JPH0938451A - Method for recovering solvent - Google Patents
Method for recovering solventInfo
- Publication number
- JPH0938451A JPH0938451A JP7198446A JP19844695A JPH0938451A JP H0938451 A JPH0938451 A JP H0938451A JP 7198446 A JP7198446 A JP 7198446A JP 19844695 A JP19844695 A JP 19844695A JP H0938451 A JPH0938451 A JP H0938451A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- concentration
- solvent
- concn
- exhaust gas
- 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.)
- Granted
Links
Landscapes
- Separation Of Gases By Adsorption (AREA)
- Treating Waste Gases (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は化学工場において有
機溶剤を溶媒として用いる製膜工程、塗布工程等におい
て、蒸発した溶剤を吸着剤を用いて回収する溶剤回収処
理方法に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a solvent recovery treatment method for recovering an evaporated solvent by using an adsorbent in a film forming process, a coating process and the like using an organic solvent as a solvent in a chemical factory.
【０００２】[0002]
【従来の技術】溶剤濃度の異なる少なくとも３種以上の
溶剤含有排ガスを発生させる工程として製膜工程、塗布
工程等がある。これらの工程で発生する溶剤を処理する
溶剤回収方法として、各溶剤排ガス発生源よりの溶剤含
有排ガスをそれぞれ冷却器で冷却した後、送風機によっ
て混合してから吸着装置に送り吸着剤に溶剤を吸着させ
ていた。吸着塔の排ガスはそのまま排気するか、又はフ
ィルターを通してから再び送風機で循環処理してもよ
い。一方、吸着装置には加熱再生用気体を送って吸着剤
に吸着された溶剤を脱着し、これをコンデンサーにおい
て凝縮し、溶剤を溶剤貯蔵タンクに回収していた。吸着
装置には２塔を使用して、相互に吸着と脱着回収を各バ
ルブの切替によって行い連続操業を行なっていた。2. Description of the Related Art As a process for generating at least three kinds of solvent-containing exhaust gas having different solvent concentrations, there are a film forming process and a coating process. As a solvent recovery method for treating the solvent generated in these steps, after cooling the solvent-containing exhaust gas from each solvent exhaust gas source with a cooler, respectively, after mixing with a blower send to the adsorption device adsorb the solvent to the adsorbent I was letting it. The exhaust gas from the adsorption tower may be exhausted as it is, or may be passed through a filter and then circulated again by a blower. On the other hand, heating regeneration gas was sent to the adsorption device to desorb the solvent adsorbed by the adsorbent, which was condensed in the condenser and the solvent was collected in the solvent storage tank. Two towers were used as an adsorption device, and adsorption and desorption recovery were mutually performed by switching each valve, and continuous operation was performed.
【０００３】又、溶剤濃度の異なる各溶剤含有排ガス発
生源の吸着装置を各々別個に設けて、上記と同様な方法
で吸着、脱着回収処理する方法もあった。There has also been a method in which an adsorption device for an exhaust gas source containing each solvent having different solvent concentrations is provided separately, and adsorption, desorption and recovery processing is carried out in the same manner as described above.
【０００４】しかしながら、これらの方法では濃厚ガス
が希薄ガスと混合されるため濃厚ガスが希釈されること
によって吸着剤の吸着能力が減じあるいは吸着装置が増
えて設備費が多額になり、かつ単位溶剤処理当たりの再
生コストが高くついた。However, in these methods, since the rich gas is mixed with the lean gas, the rich gas is diluted, so that the adsorption capacity of the adsorbent is reduced or the adsorbing device is increased, resulting in a large equipment cost and a unit solvent. The cost of regeneration per treatment was high.
