不凝縮性のガスを、気
液分離容器７に導いて、凝縮水と、不凝縮性のガスとに
分離し、凝縮水を気液分離容器７の外に取り出す一方、
不凝縮性のガスを、真空ポンプ８等の真空発生源にて吸
引して、前記蒸発缶２内を大気圧以下の減圧に保持する
ことにより、前記蒸発缶２内で廃水を沸騰・蒸発する。An indirect heat exchange type feed water heater 5 also serving as a condenser is provided in the middle of the waste water supply pipe 3, and the feed water heater 5 is used for boiling / evaporating in the evaporation can 2. The generated water vapor and non-condensable gas are sucked into a compressor 6 such as a blower that is driven to rotate by an electric motor, compressed, and then introduced to the evaporator 2 through the waste water supply pipe 3. While the waste water sent is heated (feed water heating), the condensed water and the non-condensable gas in the feed water heater 5 are introduced into the gas-liquid separation container 7 and separated into condensed water and non-condensable gas. , While the condensed water is taken out of the gas-liquid separation container 7,
The non-condensable gas is sucked by a vacuum generation source such as a vacuum pump 8 and the inside of the evaporator 2 is kept at a reduced pressure below atmospheric pressure to boil and evaporate waste water in the evaporator 2. .
【００１４】この蒸発缶２内での廃水の沸騰・蒸発によ
り、この廃水の一部が水蒸気になると同時に、この廃水
中に含まれている揮発性有機化合物は、廃水の沸騰・蒸
発と同時に揮発し気体になって廃水から分離するから、
前記蒸発缶２内には、水蒸気、及び前記揮発性有機化合
物の気体と空気等とを含む不凝縮性のガスが発生する一
方、この蒸発缶１内で揮発性有機化合物を分離したあと
における処理済の廃水は、排出口４から排出される。By boiling and evaporating the waste water in the evaporator 2, a part of the waste water becomes steam, and at the same time, the volatile organic compounds contained in the waste water volatilize simultaneously with the boiling and evaporation of the waste water. It becomes a gas and separates from the wastewater,
Water vapor and a non-condensable gas containing the gas of the volatile organic compound and air are generated in the evaporator 2 while the treatment after the volatile organic compound is separated in the evaporator 1 The used waste water is discharged from the discharge port 4.
【００１５】この場合、蒸発缶２内での廃水の沸騰・蒸
発を、当該廃水の水面からの液深さが深い部分において
行うようにすることにより、廃水中から揮発性有機化合
物を蒸発にて分離するときにおける分離率を、廃水の沸
騰・蒸発を廃水の水面のみにおいて行うように構成した
場合に比べて、大幅に向上できる。これに加えて、蒸発
缶２の内部に、ラシヒリング等による充填層２ａを設け
ることで、更なる分離率のアップを図ることができる。In this case, by boiling and evaporating the waste water in the evaporator 2 at a portion where the liquid depth of the waste water is deep, the volatile organic compounds can be evaporated from the waste water. The separation rate at the time of separation can be significantly improved as compared with the case where the waste water is boiled and evaporated only on the surface of the waste water. In addition to this, by providing the filling layer 2a by Raschig ring or the like inside the evaporator 2, the separation rate can be further increased.
【００１６】そして、前記蒸発缶２内における水蒸気及
び不凝縮性のガスは、給水加熱器６において凝縮され、
水蒸気は凝縮水として取り出される一方、不凝縮性のガ
スは真空ポンプ８にて吸引され、排出ガスとして排出さ
れる。The water vapor and the non-condensable gas in the evaporator 2 are condensed in the feed water heater 6,
The water vapor is taken out as condensed water, while the non-condensable gas is sucked by the vacuum pump 8 and discharged as exhaust gas.
【００１７】この真空ポンプ８からの排出ガスは、減圧
状態の蒸発缶２内等の漏れて流入した空気と、廃水から
分離した揮発性有機化合物の気化物の略合計であり、そ
の量は、従来のバブリングによる分離方法よりも遥かに
少ないとともに、当該排出ガスにおける揮発性有機化合
物の濃度も遥かに高いから、この排出ガスを、後述する
ガス分解装置１０に導いて分解処理する。The exhaust gas from the vacuum pump 8 is substantially the sum of the leaked air such as in the evaporator 2 in a depressurized state and the vaporized volatile organic compounds separated from the waste water. Since the amount of volatile organic compounds in the exhaust gas is much higher than that of the conventional separation method by bubbling, the exhaust gas is guided to the gas decomposition apparatus 10 described later to be decomposed.
