JP2002035541A - Method for recovering alcohols, etc., from waste gas - Google Patents
Method for recovering alcohols, etc., from waste gasInfo
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- JP2002035541A JP2002035541A JP2000226471A JP2000226471A JP2002035541A JP 2002035541 A JP2002035541 A JP 2002035541A JP 2000226471 A JP2000226471 A JP 2000226471A JP 2000226471 A JP2000226471 A JP 2000226471A JP 2002035541 A JP2002035541 A JP 2002035541A
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- gas
- adsorption
- exhaust gas
- adsorbent
- hydrocarbon gas
- Prior art date
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- Treating Waste Gases (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、排ガス中の炭化水
素ガス、アルコール類及びその他の揮発性有機化合物を
それらに適合した吸着剤に吸着させ、それらの吸着剤か
ら脱着させるのに際し、熱及び圧力を効率良く利用して
なる排ガス中の炭化水素ガス等の回収方法に関するもの
である。BACKGROUND OF THE INVENTION The present invention relates to a method for adsorbing hydrocarbon gas, alcohols and other volatile organic compounds in exhaust gas onto adsorbents suitable for the same, and desorbing from the adsorbents heat and heat. The present invention relates to a method for recovering hydrocarbon gas and the like in exhaust gas by utilizing pressure efficiently.
【０００２】[0002]
【従来の技術】光化学スモッグの原因物質である炭化水
素ガス等は、欧米はもとより、台湾、東南アジアにおい
ても、その排出濃度が法的に厳しく規制されている。日
本においても、大気汚染防止法による指針、悪臭防止法
及び各自治体の条例等で炭化水素ガス等の排出濃度が規
制されており、今後、これらの規制は更に厳しくなる方
向にある。2. Description of the Related Art The emission concentration of hydrocarbon gas, etc., which is a causative substance of photochemical smog, is strictly regulated not only in Europe and the United States but also in Taiwan and Southeast Asia. In Japan, too, the emission concentration of hydrocarbon gas and the like is regulated by the Air Pollution Control Law guidelines, the Odor Control Law, and the regulations of each local government, and these regulations are expected to become more stringent in the future.
【０００３】炭化水素ガス等の発生源として特に問題と
なるのは、貯留タンクとローリー車との間やタンカーと
貯留タンクとの間で揮発性炭化水素の受け渡しの際に発
生する排ガスである。この排ガスには１０〜３０％の高
濃度の炭化水素ガス等を含んでいる。次に問題となるの
は、塗装工場や印刷所等で使用する溶剤から発生する炭
化水素ガス等であり、濃度が数十〜数千ppm と低いが場
所的条件や数の点で大きな問題となる。このような排ガ
スの処理回収方法として、高濃度の炭化水素ガス等は吸
収液による吸収法が、低濃度では吸着剤による吸着法が
一般的である。A particularly problematic source of hydrocarbon gas and the like is exhaust gas generated when volatile hydrocarbons are transferred between a storage tank and a lorry or between a tanker and a storage tank. The exhaust gas contains a high concentration of hydrocarbon gas of 10 to 30%. The next problem is hydrocarbon gas generated from solvents used in painting factories and printing shops, etc., whose concentration is as low as several tens to several thousand ppm, but poses major problems in terms of location conditions and number. . As a method for treating and recovering such exhaust gas, an absorption method using an absorbent is generally used for a hydrocarbon gas or the like having a high concentration, and an adsorption method using an adsorbent is used at a low concentration.
【０００４】上記の吸着法には、固定床式と流動床式と
があり、吸着剤は活性炭、ゼオライト、シリカゲル等が
使用される。固定床式では、ＴＳＡ法（温度変動吸脱着
法）、ＰＳＡ法（圧力変動吸脱着法）及びこれら両者を
組み合わせたＴＰＳＡ法（温度・圧力変動吸脱着法）が
あり、炭化水素ガス等の種類や回収条件により、これら
を使い分ける。すなわち、ＴＳＡ法は、常温常圧下で炭
化水素ガス等を吸着剤にて吸着し高温常圧下で脱着する
もので、吸着剤の吸着容量が温度依存性を有することを
利用するものである。ＰＳＡ法は、昇圧下で炭化水素ガ
ス等を吸着し常圧下で脱着、あるいは常圧下で吸着し減
圧下で脱着するもので、吸着剤の吸着容量が圧力依存性
を有することを利用するものである。ＴＰＳＡ法は、常
温常圧下で吸着し高温減圧下で脱着するもので、ＴＳＡ
法とＰＳＡ法との双方の特徴を備えるものである。The above adsorption methods include a fixed bed type and a fluidized bed type, and activated carbon, zeolite, silica gel or the like is used as an adsorbent. The fixed bed type includes the TSA method (temperature fluctuation adsorption / desorption method), the PSA method (pressure fluctuation adsorption / desorption method), and the TPSA method (temperature / pressure fluctuation adsorption / desorption method) combining these two methods. These are used properly depending on the conditions and the recovery conditions. That is, the TSA method involves adsorbing a hydrocarbon gas or the like with an adsorbent at normal temperature and normal pressure and desorbing the gas under high temperature and normal pressure, and utilizes the fact that the adsorption capacity of the adsorbent has temperature dependence. The PSA method adsorbs hydrocarbon gas or the like at elevated pressure and desorbs it under normal pressure, or adsorbs at normal pressure and desorbs it under reduced pressure, and utilizes the fact that the adsorption capacity of an adsorbent has pressure dependency. is there. In the TPSA method, adsorption is performed at normal temperature and normal pressure and desorption is performed under high temperature and reduced pressure.
The method has characteristics of both of the method and the PSA method.
【０００５】[0005]
【発明が解決しようとする課題】上記ＴＳＡ法を用いた
アルコール類や炭化水素を含む排ガス処理は、活性炭が
アルコール類を吸着する能力が低いから使用できず、シ
リカゲルはアルコール類の吸着能力が優れているが、ア
ルコール類に伴い水を吸着すると発熱し、吸着した水の
量が多いと遂には破壊されてしまい、更にシリカゲルは
炭化水素の吸着能力が低い。従って、アルコール類や炭
化水素を含む排ガスは、ＴＳＡ法を用いて処理すること
が、現状では困難である。また、このＴＳＡ法では、吸
着剤からの脱着ガスを冷却凝縮して得た凝縮液から、比
重差を利用して水と炭化水素等とを分離するが、炭化水
素等の比重が水に近いと分離することができない。The treatment of exhaust gas containing alcohols and hydrocarbons using the above TSA method cannot be used because activated carbon has a low ability to adsorb alcohols, and silica gel has an excellent ability to adsorb alcohols. However, when water is adsorbed with alcohols, heat is generated when the water is adsorbed, and when the amount of adsorbed water is large, the water is finally destroyed, and silica gel has a low ability to adsorb hydrocarbons. Therefore, it is difficult at present to treat exhaust gas containing alcohols and hydrocarbons using the TSA method. In this TSA method, water and hydrocarbons are separated from the condensate obtained by cooling and condensing the desorbed gas from the adsorbent by utilizing the difference in specific gravity, but the specific gravity of hydrocarbons and the like is close to that of water. And cannot be separated.