【０００５】これらの問題点を解決した溶剤回収処理方
法として、溶剤含有濃度の異なる少なくとも２種の溶剤
ガス含有気体を吸着する溶剤回収処理方法において、先
ず希薄なる溶剤ガス含有気体を第１の吸着装置に通し、
吸着剤が破過開始する前の一定時間後に該含有気体を第
２の吸着装置に切り替え送風し、第１の吸着装置には濃
厚なる溶剤ガス含有気体を通し、その濃厚なる溶剤ガス
の吸着を吸着剤が破過開始する時間内でかつ前記希薄な
る溶剤ガス吸着時間に合わせた時間行った後、第２の吸
着装置に切り替え送風し、同時に希薄なる溶剤ガス含有
気体は第３の吸着装置に切り替え送風し、第１の吸着装
置は再生操作に移ることを順次繰返し行う方法が開発さ
れている（特開平４−５９０１９号公報）。As a solvent recovery processing method that solves these problems, in a solvent recovery processing method of adsorbing at least two kinds of solvent gas-containing gases having different solvent-containing concentrations, first, a dilute solvent gas-containing gas is first adsorbed. Through the device,
After a certain period of time before the adsorbent starts to break through, the contained gas is switched to the second adsorption device and blown, and the concentrated solvent gas-containing gas is passed through the first adsorption device to adsorb the concentrated solvent gas. After the adsorbent has started to break through and the time corresponding to the lean solvent gas adsorption time, the air is switched to the second adsorber and air is blown, and at the same time, the lean solvent gas-containing gas is admitted to the third adsorber. A method has been developed in which switched air is blown and the first adsorbing device is sequentially regenerated, which is repeated (JP-A-4-59019).
【０００６】[0006]
【発明が解決しようとする課題】上記の方法を溶剤濃度
の異なる少なくとも３種類の溶剤含有排ガスに適用した
場合、低濃度ガスの吸着工程における溶剤ガスの破過が
予想外に早いため、大気放出から再吸着への切替を早期
に行なわなければならず、これが設備負担を増加させ、
溶剤回収コストを上昇させていた。When the above-mentioned method is applied to at least three kinds of solvent-containing exhaust gas having different solvent concentrations, the breakthrough of the solvent gas in the adsorption process of low-concentration gas is unexpectedly fast, so that it is released into the atmosphere. To switch to re-adsorption must be done early, which increases equipment burden and
Solvent recovery costs were rising.
【０００７】本発明の目的は、溶剤濃度の異なる少なく
とも３種類の溶剤含有排ガスから溶剤を吸着回収するに
あたり、吸着剤の吸着能力を充分に発揮させて溶剤を効
率よく回収するとともに吸着塔からの排ガスの溶剤濃度
を極めて低濃度に抑えることができる溶剤回収処理方法
を提供することにある。The object of the present invention is to adsorb and recover a solvent from at least three kinds of solvent-containing exhaust gas having different solvent concentrations, so that the adsorbing ability of the adsorbent can be sufficiently exhibited and the solvent can be efficiently recovered and the adsorbent from the adsorption tower. An object of the present invention is to provide a solvent recovery treatment method capable of suppressing the solvent concentration of exhaust gas to an extremely low concentration.
【０００８】[0008]
【課題を解決するための手段】上記目的は、溶剤濃度の
異なる少なくとも３種類の溶剤含有排ガスを少なくとも
４塔の吸着塔を有する吸着装置の各塔に順次導入して溶
剤の吸着回収を行ない、少なくとも１塔では脱着再生を
行なう方法であって、各塔には前記溶剤含有排ガスのう
ち中濃度排ガス、低濃度排ガス、高濃度排ガスの順に供
給し、低濃度排ガスを送入した塔の排ガスは放出あるい
は次の処理工程に移し、高濃度排ガスを送入した塔は次
いで脱着再生を行なうことを特徴とする溶剤回収処理方
法によって達成される。The above object is to introduce at least three kinds of solvent-containing exhaust gas having different solvent concentrations into each column of an adsorption device having at least four adsorption columns to adsorb and recover the solvent. A method of performing desorption regeneration in at least one tower, in which medium-concentration exhaust gas, low-concentration exhaust gas, and high-concentration exhaust gas of the solvent-containing exhaust gas are sequentially supplied to each tower, and the exhaust gas of the tower into which the low-concentration exhaust gas is fed is This is achieved by a solvent recovery treatment method characterized by carrying out desorption regeneration for the column into which the high-concentration exhaust gas has been introduced after being discharged or transferred to the next treatment step.