【００１８】このガス分解装置１０は、前記分離装置１
からの排出ガスを、電熱ヒータ又は赤外線ランプ等にて
９００℃以上の温度、好ましくは１１００℃以上の温度
に加熱するための加熱手段１１と、この加熱手段１１に
て加熱した排出ガスを、アルカリ水溶液と直接的に接触
する気液接触手段１２とで構成されている。This gas decomposition apparatus 10 is the same as the separation apparatus 1 described above.
Heating means 11 for heating the exhaust gas from the heater to a temperature of 900 ° C. or higher, preferably 1100 ° C. or higher with an electric heater or an infrared lamp, and the exhaust gas heated by the heating means 11 It is composed of a gas-liquid contact means 12 that comes into direct contact with the aqueous solution.
【００１９】前記気液接触手段１２は、本実施の形態の
場合、ＰＨを約１１に調整したアルカリ水溶液を入れた
タンク１２ａと、このタンク１２ａ内から循環ポンプ１
２ｂにて汲み出したアルカリ水溶液で、前記加熱手段１
１からの排出ガスを吸引・混合するエゼクター１２ｃ
と、ラシヒリング等の充填層１２ｅを内蔵し、且つ、大
気へのガス排出口１２ｆを備えた気液接触塔１２ｄとに
よって構成されている。In the case of the present embodiment, the gas-liquid contacting means 12 is a tank 12a containing an alkaline aqueous solution whose pH is adjusted to about 11, and a circulation pump 1 from this tank 12a.
With the alkaline aqueous solution pumped out in 2b, the heating means 1
Ejector 12c for sucking and mixing exhaust gas from 1
And a gas-liquid contact tower 12d having a packed bed 12e such as Raschig rings built therein and having a gas outlet 12f to the atmosphere.
【００２０】前記分離装置１からの排出ガスを、加熱手
段１１にて９００℃以上の温度、好ましくは１１００℃
以上の温度に加熱することにより、この排出ガス中にお
けるトリクロロエチレン（Ｃｌ2 Ｃ＝ＣＨＣｌ）は、酸
素の存在のともに、有害なホスゲン（ＣＯＣｌ2 ）、塩
化水素ガス（ＨＣｌ）、塩素ガス（Ｃｌ2 ）及び炭酸ガ
ス（ＣＯ2 、ＣＯ）に熱分解する。The exhaust gas from the separation device 1 is heated by the heating means 11 to a temperature of 900 ° C. or higher, preferably 1100 ° C.
By heating to the above temperature, trichlorethylene (Cl 2 C = CHCl) in this exhaust gas is toxic to phosgene (COCl 2 ), hydrogen chloride gas (HCl), chlorine gas (Cl 2 ) in the presence of oxygen. ) And carbon dioxide (CO 2 , CO).
【００２１】この場合において、前記分離装置１からの
排出ガスの量は、従来のバブリングによる分離方法より
も遥かに少ないことにより、比較的簡単な加熱手段にて
温度むらを少なくするように加熱できるから、この排出
ガス中におけるトリクロロエチレンの殆ど総てを安定し
て熱分解できる。In this case, since the amount of the exhaust gas from the separating device 1 is much smaller than that in the conventional separating method by bubbling, it can be heated by a relatively simple heating means so as to reduce the temperature unevenness. Therefore, almost all of the trichlorethylene in this exhaust gas can be thermally decomposed stably.
【００２２】このように加熱手段１１にて熱分解した排
出ガスは、この後におけるエゼクター１２ｃにおけるア
ルカリ水溶液との直接的な接触により急冷されるととも
に、前記熱分解した成分のうち塩化水素ガス（ＨＣ
ｌ）、塩素ガス（Ｃｌ2 ）は、アルカリ水溶液にて中和
されることにより、この塩化水素ガス（ＨＣｌ）、塩素
ガス（Ｃｌ2 ）が有害なホスゲン（ＣＯＣｌ2 ）に化合
することを防止できる。The exhaust gas thus thermally decomposed by the heating means 11 is rapidly cooled by direct contact with the alkaline aqueous solution in the ejector 12c after that, and hydrogen chloride gas (HC
l) and chlorine gas (Cl 2 ) are neutralized with an alkaline aqueous solution to prevent the hydrogen chloride gas (HCl) and chlorine gas (Cl 2 ) from combining with harmful phosgene (COCl 2 ). it can.