【０００６】また、ＰＳＡ法では、炭化水素等を吸着し
た後の吸着剤からの脱着を空気等のイナートガスをパー
ジガスとして用いるが、排ガスと同程度の排気量を有す
る真空ポンプ等の減圧装置が必要となり、設備コスト及
び運転コストが莫大となり、現実的でない。In the PSA method, an inert gas such as air is used as a purge gas for desorption from an adsorbent after adsorbing hydrocarbons and the like, but a decompression device such as a vacuum pump having a displacement similar to that of exhaust gas is required. Therefore, equipment costs and operation costs become enormous, which is not practical.
【０００７】更に、ＴＳＡ法とＰＳＡ法との双方の特徴
を備えるＴＰＳＡ法では、炭化水素等を吸着した後の吸
着剤からの脱着に水蒸気を用いると排水が出るし、回収
液を再利用する場合に水分を嫌う回収液では水蒸気を用
いることができない。それでは、水蒸気を使わないと、
排ガス中の炭化水素等の濃度が数百ppm の低濃度では多
量の吸着剤が必要となり不経済となるし、更に空気等の
イナートガスをパージガスとして用いると、排ガスと同
程度の排気量を有する真空ポンプ等の減圧装置が必要と
なり、設備コスト及び運転コストが莫大となり、現実的
でない。Further, in the TPSA method having both characteristics of the TSA method and the PSA method, if steam is used for desorption from the adsorbent after adsorbing hydrocarbons or the like, wastewater is discharged and the recovered liquid is reused. In such a case, steam cannot be used in a recovery liquid that dislikes moisture. Then, without using steam,
If the concentration of hydrocarbons and the like in the exhaust gas is as low as several hundred ppm, a large amount of adsorbent is required, which is uneconomical.In addition, when an inert gas such as air is used as a purge gas, a vacuum having the same exhaust volume as the exhaust gas is used. A decompression device such as a pump is required, and equipment costs and operation costs become enormous, which is not practical.
【０００８】従って、本発明の目的は、アルコール類、
水と比重差の無い炭化水素、その他の揮発性有機化合物
を含む排ガスでも、多量の吸着剤を使うことなく吸着処
理でき、吸着剤からの脱着のためのパージガスに空気等
を用いても、排ガスと同程度の排気量を有する減圧装置
を必要としないで、設備コスト及び運転コストを低減す
ることができる排ガス中の炭化水素ガス等の回収方法を
提供することにある。Accordingly, an object of the present invention is to provide alcohols,
Exhaust gas containing hydrocarbons and other volatile organic compounds that have no specific gravity difference from water can be adsorbed without using a large amount of adsorbent, and even if air is used as a purge gas for desorption from the adsorbent, exhaust gas It is an object of the present invention to provide a method of recovering hydrocarbon gas or the like in exhaust gas, which can reduce equipment costs and operation costs without requiring a decompression device having the same displacement as the above.
【０００９】[0009]
【課題を解決するための手段】本発明者は、上記目的を
達成するため鋭意研究した結果、(1)排ガス中のアルコ
ール類を疎水化シリカゲルにて吸着し、また、排ガス中
に更に炭化水素類を含む場合は低濃度の炭化水素を疎水
性ゼオライトにて吸着し、(2)水との比重差のない炭化
水素に対しては沸点温度の差を利用して分離し、(3)パ
ージガスとして空気に代えて水蒸気を用い、減圧下で脱
着し減圧装置の手前で冷却凝縮して未凝縮ガスのみを減
圧装置にて吸引することで小型化し、(4)更に、低濃度
の炭化水素を含む排ガスでは活性炭で吸着し減圧下で加
熱空気にて脱着して炭化水素濃度を高め、次に、疎水化
シリカゲル及び疎水性ゼオライトで高濃度の炭化水素を
吸着し、パージガスとして加熱空気を用い減圧下で脱着
し、減圧装置の下流で冷却凝縮して排ガス中の低濃度の
炭化水素を回収できることなどを見出し、本発明を完成
するに至った。The present inventors have conducted intensive studies to achieve the above object. As a result, the present inventors have found that (1) alcohols in exhaust gas are adsorbed on hydrophobic silica gel, and hydrocarbons are further contained in the exhaust gas. If it contains water, low-concentration hydrocarbons are adsorbed by the hydrophobic zeolite, (2) hydrocarbons that have no specific gravity difference from water are separated using the difference in boiling point temperature, and (3) purge gas Using steam instead of air, desorbed under reduced pressure, cooled and condensed in front of the decompression device, and reduced the size by sucking only the uncondensed gas with the decompression device. (4) Further, low-concentration hydrocarbons were The exhaust gas contained is adsorbed with activated carbon, desorbed with heated air under reduced pressure to increase the hydrocarbon concentration, then adsorbed a high concentration of hydrocarbon with hydrophobic silica gel and hydrophobic zeolite, and decompressed using heated air as a purge gas. Desorption below, cooling downstream of the decompression device Condensation was found and can be recovered low concentration of hydrocarbons in the exhaust gas, thereby completing the present invention.
【００１０】すなわち、請求項１の発明は、アルコール
類を含む排ガスを、吸着工程と再生工程とを交互に繰り
返す１以上の吸着塔に導入して処理してなる排ガス中の
アルコール類等の回収方法において、前記吸着塔に疎水
化シリカゲル単独又は疎水化シリカゲルと疎水性ゼオラ
イトとの組合わせを吸着剤として充填し、前記吸着工程
にて前記吸着剤に排ガス中のアルコール類等を吸着除去
して大気放出し、前記再生工程にて前記吸着剤からアル
コール類等を水蒸気又は減圧下のパージガスにて脱着
し、該脱着ガスを冷却凝縮してアルコール類等を回収す
る排ガス中のアルコール類等の回収方法を提供するもの
である。[0010] That is, the invention of claim 1 recovers alcohols and the like in exhaust gas obtained by introducing and treating an exhaust gas containing alcohols into one or more adsorption towers in which an adsorption step and a regeneration step are alternately repeated. In the method, the adsorption tower is filled with hydrophobized silica gel alone or a combination of hydrophobized silica gel and hydrophobic zeolite as an adsorbent, and the adsorbent adsorbs and removes alcohols and the like in exhaust gas in the adsorption step. Release to the atmosphere, desorb alcohol and the like from the adsorbent in the regeneration step with water vapor or a purge gas under reduced pressure, and cool and condense the desorbed gas to recover alcohol and the like Recovering alcohol and the like in exhaust gas It provides a method.