【０００９】すなわち、本発明では、脱着工程後の吸着
１段目で中濃度ガスの吸着を行い、また排気は再処理の
ため低濃度ガスと合わせ吸着回収し、２段目以降低濃度
ガスの吸着を行い、大気放出する。最終段で高濃度ガス
の吸着を行い、排気は再処理のため低濃度ガスと合わせ
吸着回収するのである。That is, in the present invention, the medium-concentration gas is adsorbed in the first stage of adsorption after the desorption process, and the exhaust gas is adsorbed and recovered together with the low-concentration gas for reprocessing, and the second-stage and subsequent stages of the low-concentration gas are collected. Adsorb and release to the atmosphere. The high-concentration gas is adsorbed in the final stage, and the exhaust gas is adsorbed and collected together with the low-concentration gas for reprocessing.
【００１０】[0010]
【発明の実施の形態】本発明の実施態様を図１を用いて
説明する。BEST MODE FOR CARRYING OUT THE INVENTION An embodiment of the present invention will be described with reference to FIG.
【００１１】図１において低濃度ガス発生源１と中濃度
ガス発生源２と高濃度ガス発生源３とがあり、それに対
して第１の吸着塔１０ａから第６の吸着塔１０ｆまでに
それぞれ通じる管路があり、バルブ１５で切り替えが出
来るようになっている。In FIG. 1, there are a low-concentration gas generation source 1, a medium-concentration gas generation source 2 and a high-concentration gas generation source 3, which are connected to the first adsorption tower 10a to the sixth adsorption tower 10f, respectively. There is a pipeline, and it can be switched by the valve 15.
【００１２】第１の吸着塔１０ａには中濃度ガス発生源
２よりの溶剤ガスが通された後、一定時間後、第２の吸
着装置１０ｂに切り換えられ、第１の吸着装置１０ａに
は低濃度ガス発生源１からの溶剤ガスが通され、一定時
間後排気ガス濃度が所定の濃度になる前に第２の吸着装
置１０ｂに切り換えられ、中濃度溶剤ガスは第３の吸着
装置１０ｃに切り換えられる。第１の吸着装置１０ａは
低濃度ガスの吸着により排気ガス濃度が一定値以上とな
ると切り換えられ高濃度ガス発生源３よりの溶剤ガスが
通される。前記の一定時間とは低濃度ガスの吸着による
排気ガス濃度が所定の濃度以下を保つ時間を基準として
定める。図１において、第１の吸着装置１０ａが再生状
態に入った状態を表すとして説明すると、中濃度ガス発
生源２よりの溶剤ガスは冷却器５によって冷却され、送
風機８によって第６の吸着装置１０ｆに通され、吸着剤
１１ｆにその溶剤ガスを吸着されている。吸着後の気体
中には溶剤ガスが含まれているので、再び低濃度ガスと
して吸着処理される。低濃度ガス発生源１からの溶剤ガ
スは冷却器４によって冷却され、送風機７によって第５
の吸着装置１０ｅ、第４の吸着装置１０ｄおよび第３の
吸着装置１０ｃに通され、吸着剤１１ｅ、１１ｄ、１１
ｃにその溶剤ガスを吸着されている。吸着後の気体には
所定の濃度以下の溶剤しか含まれていない。After the solvent gas from the medium-concentration gas generating source 2 is passed through the first adsorption tower 10a, after a certain time, the solvent is switched to the second adsorption device 10b, and the first adsorption device 10a has a low temperature. The solvent gas from the concentration gas generation source 1 is passed, and after a certain period of time, the exhaust gas concentration is switched to the second adsorption device 10b before reaching a predetermined concentration, and the medium concentration solvent gas is switched to the third adsorption device 10c. To be The first adsorption device 10a is switched when the exhaust gas concentration becomes a certain value or more due to the adsorption of the low concentration gas, and the solvent gas from the high concentration gas generation source 3 is passed through. The above-mentioned fixed time period is defined based on the time period during which the exhaust gas concentration due to the adsorption of the low-concentration gas remains below the predetermined concentration. In FIG. 1, description will be given assuming that the first adsorption device 10a has entered the regeneration state, and the solvent gas from the medium-concentration gas generation source 2 is cooled by the cooler 5 and the blower 8 causes the sixth adsorption device 10f. The solvent gas is adsorbed by the adsorbent 11f. Since the solvent gas is contained in the gas after the adsorption, the adsorption treatment is performed again as a low concentration gas. The solvent gas from the low-concentration gas generation source 1 is cooled by the cooler 4, and is blown by the blower 7 to the fifth
Of the adsorbents 11e, 11d, 11 which are passed through the adsorbing device 10e, the fourth adsorbing device 10d, and the third adsorbing device 10c.