【００２３】一方、有害なホスゲン（ＣＯＣｌ2 ）は、
エゼクター１２ｃにおけるアルカリ水溶液との直接的な
接触及びその後における気液接触塔１２ｄでのアルカリ
水溶液との直接的な接触により、アルカリ水溶液にて、
ＣＯＣｌ2 ＋Ｈ2 ０→ＣＯ2 ＋２ＨＣｌ
の反応により加水分解し、この加水分解にて発生する塩
化水素ガス（ＨＣｌ）は、アルカリ水溶液にて中和され
るというように分解されるから、ガス排出口１２ｆから
大気中に放出される有害成分を大幅に低減することがで
きる。On the other hand, harmful phosgene (COCl 2 ) is
The direct contact with the alkaline aqueous solution in the ejector 12c and the subsequent direct contact with the alkaline aqueous solution in the gas-liquid contact tower 12d causes hydrolysis in the alkaline aqueous solution by the reaction of COCl 2 + H 2 0 → CO 2 + 2HCl. However, the hydrogen chloride gas (HCl) generated by this hydrolysis is decomposed by being neutralized with an alkaline aqueous solution, so that the harmful components released from the gas outlet 12f into the atmosphere are greatly reduced. can do.
【００２４】本発明者達の実験によると、加熱手段１１
を通過した後においてエゼクター１２ｃでのＰＨ１１の
アルカリ水溶液との直接的な接触により、ホスゲンの濃
度を２０ｐｐｍから０．１ｐｐｍに、塩化水素の濃度を
１０００ｐｐｍから２０〜３０ｐｐｍにまで下げること
ができるのであった。According to the experiments conducted by the present inventors, the heating means 11
It is possible to reduce the concentration of phosgene from 20 ppm to 0.1 ppm and the concentration of hydrogen chloride from 1000 ppm to 20 to 30 ppm by direct contact with the alkaline aqueous solution of PH11 at the ejector 12c after passing through It was
【００２５】なお、前記気液接触手段１２におけるエゼ
クター１２ｃの下流側には、気液接触塔１２ｄを設ける
ことにより、前記した加水分解及び中和を更に促進する
ように構成されており、この気液接触塔１２ｄの内部に
は、水滴を捕捉しその大気中に飛散を防止するためのデ
ミスター１２ｇが設けられている。A gas-liquid contact tower 12d is provided downstream of the ejector 12c in the gas-liquid contact means 12 so as to further promote the above-mentioned hydrolysis and neutralization. Inside the liquid contact tower 12d, a demister 12g for catching water droplets and preventing them from scattering in the atmosphere is provided.
【００２６】また、前記気液接触塔１２ｄにおける充填
層１２ｅ，１２ｇを、活性炭による充填層１２ｅ，１２
ｇにして、ホスゲンを活性炭に吸着しておいて、アルカ
リ水溶液にて加水分解するようにしても良い。The packed beds 12e and 12g in the gas-liquid contact tower 12d are replaced with packed beds 12e and 12 made of activated carbon.
Alternatively, phosgene may be adsorbed on activated carbon and then hydrolyzed with an alkaline aqueous solution.
【００２７】更にまた、前記気液接触手段１２における
タンク１２ａのアルカリ水溶液は、常時、ＰＨが１１に
なるように調整されるとともに、前記蒸発缶２から排出
される処理済廃水の一部を管路１２ｈにて導入し、余剰
のアルカリ水溶液を管路１２ｉを介して前記蒸発缶２へ
の廃水供給管路３に戻すことにより、アルカリ水溶液を
更新することと、前記加熱手段１１において加えた熱を
蒸発缶２での蒸発促進に回収することとを図るように構
成されている。Furthermore, the alkaline aqueous solution in the tank 12a in the gas-liquid contact means 12 is constantly adjusted to have a pH of 11, and a part of the treated waste water discharged from the evaporator 2 is piped. The excess alkaline aqueous solution introduced through the line 12h is returned to the wastewater supply pipeline 3 to the evaporator 2 via the pipeline 12i to renew the alkaline aqueous solution and the heat added in the heating means 11. Are collected to accelerate evaporation in the evaporator 2.