【００１１】また、請求項２の発明は、炭化水素ガス等
を含む排ガスを、吸着工程と再生工程とを交互に繰り返
す１以上の吸着塔に導入して処理してなる排ガス中の炭
化水素ガス等の回収方法において、前記吸着工程にて前
記吸着塔に充填した吸着剤に排ガス中の炭化水素ガス等
を吸着除去して大気放出し、前記再生工程にて前記吸着
剤から炭化水素ガス等を水蒸気にて脱着し、該脱着ガス
を１次冷却して主に水蒸気を液体にした後、２次冷却し
て未凝縮の炭化水素ガス等を液体にして回収する排ガス
中の炭化水素ガス等の回収方法を提供するものである。[0011] Further, the invention of claim 2 provides a method for introducing and treating an exhaust gas containing a hydrocarbon gas or the like into one or more adsorption towers in which an adsorption step and a regeneration step are alternately repeated. In the recovery method, etc., in the adsorption step, the adsorbent filled in the adsorption tower adsorbs and removes the hydrocarbon gas and the like in the exhaust gas and releases it to the atmosphere, and in the regeneration step, removes the hydrocarbon gas and the like from the adsorbent. After desorbing with steam, the desorbed gas is primarily cooled to convert the steam into liquid mainly, and then secondary cooled to convert uncondensed hydrocarbon gas and the like into a liquid. It provides a collection method.
【００１２】また、請求項３の発明は、炭化水素ガス等
を含む排ガスを、吸着工程と再生工程とを交互に繰り返
す１以上の吸着塔に導入して処理してなる排ガス中の炭
化水素ガス等の回収方法において、前記吸着工程にて前
記吸着塔に充填した吸着剤に排ガス中の炭化水素ガス等
を吸着除去して大気放出し、前記再生工程にて前記吸着
塔内を減圧装置にて減圧し、その状態で水蒸気又は水蒸
気と空気との混合ガスにて前記吸着剤に吸着した炭化水
素ガス等を脱着し、該脱着ガスを冷却凝縮して主に水蒸
気を液体にした後、前記減圧装置の下流で冷却凝縮して
未凝縮の炭化水素ガス等を液体にして回収することを特
徴とする排ガス中の炭化水素ガス等の回収方法を提供す
るものである。[0012] The invention of claim 3 provides a hydrocarbon gas in an exhaust gas obtained by introducing and treating an exhaust gas containing a hydrocarbon gas or the like into one or more adsorption towers in which an adsorption step and a regeneration step are alternately repeated. In the recovery method, etc., in the adsorption step, the adsorbent filled in the adsorption tower adsorbs and removes the hydrocarbon gas and the like in the exhaust gas and discharges it to the atmosphere. The pressure is reduced, and in that state, the hydrocarbon gas or the like adsorbed on the adsorbent is desorbed with water vapor or a mixed gas of water vapor and air, and the desorbed gas is cooled and condensed to mainly convert water vapor into a liquid. It is intended to provide a method for recovering hydrocarbon gas and the like in exhaust gas, characterized in that uncondensed hydrocarbon gas and the like are cooled and condensed downstream of the apparatus and recovered as liquid.
【００１３】また、請求項４の発明は、炭化水素ガス等
を含む排ガスを、活性炭を充填した１以上の前吸着塔に
導入して吸着工程と再生工程とを交互に繰り返し処理す
る前処理と、該前処理による前処理脱着ガスを、疎水化
シリカゲル及び疎水性ゼオライトを吸着剤として充填し
た１以上の後吸着塔に導入して吸着工程と再生工程とを
交互に繰り返し処理する後処理と、からなり、前処理の
吸着工程にて活性炭に排ガス中の炭化水素ガス等を吸着
除去して大気放出し、前処理の再生工程にて前吸着塔内
を第１減圧装置にて減圧し、その状態で加熱空気又は清
浄化した加熱前処理済排ガスにて前記活性炭から炭化水
素ガス等を脱着し、この前処理脱着ガスを第１減圧装置
の下流で冷却して後処理の吸着工程に送り、後処理の吸
着工程にて吸着剤に前処理脱着ガス中の炭化水素ガス等
を吸着除去して大気放出し、後処理の再生工程にて後吸
着塔内を第２減圧装置にて減圧し、その状態で空気又は
清浄化した後処理済ガスにて前記吸着剤から炭化水素ガ
ス等を脱着し、この後処理脱着ガスを第２減圧装置の下
流で冷却凝縮して炭化水素ガス等を回収することを特徴
とする排ガス中の炭化水素ガス等の回収方法を提供する
ものである。[0013] Further, the present invention provides a pretreatment in which an exhaust gas containing a hydrocarbon gas or the like is introduced into one or more preadsorption towers filled with activated carbon, and an adsorption step and a regeneration step are alternately and repeatedly performed. A post-treatment in which the pre-treatment desorption gas by the pre-treatment is introduced into one or more post-adsorption towers filled with hydrophobic silica gel and hydrophobic zeolite as an adsorbent, and the adsorption step and the regeneration step are alternately and repeatedly performed; In the pretreatment adsorption step, the activated carbon absorbs and removes the hydrocarbon gas and the like in the exhaust gas and releases it to the atmosphere. In the pretreatment regeneration step, the pressure in the preadsorption tower is reduced by a first decompression device. In the state, hydrocarbon gas or the like is desorbed from the activated carbon with heated air or purified heated pre-treated exhaust gas, and the pre-treated desorbed gas is cooled downstream of the first decompression device and sent to a post-treatment adsorption step, Adsorbent in post-treatment adsorption process After treatment, the hydrocarbon gas etc. in the pretreatment desorbed gas is adsorbed and released to the atmosphere, and in the post-treatment regeneration step, the inside of the post-adsorption tower is depressurized by the second decompression device, and air or purified in that state. Hydrocarbon gas or the like from the adsorbent with the used gas, and the post-treatment desorbed gas is cooled and condensed downstream of the second decompression device to recover the hydrocarbon gas and the like. A method for recovering gas or the like is provided.
【００１４】[0014]
【発明の実施の形態】以下、本発明の実施の形態におけ
る排ガス中のアルコール類等の回収方法を図１〜図４を
参照して説明する。図１は本発明の実施の形態である排
ガス中のアルコール類等の回収方法を示すフロー図であ
る。図において、この排ガス中のアルコール類等の回収
方法は、ＴＳＡ法を応用したものであり、アルコール類
を含む排ガスを、吸着工程と再生工程とを交互に繰り返
す吸着塔１に導入して処理するものである。アルコール
類を含む排ガスには、炭化水素ガスやアルコール類以外
の揮発性有機化合物を含んでいてもよい。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS A method for recovering alcohols and the like in exhaust gas according to an embodiment of the present invention will be described below with reference to FIGS. FIG. 1 is a flowchart showing a method for recovering alcohols and the like in exhaust gas according to an embodiment of the present invention. In the figure, the method of recovering alcohols and the like in the exhaust gas is based on the TSA method, and the exhaust gas containing the alcohols is introduced into the adsorption tower 1 where the adsorption step and the regeneration step are alternately repeated to be treated. Things. The exhaust gas containing alcohols may contain volatile organic compounds other than hydrocarbon gas and alcohols.