The solvent gas is adsorbed by c. The gas after adsorption contains only a solvent having a predetermined concentration or less.
【００１３】高濃度ガス発生源３よりの溶剤ガスは冷却
器６によって冷却され、送風機９によって既に中濃度溶
剤ガス、低濃度溶剤ガスを吸着した第２の吸着装置１０
ｂに通され、吸着剤１１ｂにその溶剤ガスを吸着されて
いる。排気ガスに溶剤ガスが含まれる場合には中濃度ガ
スの吸着後の排気と同様に再び吸着処理される。The solvent gas from the high-concentration gas generation source 3 is cooled by the cooler 6, and the blower 9 has already adsorbed the medium-concentration solvent gas and the low-concentration solvent gas.
The solvent gas is adsorbed by the adsorbent 11b. When the exhaust gas contains a solvent gas, the adsorption treatment is performed again in the same manner as the exhaust after the adsorption of the medium concentration gas.
【００１４】第１の吸着装置１０ａは、中濃度溶剤ガ
ス、低濃度溶剤ガス、高濃度溶剤ガスの順に吸着したあ
と、再生中であり、加熱再生用気体１２が吹き込まれ吸
着剤１１ａに吸着された溶剤は加熱再生用気体に蒸発し
てコンデンサー１３によって冷却凝縮し、液体となって
回収され、溶剤貯蔵タンク１４に貯蔵される。The first adsorption device 10a is in the process of regenerating after adsorbing the medium concentration solvent gas, the low concentration solvent gas, and the high concentration solvent gas in this order, and the heating regeneration gas 12 is blown into the first adsorption device 10a to be adsorbed by the adsorbent 11a. The solvent is evaporated into a heating regeneration gas, cooled and condensed by the condenser 13, collected as a liquid, and stored in the solvent storage tank 14.
【００１５】吸着塔は少なくとも４塔あればよい。一
方、吸着あるいは脱着を２塔以上直列に連結して連塔方
式で行なうこともでき、その場合にはそれに必要な塔数
を増設する。At least four adsorption columns may be used. On the other hand, adsorption or desorption can be performed in a continuous tower system by connecting two or more towers in series, and in that case, the number of towers required for it is increased.
【００１６】溶剤は吸着剤で吸着回収できるものであれ
ばよく、例えば塩化メチレン、アセトン、メタノール、
ｎ−ブタノール等がある。Any solvent may be used as long as it can be adsorbed and recovered by an adsorbent, and examples thereof include methylene chloride, acetone, methanol,
There is n-butanol and the like.
【００１７】本発明が適用される溶剤含有排ガスの溶剤
濃度は本発明の効果を発揮しうるものであればよいが、
例えば、高濃度ガスは１，０００ｐｐｍ以上、中濃度ガ
スは５００ｐｐｍ以上１，０００ｐｐｍ未満、低濃度ガ
スは５００ｐｐｍ未満である。The solvent concentration of the solvent-containing exhaust gas to which the present invention is applied may be any as long as the effect of the present invention can be exhibited,
For example, the high concentration gas is 1,000 ppm or more, the medium concentration gas is 500 ppm or more and less than 1,000 ppm, and the low concentration gas is less than 500 ppm.
【００１８】溶剤含有排ガスが４種類ある場合には、ま
ず２番目又は３番目の濃度のガスを供給し、次に、低濃
度ガス、３番目又は２番目の濃度のガス、高濃度ガスの
順に供給すればよい。When there are four kinds of solvent-containing exhaust gas, first the gas of the second or third concentration is supplied, and then the low concentration gas, the gas of the third or second concentration, and the high concentration gas in this order. Just supply it.
【００１９】吸着剤は、ゼオライト、粒状活性炭、繊維
活性炭等を使用できる。吸着は常圧、加圧のいずれで行
なってもよい。As the adsorbent, zeolite, granular activated carbon, fiber activated carbon or the like can be used. The adsorption may be carried out either under normal pressure or under pressure.
【００２０】脱着は水蒸気の他、加熱窒素、加熱空気等
を用いてもよい。For desorption, heated nitrogen, heated air or the like may be used in addition to water vapor.