【００２８】次に、図２は、第２の実施の形態を示す。Next, FIG. 2 shows a second embodiment.
【００２９】この第２の実施の形態は、ガス吸収・脱気
式の分離装置２０に適用した場合である。The second embodiment is applied to a gas absorption / deaeration type separation device 20.
【００３０】すなわち、この分離装置２０は、ラシヒリ
ング等の充填層２２を内蔵したガス吸収容器２１と、密
閉型の脱気容器２３とを備え、前記ガス吸収容器２１内
のうち前記充電層２２の上方に、廃水供給管路２４にて
送られて来るトリクロロエチレン又はテトラクロロエチ
レン等のような揮発性有機化合物を含む廃水を散布する
一方、前記ガス吸収容器２１内のうち前記充填層２２の
下方に、コンプレッサー２５にて圧縮された空気をガス
供給管路２６を介して吹き込むことにより、前記廃水に
空気を吸収させる。That is, this separating device 20 is provided with a gas absorption container 21 having a filling layer 22 such as Raschig rings and a closed type degassing container 23, and the charging layer 22 of the gas absorption container 21 is filled with the charging layer 22. Waste water containing a volatile organic compound such as trichlorethylene or tetrachloroethylene sent through a waste water supply pipe 24 is sprayed upward, while a compressor is provided below the packed bed 22 in the gas absorption container 21. The waste water absorbs air by blowing the air compressed in 25 through the gas supply line 26.
【００３１】なお、この廃水に対する空気の吸収率は、
圧力に比例するから、大気圧より高い圧力の状態で行う
ことが好ましい。The air absorption rate for this wastewater is
Since the pressure is proportional to the pressure, it is preferable that the pressure is higher than the atmospheric pressure.
【００３２】また、廃水に吸収するガスとしては、前記
空気に限らず、有害性のない炭酸ガス、窒素ガス及び酸
素ガス等の他のガスを使用しても良い。Further, the gas absorbed in the waste water is not limited to the above air, and other gases such as carbon dioxide gas, nitrogen gas and oxygen gas, which are not harmful, may be used.
【００３３】このように、ガス吸収容器２１において空
気等のガスを吸収した廃水は、管路２７を介して前記脱
気容器２３内に底部に送られ、この脱気容器２３内に適
宜深さＨ２に溜められたのち、排水管路２８から排出さ
れる。The waste water which has absorbed gas such as air in the gas absorption container 21 is sent to the bottom of the degassing container 23 through the pipe 27, and the depth of the degassing container 23 is appropriately adjusted. After being stored in H2, it is discharged from the drainage pipe 28.
【００３４】このとき、前記脱気容器２３内を、真空ポ
ンプ２９等の真空発生源による吸引にて大気圧以下の減
圧状態にすることにより、この脱気容器２３内で廃水の
脱気を行う。At this time, the deaeration container 23 is degassed under atmospheric pressure by suction from a vacuum generating source such as a vacuum pump 29, so that waste water is deaerated in the deaeration container 23. .
【００３５】この脱気容器２３内での廃水の脱気によ
り、この廃水中に含まれている揮発性有機化合物は、廃
水の脱気と同時に揮発し気体になって廃水から分離する
から、この脱気容器２３における排水管路２８からは、
揮発性有機化合物を分離したあとにおける処理済の廃水
が排出される。By degassing the waste water in the degassing container 23, the volatile organic compounds contained in the waste water are volatilized at the same time as the degassing of the waste water to become a gas, which is separated from the waste water. From the drain line 28 in the degassing container 23,
The treated wastewater after separating the volatile organic compounds is discharged.
【００３６】この場合、脱気容器２３内での廃水の脱気
及び発泡を、当該廃水の水面からの液深さが深い部分に
おいて行うようにすることにより、廃水中から揮発性有
機化合物を脱気によって分離するときにおける分離率
を、廃水の脱気及び発泡を廃水の水面のみにおいて行う
ように構成した場合に比べて、大幅に向上できる。これ
に加えて、脱気容器２３の内部に、ラシヒリング等によ
る充填層２３ａを設けることで、更なる分離率のアップ
を図ることができる。In this case, by degassing and foaming the waste water in the degassing container 23 at a portion where the liquid depth of the waste water is deep, the volatile organic compounds are removed from the waste water. The separation rate at the time of separating by air can be significantly improved compared to the case where the waste water is degassed and foamed only on the surface of the waste water. In addition to this, by providing the filling layer 23a by Raschig ring or the like inside the degassing container 23, the separation rate can be further increased.