【００１５】前記吸着塔１の構造は、固定床式であり、
その固定床上に疎水化シリカゲル単独、又は疎水化シリ
カゲルと疎水性ゼオライトを組合わせたものが充填され
ている。吸着工程は、吸着塔１にアルコール類の多い排
ガスを導入して、吸着剤のうち主に疎水化シリカゲルに
アルコール類を吸着させ、また、更に疎水性ゼオライト
に低濃度の炭化水素や他の揮発性有機化合物を吸着させ
て、これらを除去し清浄化して、処理済排ガスとして大
気に放出する。そして、吸着工程の終了は、タイマーに
おける設定時間の到達若しくは処理済排ガス中の炭化水
素ガス等の濃度が所定濃度に達することで、吸着剤の吸
着容量の限界に近づいて来たことを検知し、吸着塔１へ
の排ガスの供給を止めると共に処理済排ガスの大気放出
も止め、吸着工程を終了させ、再生工程に入る。The structure of the adsorption tower 1 is a fixed bed type.
The fixed bed is filled with hydrophobic silica gel alone or a combination of hydrophobic silica gel and hydrophobic zeolite. In the adsorption step, an exhaust gas containing a large amount of alcohol is introduced into the adsorption tower 1 so that alcohols are mainly adsorbed on the hydrophobized silica gel among the adsorbents, and low-concentration hydrocarbons and other volatile substances are further added to the hydrophobic zeolite. Organic compounds are adsorbed, removed and purified, and released to the atmosphere as treated exhaust gas. The end of the adsorption step is detected when the set time of the timer is reached or the concentration of the hydrocarbon gas or the like in the treated exhaust gas reaches the predetermined concentration, thereby approaching the limit of the adsorption capacity of the adsorbent. Then, the supply of the exhaust gas to the adsorption tower 1 is stopped, and the release of the treated exhaust gas to the atmosphere is also stopped.
【００１６】再生工程は、吸着塔１に水蒸気を送り塔内
の温度を上げ、吸着剤からアルコール類、炭化水素及び
他の揮発性有機化合物を脱着させ、その脱着ガスを水蒸
気と共に冷却器２に送り冷却凝縮させて、セパレータ３
にて凝縮液と未凝縮ガスとを分離し、凝縮液をセパレー
タ３から回収、更に凝縮液は比重差を利用した分離回収
も可能で、未凝縮ガスはセパレータ３を通り吸着塔１に
送られ循環する。再生工程の終了は、タイマーによる設
定時間の到達若しくは脱着ガスの炭化水素ガス等の濃度
が所定以下に達したことを検知し、吸着塔１への水蒸気
の供給を止めるとので行う。以下、上記と同じ吸着工程
と再生工程とを繰り返し、排ガス中の炭化水素ガス等を
回収すると共に排ガスを清浄化する。図１は、ＴＳＡ法
によるフロー図であるが、本実施の形態例では、このＴ
ＳＡ法に代えて、吸着塔に減圧下、パージガスによる脱
着を行うＰＳＡ法を利用してもよい。また、再生工程に
おいては、水蒸気の供給と減圧下のパージガスの供給と
を併用してもよい。In the regeneration step, steam is sent to the adsorption tower 1 to raise the temperature inside the tower, to desorb alcohols, hydrocarbons and other volatile organic compounds from the adsorbent, and the desorbed gas is sent to the cooler 2 together with the steam. Feed cooling and condensing, separator 3
To separate the condensed liquid from the uncondensed gas, recovering the condensed liquid from the separator 3. Further, the condensed liquid can be separated and recovered using the difference in specific gravity. The uncondensed gas is sent to the adsorption tower 1 through the separator 3. Circulate. The end of the regeneration step is performed when it is detected that the set time by the timer has been reached or the concentration of the hydrocarbon gas or the like in the desorbed gas has reached a predetermined value or less, and the supply of steam to the adsorption tower 1 is stopped. Hereinafter, the same adsorption step and regeneration step as described above are repeated to collect hydrocarbon gas and the like in the exhaust gas and to purify the exhaust gas. FIG. 1 is a flow chart based on the TSA method.
Instead of the SA method, a PSA method of desorbing the adsorption tower with a purge gas under reduced pressure may be used. In the regeneration step, the supply of steam and the supply of purge gas under reduced pressure may be used in combination.
【００１７】図２は本発明の実施の形態である他の排ガ
ス中の炭化水素ガス等の回収方法を示すフロー図であ
る。この排ガス中の炭化水素ガス等の回収方法は、排ガ
ス中に含まれる炭化水素や他の揮発性有機化合物等の比
重が水と大差無い場合に適用されるものであり、吸着工
程は図１の回収方法と同様であるが、吸着剤は疎水化シ
リカゲルや疎水性ゼオライトでなくても良く、排ガス中
に含まれる炭化水素ガス等の種類により選定され、活性
炭を使用しても良い。そして、図１の場合と同様に、図
２における再生工程の吸着塔１からの脱着ガスを水蒸気
と共に第１冷却器４に送り、１次冷却して主に水蒸気を
液体にした後、第１セパレータ５にて第１凝縮液と第１
未凝縮ガスとに分離し、第１凝縮液を第１セパレータ５
から取り出す。第１セパレータ５を通過した第１未凝縮
ガスを、第２冷却器６にて２次冷却して主に炭化水素ガ
ス等を凝縮した後、第２セパレータ７にて第２凝縮液と
第２未凝縮ガスとに分離し、第２凝縮液を第２セパレー
タ７から回収する。第２セパレータ７を通過した第２未
凝縮ガスは吸着塔１に送られ循環する。再生工程の終了
は、図１と同様に、タイマーにおける設定時間の到達若
しくは脱着ガスの炭化水素ガス等の濃度が所定以下に達
したことを検知して行う。以下、図１と同じ吸着工程と
上記した再生工程とを繰り返し、排ガス中の炭化水素ガ
ス等を回収すると共に排ガスを清浄化する。なお、第１
冷却器４の温度は、第２冷却器６の温度より高い。FIG. 2 is a flowchart showing a method of recovering hydrocarbon gas and the like in exhaust gas according to another embodiment of the present invention. This method of recovering hydrocarbon gas and the like in the exhaust gas is applied when the specific gravity of hydrocarbons and other volatile organic compounds contained in the exhaust gas is not much different from that of water. It is the same as the recovery method, but the adsorbent may not be hydrophobic silica gel or hydrophobic zeolite, but is selected according to the type of hydrocarbon gas or the like contained in the exhaust gas, and activated carbon may be used. Then, as in the case of FIG. 1, the desorbed gas from the adsorption tower 1 in the regeneration step in FIG. 2 is sent to the first cooler 4 together with the steam, and the primary cooling is performed to mainly convert the steam into a liquid. The first condensate and the first condensate
The first condensate is separated into uncondensed gas and the first condensate
Remove from The first uncondensed gas that has passed through the first separator 5 is secondarily cooled by the second cooler 6 to condense mainly hydrocarbon gas and the like, and then the second condensate and the second It is separated into uncondensed gas and the second condensate is recovered from the second separator 7. The second uncondensed gas that has passed through the second separator 7 is sent to the adsorption tower 1 and circulated. The end of the regeneration step is performed, similarly to FIG. 1, by detecting that the set time of the timer has been reached or that the concentration of the hydrocarbon gas or the like of the desorbed gas has reached a predetermined value or less. Hereinafter, the same adsorption step as in FIG. 1 and the above-mentioned regeneration step are repeated to collect hydrocarbon gas and the like in the exhaust gas and to purify the exhaust gas. The first
The temperature of the cooler 4 is higher than the temperature of the second cooler 6.