【００２１】濃度の異なる少なくとも３種類の溶剤ガス
（高濃度，中濃度，低濃度）を吸着回収するに対し、吸
着剤の吸着能力を十分活用し、且つ吸着塔からの大気排
気濃度を極低濃度（５ｐｐｍ以下）に押さえると共に、
設備費、再生コストを低減させるため、本発明では、脱
着工程後の吸着１段目で中濃度ガスの吸着を行い、また
排気は再処理のため低濃度ガスと合わせ吸着回収し、２
段目以降低濃度ガスの吸着を行い、大気放出する。最終
段で高濃度ガスの吸着を行い、排気は再処理のため低濃
度ガスと合わせ吸着回収することを特徴とする。従来技
術では吸着１段目から低濃度ガスの吸着を行い、順次高
濃度側の吸着を行っていた。At least three kinds of solvent gas having different concentrations (high concentration, medium concentration and low concentration) are adsorbed and recovered, while the adsorbing ability of the adsorbent is fully utilized and the atmospheric exhaust concentration from the adsorption tower is extremely low. While keeping the concentration (5 ppm or less),
In order to reduce equipment cost and regeneration cost, in the present invention, medium concentration gas is adsorbed in the first stage of adsorption after the desorption process, and exhaust gas is adsorbed and collected with low concentration gas for reprocessing.
After the second stage, low concentration gas is adsorbed and released into the atmosphere. The high-concentration gas is adsorbed in the final stage, and the exhaust gas is adsorbed and collected together with the low-concentration gas for reprocessing. In the prior art, low-concentration gas was adsorbed from the first stage of adsorption, and the high-concentration side was sequentially adsorbed.
【００２２】この従来技術では、通常脱着直後の吸着１
段目の排気は水蒸気を多量に含み、また溶剤分を若干含
んでおり白煙状で大気に放出するが、本発明では吸着１
段目の排気を再処理のため低濃度ガスと合わせ吸着再処
理するため、環境への水蒸気、溶剤分の放出を極力低減
できる。In this conventional technique, adsorption 1 usually immediately after desorption
The exhaust gas in the second stage contains a large amount of water vapor and a small amount of solvent, and is emitted as white smoke into the atmosphere.
Since the exhaust gas in the first stage is adsorbed and reprocessed together with a low-concentration gas for reprocessing, the release of water vapor and solvent to the environment can be reduced as much as possible.
【００２３】また、従来の知見ではサイクルタイムを延
長すると低濃度ガスの吸着工程で破過が始まり、大気放
出ガス濃度を目標値以下に維持できなかったが、本発明
の方法によれば、吸着１段目の中濃度ガスによる吸着剤
を乾燥する効果が大きくなることにより、２段目以降の
吸着能力が向上しサイクルタイムを延長しても、大気放
出ガス濃度を目標値以下に維持することができた。この
ため脱着のための水蒸気量を約２／３に削減でき、省エ
ネ効果を出すことができた。Further, according to the conventional knowledge, when the cycle time was extended, breakthrough started in the adsorption process of the low concentration gas and the concentration of the gas released into the atmosphere could not be maintained below the target value, but according to the method of the present invention, Maintaining the atmospheric emission gas concentration below the target value even if the adsorption capacity of the second and subsequent stages is improved due to the greater effect of drying the adsorbent with the medium concentration gas of the first stage and the cycle time is extended. I was able to. Therefore, the amount of water vapor for desorption can be reduced to about 2/3, and the energy saving effect can be achieved.