【００３７】そして、前記脱気容器２３内において廃水
から脱気され、揮発性有機化合物をを含むガスは、真空
ポンプ２９にて吸引され、排出ガスとして排出される。The gas deaerated from the waste water in the deaeration container 23 and containing the volatile organic compound is sucked by the vacuum pump 29 and discharged as an exhaust gas.
【００３８】この真空ポンプ２９からの排出ガスは、そ
の量が廃水に対して最初に吸収するガス量と略等しく
て、従来のバブリングよりも遥かに少ないことに加え
て、揮発性有機化合物の濃度も高いから、前記した第１
の実施の形態の場合と同様に構成したガス分解装置１０
に供給することにより、ガス排出口１２ｆから大気中に
放出される有害成分を大幅に低減することができる。The exhaust gas from the vacuum pump 29 is substantially equal to the amount of gas initially absorbed in the wastewater, which is far smaller than that of conventional bubbling, and the concentration of volatile organic compounds is also small. Because it is also high, the first mentioned above
Gas decomposition apparatus 10 configured in the same manner as in the embodiment
By supplying the gas into the atmosphere, harmful components released from the gas outlet 12f into the atmosphere can be significantly reduced.
【００３９】この場合においても、前記脱気容器２３か
ら排出される処理済廃水の一部を管路１２ｈ′にて導入
し、余剰のアルカリ水溶液を管路１２ｉ′を介して前記
脱気容器２３への廃水管路２７に戻すことにより、アル
カリ水溶液を更新することと、前記加熱手段１１におい
て加えた熱を脱気容器２３での脱気・発泡の促進に回収
することとを図るように構成されている。Also in this case, a part of the treated wastewater discharged from the degassing container 23 is introduced through the conduit 12h ', and the excess alkaline aqueous solution is introduced through the conduit 12i'. By returning to the waste water pipe 27 to the above, the alkaline aqueous solution is renewed and the heat applied in the heating means 11 is recovered to promote deaeration and foaming in the deaeration container 23. Has been done.
【００４０】また、本発明は、廃水からの揮発性有機化
合物の分離を、前段階として図２に示すガス吸収・脱気
による分離を行い、次いで、前記図１に示す蒸発による
分離を行う場合にも同様に適用できることはいうまでも
ない。In the present invention, the separation of the volatile organic compounds from the wastewater is performed by the gas absorption / deaeration shown in FIG. 2 as a preceding step, and then the separation by evaporation shown in FIG. 1 is performed. It goes without saying that the same can be applied to.
【００４１】[0041]
【発明の作用・効果】このように、本発明は、廃水に含
まれている揮発性有機化合物を、廃水の減圧状態での沸
騰・蒸発、又は、廃水へのガス吸収及び脱気にて、少な
い排出ガスで、且つ、揮発性有機化合物の濃度が高い状
態で廃水から分離し、次いで、これを加熱したのちアル
カリ水溶液と直接的な接触して分解処理するものである
ことにより、廃水からの分離及び分解処理を、従来のバ
ブリングによる分離、及び多量の排出ガスに対する分解
処理に比べて、低いランニングコストで、且つ、使用済
み活性炭の廃棄処分の問題を招来することなく、安定し
て達成でき、しかも、装置を大幅に小型化できる効果を
有する。As described above, according to the present invention, the volatile organic compound contained in the wastewater is boiled / vaporized in a reduced pressure state of the wastewater, or gas is absorbed and deaerated in the wastewater. The waste gas is separated from the waste water with a small amount of exhaust gas and in a state where the concentration of volatile organic compounds is high, and then heated and then directly contacted with an alkaline aqueous solution to be decomposed. Separation and decomposition treatment can be achieved stably at a lower running cost than the conventional bubbling separation and decomposition treatment for large amounts of exhaust gas and without causing the problem of disposal of used activated carbon. Moreover, there is an effect that the device can be significantly downsized.
【図１】本発明における第１の実施の形態を示すフロー
シートである。FIG. 1 is a flow sheet showing a first embodiment of the present invention.