【００１８】図３は本発明の実施の形態である他の排ガ
ス中の炭化水素ガス等の回収方法を示すフロー図であ
る。この排ガス中の炭化水素ガス等の回収方法は、ＰＳ
Ａ法を応用し、減圧装置の容量を小型化したものであ
り、吸着工程は図１、２の回収方法と同様であるが、吸
着剤は疎水化シリカゲル又は疎水性ゼオライトでなくて
も良く、排ガス中に含まれる炭化水素ガス等の種類によ
り選定され、活性炭を使用しても良い。FIG. 3 is a flow chart showing a method of recovering hydrocarbon gas and the like in exhaust gas according to another embodiment of the present invention. The method for recovering hydrocarbon gas and the like in this exhaust gas is PS
The method A is applied, and the capacity of the decompression device is reduced. The adsorption step is the same as the recovery method of FIGS. 1 and 2, but the adsorbent may not be hydrophobic silica gel or hydrophobic zeolite. Activated carbon may be used depending on the type of hydrocarbon gas contained in the exhaust gas.
【００１９】そして、再生工程では、図１、２の場合と
違って吸着塔１０内を減圧装置、例えば、真空ポンプ１
１にて減圧し、その状態で水蒸気又は水蒸気＋空気等の
混合ガスをパージガスとして吸着塔１０内に送り、吸着
剤から炭化水素等を脱着させ、その脱着ガスをパージガ
スと共に第１冷却器１２に送り１次冷却して主に水蒸気
を液化した後、第１セパレータ１３にて第１凝縮液（主
に水）と第１未凝縮ガスとに分離し、第１凝縮液を第１
セパレータ１３から取り出す。第１セパレータ１３及び
真空ポンプ１１を通過した第１未凝縮ガスを、第２冷却
器１４にて２次冷却して主に炭化水素ガス等を凝縮した
後、第２セパレータ１５にて第２凝縮液と第２未凝縮ガ
スとに分離し、第２凝縮液を第２セパレータ１５から取
り出す。この際、第２凝縮液を比重差を利用して凝縮水
と炭化水素液とに分離回収することもできる。第２セパ
レータ１５を通過した第２未凝縮ガスは吸着塔１０に送
られ循環する。再生工程の終了は、図１の場合と同様で
ある。以下、吸着工程と再生工程とを繰り返し、排ガス
中の炭化水素ガス等を回収すると共に排ガスを清浄化す
る。In the regeneration step, unlike in the case of FIGS. 1 and 2, the inside of the adsorption tower 10 is depressurized, for example, a vacuum pump 1.
The pressure is reduced at 1, and in that state, a mixed gas such as steam or steam + air is sent as a purge gas into the adsorption tower 10 to desorb hydrocarbons and the like from the adsorbent, and the desorbed gas is sent to the first cooler 12 together with the purge gas. After the primary cooling and primary liquefaction of the water vapor, the first condensate (mainly water) and the first uncondensed gas are separated by the first separator 13 and the first condensate is separated into the first condensate by the first separator 13.
Take out from the separator 13. The first uncondensed gas that has passed through the first separator 13 and the vacuum pump 11 is secondarily cooled by the second cooler 14 to condense mainly hydrocarbon gas and the like, and then secondly condensed by the second separator 15. The liquid is separated into a liquid and a second uncondensed gas, and the second condensed liquid is taken out from the second separator 15. At this time, the second condensate can be separated and recovered into a condensed water and a hydrocarbon liquid by utilizing a specific gravity difference. The second uncondensed gas that has passed through the second separator 15 is sent to the adsorption tower 10 and circulated. The end of the regeneration step is the same as in FIG. Hereinafter, the adsorption step and the regeneration step are repeated to collect the hydrocarbon gas and the like in the exhaust gas and to purify the exhaust gas.
【００２０】図４は本発明の実施の形態である他の排ガ
ス中の炭化水素ガス等の回収方法を示すフロー図であ
る。この排ガス中の炭化水素ガス等の回収方法は、ＰＴ
ＳＡ法とＰＳＡ法とを組み合わせ応用し、低濃度の炭化
水素ガス等を水蒸気を使用しないで、効率よく回収する
ものであり、炭化水素ガス等を含む排ガスを、活性炭を
充填した前吸着塔２０に導入して吸着工程と再生工程と
を交互に繰り返し処理する前処理と、該前処理による前
処理脱着ガスを、疎水化シリカゲル及び疎水性ゼオライ
トを吸着剤として充填した後吸着塔２１に導入して吸着
工程と再生工程とを交互に繰り返し処理する後処理と、
からなるものである。FIG. 4 is a flow chart showing a method of recovering hydrocarbon gas and the like in exhaust gas according to another embodiment of the present invention. The method for recovering hydrocarbon gas and the like in this exhaust gas is PT
The method combines the SA method and the PSA method to efficiently recover low-concentration hydrocarbon gas and the like without using water vapor. A pretreatment in which the adsorption step and the regeneration step are alternately and repeatedly performed, and a pretreatment desorption gas obtained by the pretreatment is introduced into the adsorption tower 21 after filling with hydrophobic silica gel and hydrophobic zeolite as an adsorbent. Post-treatment in which the adsorption step and the regeneration step are alternately and repeatedly performed,
It consists of
【００２１】前処理における前吸着塔２０の構造は、固
定床式であり、その固定床上に活性炭が充填されてい
る。この前吸着塔２０に排ガスを導入して、活性炭に炭
化水素ガス等を吸着させて、これらを除去し清浄化し
て、前処理済排ガスとして大気に放出する。そして、タ
イマーにおける設定時間の到達若しくは処理済排ガス中
の炭化水素ガス等の濃度が所定濃度に達することで、活
性炭の吸着容量の限界に近づいて来たことを検知し、前
吸着塔２０への排ガスの供給を止めると共に前処理済排
ガスの大気放出も止め、吸着工程を終了させ再生工程に
入る。この再生工程では、前吸着塔２０内を第１減圧装
置である第１真空ポンプ２２にて減圧し、その状態で加
熱器２３を通した加熱空気あるいは清浄化した加熱前処
理済排ガスをパージガスとして前吸着塔２０内に送り、
活性炭から炭化水素ガス等を脱着させ、その前処理脱着
ガスをパージガスと共に第１真空ポンプ２２を経て前冷
却器２４に送り冷却してから、後処理の吸着工程にある
後吸着塔２１内に送る。The structure of the pre-adsorption tower 20 in the pre-treatment is of a fixed bed type, and the fixed bed is filled with activated carbon. Exhaust gas is introduced into the pre-adsorption tower 20, and the activated carbon adsorbs hydrocarbon gas and the like, removes and cleans them, and releases it to the atmosphere as pre-treated exhaust gas. When the set time reached by the timer or the concentration of hydrocarbon gas or the like in the treated exhaust gas reaches a predetermined concentration, it is detected that the limit of the adsorption capacity of the activated carbon has been approached. The supply of the exhaust gas is stopped, and the release of the pretreated exhaust gas to the atmosphere is also stopped. In this regeneration step, the inside of the pre-adsorption tower 20 is depressurized by the first vacuum pump 22 which is the first decompression device, and in this state, heated air passed through the heater 23 or purified exhaust gas after heating is used as a purge gas. Sent into the pre-adsorption tower 20,
Hydrocarbon gas and the like are desorbed from the activated carbon, and the pretreatment desorption gas is sent to the precooler 24 via the first vacuum pump 22 together with the purge gas to be cooled, and then sent into the post-adsorption tower 21 in the post-treatment adsorption step. .