【００２４】[0024]
【実施例】図１に示す装置を用いた。この装置は、１塔
当たり４ｍ3／ｍｉｎの風量処理能力のある吸着塔６塔
よりなっている。吸着剤には繊維活性炭を用い、１塔当
り５.２ｋｇを充填した。まず、中濃度溶剤含有ガス(塩
化メチレン５５０ｐｐｍ）３ｍ3／ｍｉｎを１段目の吸
着塔で処理し、大気放出ガス濃度を極低濃度(塩化メチ
レン５ｐｐｍ以下）とするため、排気(塩化メチレン２
０ｐｐｍ)は再処理のため低濃度ガス(塩化メチレン３０
０ｐｐｍ，８ｍ3／ｍｉｎ）及び後述の高濃度ガスを最
終段で吸着処理した後の排気(塩化メチレン３０ｐｐ
ｍ，１ｍ3／ｍｉｎ）を合わせ、２段目から４段目で処
理をし大気放出したところ、塩化メチレン濃度を５ｐｐ
ｍ以下とすることができた。高濃度ガス(塩化メチレン
１０,０００ｐｐｍ，１ｍ3／ｍｉｎ）を最終段(５段
目）で吸着処理し、その排ガスは低濃度ガスと合わせ吸
着処理を行い、大気放出した。EXAMPLES The apparatus shown in FIG. 1 was used. This device is composed of 6 adsorption towers having an air flow capacity of 4 m 3 / min per tower. Fiber adsorbent was used as the adsorbent, and 5.2 kg was packed per tower. First, the medium concentration solvent-containing gas (methylene chloride 550 ppm) 3 m 3 / min is treated in the first stage adsorption tower to make the concentration of the gas released into the atmosphere extremely low (methylene chloride 5 ppm or less).
0ppm) is a low concentration gas (methylene chloride 30
0ppm, 8m 3 / min) and exhaust gas after adsorbing high concentration gas described below at the final stage (methylene chloride 30pp
m, 1 m 3 / min) and processed in the 2nd to 4th steps and released into the atmosphere, the methylene chloride concentration was 5pp
It could be set to m or less. A high-concentration gas (methylene chloride 10,000 ppm, 1 m 3 / min) was adsorbed at the final stage (fifth stage), and the exhaust gas was adsorbed together with the low-concentration gas and released into the atmosphere.
【００２５】脱着に要したスチーム量は１２ｋｇ／Ｈｒ
であった。The amount of steam required for desorption is 12 kg / Hr
Met.
【００２６】この実施例では１塔処理風量が中濃度ガス
風量３ｍ3／ｍｉｎと高濃度ガス風量１ｍ3／ｍｉｎとの
合計風量４ｍ3／ｍｉｎとしたため再処理用の低濃度吸
着塔は１塔で間に合い、設備構成上のメリットがあっ
た。The low concentration adsorption tower 1 tower for reprocessing due to the total air volume 4m 3 / min with one column process air volume medium concentration gas air volume 3m 3 / min and the high concentration gas air volume 1 m 3 / min in this embodiment It was in time and there was a merit in the equipment structure.
【００２７】従来の方法では、低濃度ガス（塩化メチレ
ン３００ｐｐｍ，８ｍ3／ｍｉｎ）のうちの４ｍ3／ｍｉ
ｎを１段目で処理をすると大気放出の排気濃度が５ｐｐ
ｍ以上となり目的を達成できなかった。また大気放出の
排気濃度を５ｐｐｍ以下とするためには、吸着塔を１基
増設する必要があり設備費の低減化に反する結果となっ
た。According to the conventional method, 4 m 3 / mi of a low concentration gas (methylene chloride 300 ppm, 8 m 3 / min) is used.
When n is treated in the first stage, the exhaust emission concentration in the atmosphere is 5pp
It was over m and could not achieve the purpose. Further, in order to reduce the exhaust emission concentration into the atmosphere to 5 ppm or less, it is necessary to add one adsorption tower, which is contrary to the reduction of equipment cost.
【００２８】[0028]
【発明の効果】濃度の異なる少なくとも３種類の溶剤ガ
ス（高濃度，中濃度，低濃度）を吸着回収するに対し、
吸着剤の吸着能力を十分活用し、且つ吸着塔からの大気
排気濃度を極低濃度（５ｐｐｍ以下）に押さえると共
に、設備費、再生コストを低減させることができる。[Advantages of the Invention] At least three kinds of solvent gas having different concentrations (high concentration, medium concentration, low concentration) are adsorbed and recovered,
It is possible to fully utilize the adsorption capacity of the adsorbent, suppress the atmospheric exhaust gas concentration from the adsorption tower to an extremely low concentration (5 ppm or less), and reduce the equipment cost and the regeneration cost.
【図１】 本発明の溶剤回収処理方法で使用される吸着
装置の一例のフローシートである。FIG. 1 is a flow sheet of an example of an adsorption device used in the solvent recovery treatment method of the present invention.