【図２】本発明における第２の実施の形態を示すフロー
シートである。FIG. 2 is a flow sheet showing a second embodiment of the present invention.
１ 蒸発式分離装置 ２ 蒸発缶 ３ 廃水供給管路 ４ 排出口 ５ 凝縮器 ６ 圧縮機 ８ 真空ポンプ １０ ガス分解装置 １１ 加熱手段 １２ 気液接触手段 １２ａ アルカリ水溶液タンク １２ｃ エゼクター １２ｄ 気液接触塔 ２０ ガス吸収・脱気式分離装置 ２１ ガス吸収容器 ２３ 脱気容器 ２４ 廃水供給管路 ２６ ガス供給管路 ２９ 真空ポンプ 1 Evaporative separator 2 evaporation cans 3 wastewater supply pipeline 4 outlets 5 condenser 6 compressor 8 vacuum pump 10 Gas decomposition equipment 11 Heating means 12 Gas-liquid contact means 12a Alkaline solution tank 12c ejector 12d gas-liquid contact tower 20 Gas absorption / degassing separator 21 gas absorption container 23 Degassing container 24 Wastewater supply pipeline 26 gas supply line 29 Vacuum pump
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ テーマコート゛(参考） Ｂ０１Ｄ 53/77 Ｂ０１Ｄ 53/34 １３４Ｂ Ｃ０２Ｆ 1/20 (72)発明者 三保 慶明 大阪市西淀川区御幣島６丁目７番５号 株 式会社ササクラ内 Ｆターム(参考） 4D002 AA21 AC10 BA02 BA12 BA16 CA07 CA13 DA01 DA41 EA02 GA01 GB03 4D011 AA16 AB03 AD03 4D034 AA26 CA12 4D037 AA01 AA11 AB14 BA23 BB07─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 7 Identification symbol FI theme code (reference) B01D 53/77 B01D 53/34 134B C02F 1/20 (72) Inventor Keimei Miho 6-chome, Minamijima, Nishiyodogawa-ku, Osaka-shi No. 7 No. 5 F-Term in Sakura Company (Reference) 4D002 AA21 AC10 BA02 BA12 BA16 CA07 CA13 DA01 DA41 EA02 GA01 GB03 4D011 AA16 AB03 AD03 4D034 AA26 CA12 4D037 AA01 AA11 AB14 BA23 BB07
Claims (4)
下の減圧に保持した蒸発缶内に導いて沸騰・蒸発し、そ
の水蒸気を凝縮し、凝縮水を除いた排出ガスを、９００
℃以上の温度に加熱し、この加熱した排出ガスを、アル
カリ水溶液と直接的に接触することを特徴とする廃水中
の揮発性有機化合物を分離・分解処理する方法。1. A waste water containing a volatile organic compound is introduced into an evaporator which is kept at a reduced pressure below atmospheric pressure to boil and evaporate, the water vapor is condensed, and the exhaust gas excluding condensed water is converted into 900
A method for separating and decomposing a volatile organic compound in wastewater, which comprises heating the exhaust gas at a temperature of ℃ or more and directly contacting the heated exhaust gas with an alkaline aqueous solution.
スを吸収させ、この廃水を、大気圧以下の減圧に保持し
た脱気容器内に導いて脱気し、脱気した排出ガスを、９
００℃以上の温度に加熱し、この加熱した排出ガスを、
アルカリ水溶液と直接的に接触するすることを特徴とす
る廃水中の揮発性有機化合物を分離・分解処理する方
法。2. A waste water containing a volatile organic compound is allowed to absorb a gas such as air, and the waste water is introduced into a deaeration container maintained at a reduced pressure below atmospheric pressure to be deaerated, and the deaerated exhaust gas is discharged. , 9
It is heated to a temperature of 00 ° C or higher, and the heated exhaust gas is
A method for separating and decomposing volatile organic compounds in wastewater, which comprises direct contact with an alkaline aqueous solution.