【００２２】この後吸着塔２１内の疎水化シリカゲル及
び／又は疎水性ゼオライトである吸着剤に前処理脱着ガ
ス中の炭化水素ガス等を吸着させて、これらを除去し清
浄化して、後処理済ガスとして大気に放出するか、又は
吸着工程の前吸着塔に導入する。そして、前処理の場合
と同様に吸着剤の吸着容量の限界を検知し、吸着工程を
終了させ再生工程に入る。この再生工程では、後吸着塔
２１内を第２真空ポンプ２５にて減圧し、その状態で空
気あるいは後処理済ガスをパージガスとして後吸着塔２
１内送り、吸着剤から炭化水素ガス等を脱着させ、その
後処理脱着ガスをパージガスと共に第２真空ポンプ２５
を経て後冷却器２６に送り冷却凝縮し、セパレータ２７
にて凝縮液と未凝縮ガスとを分離し、凝縮液をセパレー
タ２７から回収、更に凝縮液は比重差を利用した分離回
収も可能で、未凝縮ガスはセパレータ２７を通り前吸着
塔２０に送られ循環する。再生工程の終了は、タイマー
による設定時間の到達若しくは後処理脱着ガスの炭化水
素ガス等の濃度が所定以下に達したことを検知して行
う。以下、上記と同じ前処理の吸着工程と再生工程とを
繰り返し、更に上記と同じ後処理の吸着工程と再生工程
とを繰り返して、排ガス中の炭化水素ガス等を回収する
と共に排ガスを清浄化する。Thereafter, the adsorbent, which is a hydrophobic silica gel and / or a hydrophobic zeolite, in the adsorption tower 21 is made to adsorb the hydrocarbon gas and the like in the pretreatment desorbed gas, and these are removed and cleaned, and the post-treatment is performed. It is released to the atmosphere as a gas or introduced into the adsorption tower before the adsorption step. Then, similarly to the case of the pretreatment, the limit of the adsorbing capacity of the adsorbent is detected, and the adsorbing step is terminated to start the regeneration step. In this regeneration step, the interior of the post-adsorption tower 21 is depressurized by the second vacuum pump 25, and air or a post-treated gas is used as a purge gas in that state.
1 to desorb hydrocarbon gas and the like from the adsorbent, and then treat the desorbed gas together with the purge gas to the second vacuum pump 25.
, And then sent to the cooler 26 to be cooled and condensed.
The condensed liquid is separated from the uncondensed gas by the separator, and the condensed liquid is recovered from the separator 27. Further, the condensed liquid can be separated and recovered by utilizing a difference in specific gravity. The uncondensed gas is sent to the pre-adsorption tower 20 through the separator 27. And circulate. The end of the regeneration process is performed by detecting that the time set by the timer has been reached or that the concentration of hydrocarbon gas or the like in the post-treatment desorption gas has reached a predetermined value or less. Hereinafter, the same pretreatment adsorption step and regeneration step as above are repeated, and further the same post-treatment adsorption step and regeneration step as above are repeated to collect hydrocarbon gas and the like in the exhaust gas and purify the exhaust gas. .
【００２３】以上、本発明の実施の形態として、図１〜
図４において吸着塔１、１０、前吸着塔２０、後吸着塔
２１が１塔である場合についてのみ説明したが、複数塔
であっても良く、更に、具体的な構成はこれに限定され
ず、本発明の要旨を逸脱しない範囲ないでの変更、追加
は本発明の範囲内である。As described above, as an embodiment of the present invention, FIGS.
In FIG. 4, only the case where the number of the adsorption towers 1, 10, the pre-adsorption tower 20, and the post-adsorption tower 21 is one is described, but a plurality of towers may be used, and the specific configuration is not limited to this. Modifications and additions without departing from the gist of the present invention are within the scope of the present invention.
【００２４】[0024]
【発明の効果】請求項１の発明によれば、アルコール類
を含む排ガス又はアルコール類や低濃度の炭化水素を含
む排ガスに対し、アルコール類の吸着特性の良い疎水化
シリカゲルにてアルコール類を吸着し、必要であるなら
炭化水素の吸着特性の良い疎水性ゼオライトにて更に低
濃度の炭化水素を吸着するから、多量の吸着剤を必要と
せず、アルコール類に付随する水による疎水化シリカゲ
ルの破壊も無く、排ガスを清浄化すると共に、アルコー
ル類や低濃度の炭化水素を回収することができる。According to the first aspect of the present invention, alcohols are adsorbed on exhaust gas containing alcohols or exhaust gas containing alcohols or low-concentration hydrocarbons using hydrophobic silica gel having good alcohol adsorption characteristics. If necessary, the hydrophobic zeolite, which has good hydrocarbon adsorption properties, adsorbs even lower concentrations of hydrocarbons, eliminating the need for a large amount of adsorbent and destroying hydrophobic silica gel with water accompanying alcohols. In addition, it is possible to purify exhaust gas and recover alcohols and low-concentration hydrocarbons.
【００２５】請求項２の発明によれば、比重差による分
離回収ができない場合であっても、吸着剤からの脱着ガ
スに含まれる炭化水素等や水の沸点に合わせて冷却温度
を２段以上に変えるから、炭化水素等と水あるいは炭化
水素等同士を分離回収することができる。According to the second aspect of the present invention, even when the separation and recovery cannot be performed due to the difference in specific gravity, the cooling temperature is set to two or more stages in accordance with the boiling point of hydrocarbons and water contained in the desorbed gas from the adsorbent. Therefore, hydrocarbons and the like and water or hydrocarbons and the like can be separated and recovered.