１ 低濃度ガス発生源 ２ 中濃度ガス発生源 ３ 高濃度ガス発生源 ４，５，６ 冷却器 ７，８，９ 送風機 １０ａ〜ｆ 吸着装置 １１ａ〜ｆ 吸着剤 １２ 加熱再生用気体 １３ コンデンサー １４ 溶剤貯蔵タンク １５ バルブ 1 Low-concentration gas generation source 2 Medium-concentration gas generation source 3 High-concentration gas generation source 4,5,6 Cooler 7,8,9 Blower 10a-f Adsorption device 11a-f Adsorbent 12 Heating regeneration gas 13 Condenser 14 Solvent Storage tank 15 valves
Claims (2)
剤含有排ガスを少なくとも４塔の吸着塔を有する吸着装
置の各塔に順次導入して溶剤の吸着回収を行ない、少な
くとも１塔では脱着再生を行なう方法であって、各塔に
は前記溶剤含有排ガスのうち中濃度排ガス、低濃度排ガ
ス、高濃度排ガスの順に供給し、低濃度排ガスを送入し
た塔の排ガスは放出あるいは次の処理工程に移し、高濃
度排ガスを送入した塔は次いで脱着再生を行なうことを
特徴とする溶剤回収処理方法1. At least three kinds of solvent-containing exhaust gas having different solvent concentrations are sequentially introduced into each column of an adsorption device having at least four adsorption columns to adsorb and recover the solvent, and at least one column carries out desorption regeneration. In the method, medium-concentration exhaust gas, low-concentration exhaust gas, high-concentration exhaust gas among the solvent-containing exhaust gas is sequentially supplied to each tower, and the exhaust gas of the tower into which the low-concentration exhaust gas is fed is discharged or transferred to the next treatment step. The method of recovering solvent is characterized in that the tower into which the high-concentration exhaust gas is fed is then subjected to desorption regeneration.
度ガスの塩化メチレン濃度は１,０００ｐｐｍ以上、中
濃度ガスの塩化メチレン濃度は５００以上１,０００ｐ
ｐｍ未満、低濃度ガスの塩化メチレン濃度は５００ｐｐ
ｍ未満であることを特徴とする請求項１記載の溶剤回収
処理方法2. The solvent is methylene chloride, the high-concentration gas has a methylene chloride concentration of 1,000 ppm or more, and the medium-concentration gas has a methylene chloride concentration of 500 or more and 1,000 p.
Less than pm, methylene chloride concentration of low concentration gas is 500pp
It is less than m, The solvent recovery processing method of Claim 1 characterized by the above-mentioned.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP19844695A JP3788814B2 (en) | 1995-08-03 | 1995-08-03 | Solvent recovery method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP19844695A JP3788814B2 (en) | 1995-08-03 | 1995-08-03 | Solvent recovery method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0938451A true JPH0938451A (en) | 1997-02-10 |
| JP3788814B2 JP3788814B2 (en) | 2006-06-21 |
Family
ID=16391235
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP19844695A Expired - Fee Related JP3788814B2 (en) | 1995-08-03 | 1995-08-03 | Solvent recovery method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3788814B2 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPWO2020158442A1 (en) * | 2019-01-31 | 2020-08-06 | ||
| CN115430253A (en) * | 2022-10-24 | 2022-12-06 | 南京威盾能源环保有限公司 | Chlorine-containing medium volatile gas recovery processing device |
| CN116036787A (en) * | 2022-12-28 | 2023-05-02 | 北京泷涛环境科技有限公司 | A device and method for graded and advanced treatment of textile-coated organic waste gas |
| CN116585838A (en) * | 2023-06-26 | 2023-08-15 | 艾易西(中国)环保科技有限公司 | VOCs waste gas treatment method |
-
1995
- 1995-08-03 JP JP19844695A patent/JP3788814B2/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPWO2020158442A1 (en) * | 2019-01-31 | 2020-08-06 | ||
| WO2020158442A1 (en) * | 2019-01-31 | 2020-08-06 | 東洋紡株式会社 | Organic solvent recovery system |
| CN113365718A (en) * | 2019-01-31 | 2021-09-07 | 东洋纺株式会社 | Organic solvent recovery system |
| CN113365718B (en) * | 2019-01-31 | 2023-07-25 | 东洋纺株式会社 | Organic solvent recovery system |
| CN115430253A (en) * | 2022-10-24 | 2022-12-06 | 南京威盾能源环保有限公司 | Chlorine-containing medium volatile gas recovery processing device |
| CN116036787A (en) * | 2022-12-28 | 2023-05-02 | 北京泷涛环境科技有限公司 | A device and method for graded and advanced treatment of textile-coated organic waste gas |
| CN116585838A (en) * | 2023-06-26 | 2023-08-15 | 艾易西(中国)环保科技有限公司 | VOCs waste gas treatment method |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3788814B2 (en) | 2006-06-21 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US20050109207A1 (en) | Method and apparatus for the recovery of volatile organic compounds and concentration thereof | |