の減圧状態で沸騰・蒸発する蒸発缶と、この蒸発缶で発
生した水蒸気に対する凝縮器とからなり、更に、前記凝
縮器からの排出ガスに対する加熱手段と、この加熱した
排出ガスをアルカリ水溶液に直接的に接触する手段とを
備えていることを特徴とする廃水中の揮発性有機化合物
を分離・分解処理する装置。3. An evaporator, which evaporates and evaporates waste water containing a volatile organic compound under a reduced pressure below atmospheric pressure, and a condenser for water vapor generated in the evaporator, and further discharges from the condenser. An apparatus for separating and decomposing volatile organic compounds in waste water, comprising a heating means for gas and a means for directly contacting the heated exhaust gas with an alkaline aqueous solution.
吸収容器と、このガス吸収容器からの廃水を大気圧以下
の減圧状態で脱気する脱気容器とからなり、更に、前記
脱気容器からの排出ガスに対する加熱手段と、この加熱
した排出ガスをアルカリ水溶液に直接的に接触する手段
とを備えていることを特徴とする廃水中の揮発性有機化
合物を分離・分解処理する装置。4. A gas absorption container for wastewater containing a volatile organic compound, and a degassing container for degassing the wastewater from this gas absorption container under a reduced pressure of atmospheric pressure or less. An apparatus for separating and decomposing volatile organic compounds in wastewater, comprising: a heating means for the exhaust gas of the above and a means for directly contacting the heated exhaust gas with an alkaline aqueous solution.
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|---|---|---|---|
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|---|---|---|---|
| JP2001364994A JP3795796B2 (en) | 2001-11-29 | 2001-11-29 | Equipment for separating and decomposing volatile organic compounds in wastewater |
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| JP3795796B2 JP3795796B2 (en) | 2006-07-12 |
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Cited By (5)
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| JP2012040468A (en) * | 2010-08-16 | 2012-03-01 | Japan Organo Co Ltd | Wastewater treatment method and wastewater treatment apparatus |
| JP2015518416A (en) * | 2012-03-28 | 2015-07-02 | オーロテック ゲゼルシャフト ミット ベシュレンクテル ハフツングＡＵＲＯＴＥＣ ＧｍｂＨ | Pressure-regulated multi-reactor system |
| CN106277527A (en) * | 2016-08-31 | 2017-01-04 | 江苏南大环保科技有限公司 | The process of a kind of vinylidene chloride neutralized ratio and Application way |
| CN106925076A (en) * | 2017-04-20 | 2017-07-07 | 宁波检验检疫科学技术研究院 | A kind of organic waste gas treatment system |
| CN107716486A (en) * | 2017-09-30 | 2018-02-23 | 河南省农业科学院农业质量标准与检测技术研究所 | A kind of ultra-clean cleaning device of acidproof alkaline boiling and its cleaning fluid |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2012040468A (en) * | 2010-08-16 | 2012-03-01 | Japan Organo Co Ltd | Wastewater treatment method and wastewater treatment apparatus |
| JP2015518416A (en) * | 2012-03-28 | 2015-07-02 | オーロテック ゲゼルシャフト ミット ベシュレンクテル ハフツングＡＵＲＯＴＥＣ ＧｍｂＨ | Pressure-regulated multi-reactor system |
| JP2018108588A (en) * | 2012-03-28 | 2018-07-12 | オーロテック ゲゼルシャフト ミット ベシュレンクテル ハフツングＡＵＲＯＴＥＣ ＧｍｂＨ | Multi reactor system in which pressure is adjusted |
| US10913048B2 (en) | 2012-03-28 | 2021-02-09 | Aurotec Gmbh | Pressure-regulated multi-reactor system |
| CN106277527A (en) * | 2016-08-31 | 2017-01-04 | 江苏南大环保科技有限公司 | The process of a kind of vinylidene chloride neutralized ratio and Application way |
| CN106277527B (en) * | 2016-08-31 | 2019-07-19 | 南京大学 | A kind of processing of vinylidene chloride neutralized ratio and utilize method |
| CN106925076A (en) * | 2017-04-20 | 2017-07-07 | 宁波检验检疫科学技术研究院 | A kind of organic waste gas treatment system |
| CN107716486A (en) * | 2017-09-30 | 2018-02-23 | 河南省农业科学院农业质量标准与检测技术研究所 | A kind of ultra-clean cleaning device of acidproof alkaline boiling and its cleaning fluid |
| CN107716486B (en) * | 2017-09-30 | 2023-06-23 | 河南省农业科学院农业质量标准与检测技术研究所 | Acid and alkali resistant stewing and ultra-clean cleaning device and cleaning fluid thereof |
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