【００２６】請求項３の発明によれば、炭化水素等の吸
着剤からの脱着の際、パージガスとして水蒸気を用いて
脱着ガスを得、この脱着ガスを減圧装置の手前で水蒸気
を凝縮して未凝縮ガスのみとして減少させることで、減
圧装置の容量を大幅に小さくできる。According to the third aspect of the present invention, when desorbing from an adsorbent such as a hydrocarbon, a desorbed gas is obtained by using steam as a purge gas, and the desorbed gas is condensed with steam before the pressure reducing device. By reducing only the condensed gas, the capacity of the pressure reducing device can be significantly reduced.
【００２７】請求項４の発明によれば、低濃度の炭化水
素を含む排ガスを活性炭で吸着し減圧下で加熱空気にて
脱着して高濃度の炭化水素を含む脱着ガスとし、次に疎
水化シリカゲル又は疎水性ゼオライトで高濃度の炭化水
素を吸着し、パージガスとして空気を用い減圧下で脱着
し減圧装置の下流で冷却凝縮して回収するから、排ガス
中の低濃度の炭化水素を回収できることは無論のこと、
排水が無く、水を嫌う炭化水素等を回収でき、多量の吸
着剤を必要とせず、しかも減圧装置の容量は排ガス中の
炭化水素濃度と脱着ガス中の炭化水素濃度との比率に反
比例して減らすことができる。According to the fourth aspect of the present invention, an exhaust gas containing a low concentration of hydrocarbons is adsorbed by activated carbon and desorbed by heating air under reduced pressure to obtain a desorption gas containing a high concentration of hydrocarbons. Since high concentration hydrocarbons are adsorbed by silica gel or hydrophobic zeolite, desorbed under reduced pressure using air as a purge gas, and cooled and condensed downstream of the decompression device, the low concentration hydrocarbons in the exhaust gas can be recovered. Of course,
There is no waste water, it can recover hydrocarbons that dislike water, it does not require a large amount of adsorbent, and the capacity of the pressure reducing device is inversely proportional to the ratio between the hydrocarbon concentration in the exhaust gas and the hydrocarbon concentration in the desorbed gas. Can be reduced.
【図１】本発明の実施の形態である排ガス中の炭化水素
ガス等の回収方法のフロー図である。FIG. 1 is a flowchart of a method for recovering a hydrocarbon gas or the like in an exhaust gas according to an embodiment of the present invention.
【図２】本発明の他の実施の形態である排ガス中の炭化
水素ガス等の回収方法のフロー図である。FIG. 2 is a flowchart of a method for recovering hydrocarbon gas or the like in exhaust gas according to another embodiment of the present invention.
【図３】本発明の他の実施の形態である排ガス中の炭化
水素ガス等の回収方法のフロー図である。FIG. 3 is a flowchart of a method for recovering hydrocarbon gas or the like in exhaust gas according to another embodiment of the present invention.
【図４】本発明の他の実施の形態である排ガス中の炭化
水素ガス等の回収方法のフロー図である。FIG. 4 is a flowchart of a method for recovering hydrocarbon gas or the like in exhaust gas according to another embodiment of the present invention.
１、１０ 吸着塔 ２ 冷却器 ３、２７ セパレータ ４、１２ 第１冷却器 ５、１３ 第１セパレータ ６、１４ 第２冷却器 ７、１５ 第２セパレータ １１ 真空ポンプ ２０ 前吸着塔 ２１ 後吸着塔 ２２ 第１真空ポンプ ２３ 加熱器２３ ２４ 前冷却器２４ ２５ 第２真空ポンプ ２６ 後冷却器 1, 10 adsorption tower 2 cooler 3, 27 separator 4, 12 first cooler 5, 13 first separator 6, 14 second cooler 7, 15 second separator 11 vacuum pump 20 pre-adsorption tower 21 post-adsorption tower 22 First vacuum pump 23 Heater 23 24 Precooler 24 25 Second vacuum pump 26 Postcooler
───────────────────────────────────────────────────── 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） Ｃ１０Ｇ 5/02 Ｆターム(参考） 4D002 AA33 AA34 AA40 AB03 AC10 BA04 DA41 DA45 DA46 EA08 FA01 4H006 AA02 AD17 AD18 BA32 BA33 BA71 ──────────────────────────────────────────────────続 き Continued on the front page (51) Int.Cl. 7 Identification symbol FI Theme coat ゛ (Reference) C10G 5/02 F term (Reference) 4D002 AA33 AA34 AA40 AB03 AC10 BA04 DA41 DA45 DA46 EA08 FA01 4H006 AA02 AD17 AD18 BA32 BA33 BA71
Claims (4)
と再生工程とを交互に繰り返す１以上の吸着塔に導入し
て処理してなる排ガス中のアルコール類等の回収方法に
おいて、前記吸着塔に疎水化シリカゲル単独又は疎水化
シリカゲルと疎水性ゼオライトとの組合わせを吸着剤と
して充填し、前記吸着工程にて前記吸着剤に排ガス中の
アルコール類等を吸着除去して大気放出し、前記再生工
程にて前記吸着剤からアルコール類等を水蒸気又は減圧
下のパージガスにて脱着し、該脱着ガスを冷却凝縮して
アルコール類等を回収することを特徴とする排ガス中の
アルコール類等の回収方法。1. A method for recovering alcohols and the like in exhaust gas obtained by introducing and treating an exhaust gas containing alcohols into one or more adsorption towers in which an adsorption step and a regeneration step are alternately repeated. Hydrophobized silica gel alone or a combination of hydrophobized silica gel and hydrophobic zeolite is filled as an adsorbent, and in the adsorption step, the adsorbent adsorbs and removes alcohols and the like in exhaust gas to release to the atmosphere, and the regeneration step A method of recovering alcohols and the like in exhaust gas, wherein alcohols and the like are desorbed from the adsorbent with water vapor or a purge gas under reduced pressure, and the desorbed gas is cooled and condensed to recover the alcohols and the like.
程と再生工程とを交互に繰り返す１以上の吸着塔に導入
して処理してなる排ガス中の炭化水素ガス等の回収方法
において、前記吸着工程にて前記吸着塔に充填した吸着
剤に排ガス中の炭化水素ガス等を吸着除去して大気放出
し、前記再生工程にて前記吸着剤から炭化水素ガス等を
水蒸気にて脱着し、該脱着ガスを１次冷却して主に水蒸
気を液体にした後、２次冷却して未凝縮の炭化水素ガス
等を液体にして回収することを特徴とする排ガス中の炭
化水素ガス等の回収方法。2. A method for recovering hydrocarbon gas or the like in an exhaust gas obtained by introducing and treating an exhaust gas containing a hydrocarbon gas or the like into one or more adsorption towers in which an adsorption step and a regeneration step are alternately repeated. In the adsorption step, the adsorbent filled in the adsorption tower adsorbs and removes the hydrocarbon gas and the like in the exhaust gas and releases it to the atmosphere, and in the regeneration step, desorbs the hydrocarbon gas and the like from the adsorbent with water vapor. A method for recovering hydrocarbon gas or the like in an exhaust gas, comprising first cooling the desorbed gas to convert mainly water vapor into a liquid, and then secondary cooling and converting the uncondensed hydrocarbon gas or the like to a liquid. .