| US5908490A (en) | Organic solvent recovering system and organic solvent recovering method | |
| EP0416127B1 (en) | Process for efficiently recovering adsorbable gas from gas which contains adsorbable gas at low concentration | |
| JP6318580B2 (en) | Organic solvent recovery system | |
| JP2009226257A (en) | Process for separation of blast furnace gas, and system of separating blast furnace gas | |
| JP2007105657A (en) | Gas processing equipment | |
| US4018704A (en) | Method for desorption of methyl bromide | |
| JP3788814B2 (en) | Solvent recovery method | |
| US20250304445A1 (en) | Waste gas treatment device, waste gas treatment method, and waste gas adsorption and recovery system including the same | |
| JP4548891B2 (en) | Organic solvent recovery method | |
| JPH06226029A (en) | Method for recovering solvent | |
| JPH0634897B2 (en) | Adsorption and desorption method with activated carbon | |
| JP5879881B2 (en) | Organic solvent recovery system | |
| JPH1157372A (en) | Method of recovering hydrocarbon vapor using cooling condensation | |
| WO2023145721A1 (en) | Co2 recovery method and co2 recovery device | |
| JP2004121921A (en) | Organic solvent recovery system | |
| JPH07284623A (en) | Method for treating and recovering concentrated gaseous hydrocarbon contained in discharged gas | |
| JPS59116115A (en) | Method for recovering carbon monoxide | |
| JP2572294B2 (en) | Solvent recovery processing method | |
| JPH06254395A (en) | Method for regenerating adsorbent in pressure swing adsorption for recovering co2 | |
| JPH06312117A (en) | Solvent recovery | |
| JP3080687B2 (en) | How to concentrate chlorine gas | |
| JPS62117612A (en) | Regenerating method for adsorption tower | |
| JPH04118024A (en) | Solvent recovering device | |
| RU2786205C1 (en) | Adsorbent regeneration method in natural gas processing |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A977 | Report on retrieval |
Free format text: JAPANESE INTERMEDIATE CODE: A971007 Effective date: 20040213 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20040316 |
|
| A521 | Written amendment |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20040510 |
|
| TRDD | Decision of grant or rejection written | ||
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 Effective date: 20060306 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20060324 |
|
| R150 | Certificate of patent (=grant) or registration of utility model |
Free format text: JAPANESE INTERMEDIATE CODE: R150 |
|
| FPAY | Renewal fee payment (prs date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20090407 Year of fee payment: 3 |
|
| S111 | Request for change of ownership or part of ownership |
Free format text: JAPANESE INTERMEDIATE CODE: R313111 |
|
| FPAY | Renewal fee payment (prs date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20090407 Year of fee payment: 3 |
|
| R350 | Written notification of registration of transfer |
Free format text: JAPANESE INTERMEDIATE CODE: R350 |
|
| FPAY | Renewal fee payment (prs date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20090407 Year of fee payment: 3 |
|
| FPAY | Renewal fee payment (prs date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20100407 Year of fee payment: 4 |
|
| FPAY | Renewal fee payment (prs date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20110407 Year of fee payment: 5 |
|
| FPAY | Renewal fee payment (prs date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20120407 Year of fee payment: 6 |
|
| FPAY | Renewal fee payment (prs date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20130407 Year of fee payment: 7 |
|
| FPAY | Renewal fee payment (prs date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20130407 Year of fee payment: 7 |
|
| FPAY | Renewal fee payment (prs date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20140407 Year of fee payment: 8 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| LAPS | Cancellation because of no payment of annual fees |