程と再生工程とを交互に繰り返す１以上の吸着塔に導入
して処理してなる排ガス中の炭化水素ガス等の回収方法
において、前記吸着工程にて前記吸着塔に充填した吸着
剤に排ガス中の炭化水素ガス等を吸着除去して大気放出
し、前記再生工程にて前記吸着塔内を減圧装置にて減圧
し、その状態で水蒸気又は水蒸気と空気との混合ガスに
て前記吸着剤に吸着した炭化水素ガス等を脱着し、該脱
着ガスを冷却凝縮して主に水蒸気を液体にした後、前記
減圧装置の下流で冷却凝縮して未凝縮の炭化水素ガス等
を液体にして回収することを特徴とする排ガス中の炭化
水素ガス等の回収方法。3. A method for recovering hydrocarbon gas or the like in an exhaust gas obtained by introducing and treating an exhaust gas containing a hydrocarbon gas or the like into one or more adsorption towers in which an adsorption step and a regeneration step are alternately repeated. In the adsorption step, the adsorbent filled in the adsorption tower adsorbs and removes the hydrocarbon gas and the like in the exhaust gas and releases it to the atmosphere. In the regeneration step, the pressure in the adsorption tower is reduced by a decompression device. Alternatively, a hydrocarbon gas or the like adsorbed on the adsorbent is desorbed with a mixed gas of steam and air, and the desorbed gas is cooled and condensed to mainly turn water vapor into a liquid, and then cooled and condensed downstream of the pressure reducing device. Recovering uncondensed hydrocarbon gas or the like by converting it into a liquid.
を充填した１以上の前吸着塔に導入して吸着工程と再生
工程とを交互に繰り返し処理する前処理と、該前処理に
よる前処理脱着ガスを、疎水化シリカゲル及び疎水性ゼ
オライトを吸着剤として充填した１以上の後吸着塔に導
入して吸着工程と再生工程とを交互に繰り返し処理する
後処理と、からなり、 前処理の吸着工程にて活性炭に排ガス中の炭化水素ガス
等を吸着除去して大気放出し、前処理の再生工程にて前
吸着塔内を第１減圧装置にて減圧し、その状態で加熱空
気又は清浄化した加熱前処理済排ガスにて前記活性炭か
ら炭化水素ガス等を脱着し、この前処理脱着ガスを第１
減圧装置の下流で冷却して後処理の吸着工程に送り、 後処理の吸着工程にて吸着剤に前処理脱着ガス中の炭化
水素ガス等を吸着除去して大気放出し、後処理の再生工
程にて後吸着塔内を第２減圧装置にて減圧し、その状態
で空気又は清浄化した後処理済ガスにて前記吸着剤から
炭化水素ガス等を脱着し、この後処理脱着ガスを第２減
圧装置の下流で冷却凝縮して炭化水素ガス等を回収する
ことを特徴とする排ガス中の炭化水素ガス等の回収方
法。4. A pretreatment in which an exhaust gas containing a hydrocarbon gas or the like is introduced into one or more preadsorption towers filled with activated carbon, and an adsorption step and a regeneration step are alternately and repeatedly processed, and a pretreatment by the pretreatment. A post-treatment in which the desorption gas is introduced into one or more post-adsorption towers filled with hydrophobized silica gel and hydrophobic zeolite as an adsorbent, and an adsorption step and a regeneration step are alternately and repeatedly performed. In the process, the activated carbon absorbs and removes hydrocarbon gas and the like in the exhaust gas and releases it to the atmosphere. In the pretreatment regeneration process, the pressure in the pre-adsorption tower is reduced by the first decompression device, and then heated air or purified Hydrocarbon gas and the like are desorbed from the activated carbon with the heated pretreated exhaust gas, and the pretreated desorbed gas is
Cooled downstream of the decompression device and sent to the post-treatment adsorption step. In the post-treatment adsorption step, the adsorbent adsorbs and removes the hydrocarbon gas etc. in the pretreatment desorbed gas and releases it to the atmosphere. The pressure in the post-adsorption tower is reduced by a second decompressor, and in that state, hydrocarbon gas or the like is desorbed from the adsorbent with air or a purified post-processed gas. A method for recovering hydrocarbon gas and the like in exhaust gas, comprising cooling and condensing a hydrocarbon gas and the like downstream of a pressure reducing device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000226471A JP2002035541A (en) | 2000-07-27 | 2000-07-27 | Method for recovering alcohols, etc., from waste gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000226471A JP2002035541A (en) | 2000-07-27 | 2000-07-27 | Method for recovering alcohols, etc., from waste gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JP2002035541A true JP2002035541A (en) | 2002-02-05 |
Family
ID=18720082
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2000226471A Pending JP2002035541A (en) | 2000-07-27 | 2000-07-27 | Method for recovering alcohols, etc., from waste gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2002035541A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010116720A1 (en) * | 2009-04-07 | 2010-10-14 | シャープ株式会社 | Vacuum insulation material and device provided with same |
| JP2013540707A (en) * | 2010-08-26 | 2013-11-07 | コリア インスティチュート オブ エナジー リサーチ | Method and apparatus for recovering ethylene from fluid catalytic cracking exhaust gas |
| CN114887441A (en) * | 2022-05-05 | 2022-08-12 | 紫科装备股份有限公司 | Treatment process for VOCs in crude oil |
| CN115491231A (en) * | 2022-10-21 | 2022-12-20 | 中国石油化工股份有限公司 | Isoparaffin solvent refining system and refining method |
-
2000
- 2000-07-27 JP JP2000226471A patent/JP2002035541A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010116720A1 (en) * | 2009-04-07 | 2010-10-14 | シャープ株式会社 | Vacuum insulation material and device provided with same |
| JP2013540707A (en) * | 2010-08-26 | 2013-11-07 | コリア インスティチュート オブ エナジー リサーチ | Method and apparatus for recovering ethylene from fluid catalytic cracking exhaust gas |
| US9090522B2 (en) | 2010-08-26 | 2015-07-28 | Korea Institute Of Energy Research | Method and apparatus for recovering ethylene from fluidized catalytic cracking (FCC) off-gas |
| CN114887441A (en) * | 2022-05-05 | 2022-08-12 | 紫科装备股份有限公司 | Treatment process for VOCs in crude oil |
| CN114887441B (en) * | 2022-05-05 | 2022-12-02 | 紫科装备股份有限公司 | Treatment process for VOCs in crude oil |
| CN115491231A (en) * | 2022-10-21 | 2022-12-20 | 中国石油化工股份有限公司 | Isoparaffin solvent refining system and refining method |
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