JP2010149040A - Organic solvent-containing gas treating system - Google Patents

Organic solvent-containing gas treating system Download PDF

Info

Publication number
JP2010149040A
JP2010149040A JP2008329582A JP2008329582A JP2010149040A JP 2010149040 A JP2010149040 A JP 2010149040A JP 2008329582 A JP2008329582 A JP 2008329582A JP 2008329582 A JP2008329582 A JP 2008329582A JP 2010149040 A JP2010149040 A JP 2010149040A
Authority
JP
Japan
Prior art keywords
organic solvent
water
solvent
adsorption
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.)
Pending
Application number
JP2008329582A
Other languages
Japanese (ja)
Inventor
Akinari Kimura
彰成 木村
Original Assignee
Toyobo Co Ltd
東洋紡績株式会社
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Toyobo Co Ltd, 東洋紡績株式会社 filed Critical Toyobo Co Ltd
Priority to JP2008329582A priority Critical patent/JP2010149040A/en
Publication of JP2010149040A publication Critical patent/JP2010149040A/en
Pending legal-status Critical Current

Links

Images

Abstract

<P>PROBLEM TO BE SOLVED: To provide an organic solvent-containing gas treating system having an apparatus capable of stably removing acid component and moisture out of a large amount of collected organic solvents and capable of effectively utilizing drainage separated and discharged from the apparatus without discharging it to the environment such as rivers. <P>SOLUTION: The organic solvent-containing gas treating system includes: an organic solvent collecting system that introduces treated gas into an organic solvent collecting/treating apparatus 10 having an absorption tank 13 filled with absorbent materials 14, after performing absorption treatment on the organic solvents and discharging the treated gas where the organic solvent concentration is decreased to complete the absorption treatment, introduces steam into the absorption tank of the organic solvent collecting/separating apparatus and desorbs the organic solvent from the absorbent materials, and introduces the steam containing the organic solvent generated into a solvent separating apparatus 20 that condenses and separates the steam containing the organic solvent; and an acid component removing solvent-refining apparatus 23 that introduces the collected organic solvent separated by the organic solvent collecting/treating apparatus into a solvent refining apparatus 40 having an absorption tank filled with an acid component removing agent, and discharges the treated organic solvent where the concentration of the acid component in the organic solvent is decreased. <P>COPYRIGHT: (C)2010,JPO&INPIT

Description

本発明は、有機溶剤を含有する被処理ガスから有機溶剤を回収し、その回収溶剤を精製し、分離排水を処理する有機溶剤含有ガス処理システムに関し、特に各種工場、研究施設等から排出される有機溶剤を含有した産業排ガスの浄化に用いられる有機溶剤含有ガス処理システムに関するものである。   The present invention relates to an organic solvent-containing gas treatment system that recovers an organic solvent from a gas to be treated containing an organic solvent, purifies the recovered solvent, and treats separated wastewater, and is particularly discharged from various factories and research facilities. The present invention relates to an organic solvent-containing gas treatment system used for purification of industrial exhaust gas containing an organic solvent.

従来、有機溶剤含有ガス処理システムにおける有機溶剤回収装置としては、活性炭素材で被処理ガスの有機溶剤を吸着する吸着槽と、各吸着槽に対する被処理ガス供給手段と脱着用ガス供給手段とを設け、前記吸着槽に被処理ガスを供給する吸着処理装置と脱着用ガスを供給する脱着処理状態とに切り替える切り替え手段を設けて構成されている。また、上記の有機溶剤回収装置の吸着材は、粒状活性炭や活性炭素繊維、ゼオライト、シリカゲル、活性アルミナなどが使用されている。特に活性炭素繊維は低濃度の有機ガスを吸着する機能に優れ、古くから吸着材として使われている。   Conventionally, as an organic solvent recovery device in an organic solvent-containing gas processing system, an adsorption tank for adsorbing an organic solvent of a gas to be processed with activated carbon material, a gas supply means to be processed and a desorption gas supply means for each adsorption tank are provided. A switching means for switching between an adsorption processing apparatus for supplying a gas to be processed to the adsorption tank and a desorption processing state for supplying a desorption gas is provided. Moreover, granular activated carbon, activated carbon fiber, zeolite, silica gel, activated alumina or the like is used as the adsorbent for the organic solvent recovery apparatus. In particular, activated carbon fiber has an excellent function of adsorbing low-concentration organic gas, and has been used as an adsorbent for a long time.

たとえば、活性炭素繊維を支持体に固定し、または自己支持にて円筒状に構成し、芯材内にたて型に配設した装置が特許文献1や2に提案されている。また、特許文献3〜5にも同様な吸脱着装置が提案されている。これらは、いずれも、活性炭素繊維を格納している芯材に蒸気を噴出し、活性炭素繊維に吸着された有機物を脱着させるものである。該脱着された有機溶剤含有水蒸気を有機溶剤分離装置に導入し、凝縮して有機溶剤と水を分離して有機溶剤を回収する有機溶剤回収装置から構成されている。   For example, Patent Documents 1 and 2 propose an apparatus in which activated carbon fibers are fixed to a support or are formed in a cylindrical shape by self-supporting and arranged in a vertical mold in a core material. Also, Patent Documents 3 to 5 propose similar adsorption / desorption devices. In any of these, steam is jetted onto a core material storing activated carbon fibers to desorb organic substances adsorbed on the activated carbon fibers. The desorbed organic solvent-containing water vapor is introduced into an organic solvent separator, and is condensed to separate the organic solvent and water to recover the organic solvent.

前記有機溶剤分離装置で分離された回収有機溶剤は、水分や酸成分が混入している場合が多く、そのまま工業利用できないケースがあることから、有機溶剤精製装置を設けて処理を行うか、あるいは精留メーカーに蒸留を委託している場合がある。有機溶剤精製装置として、有機溶剤を加熱蒸発させ、沸点の違いを利用して有機溶剤と不純物を分留することで、純度の高い有機溶剤を取得することができる蒸留精製装置が広く普及している(例えば、特許文献6または7参照)が、蒸留精製装置は大型な装置であるために広い設置スペースが必要であり、且つイニシャルコスト、ランニングコスト共に高いことが問題となっている。   The recovered organic solvent separated by the organic solvent separator is often mixed with moisture and acid components, and may not be industrially used as it is. In some cases, distillation is entrusted to a rectification manufacturer. As an organic solvent refining device, a distillation refining device that can obtain a high-purity organic solvent by heating and evaporating the organic solvent and fractionating the organic solvent and impurities using the difference in boiling point is widely used. However, since the distillation purification apparatus is a large apparatus, a large installation space is required, and both the initial cost and running cost are high.

かかる問題を解決するために、活性炭、ゼオライト、イオン交換樹脂、モレキュラーシーブス、活性アルミナ等の吸着剤を充填させた吸着塔に有機溶剤を通液させて不純物を取り除く方法が知られている(例えば、特許文献8または9参照)が、多量の有機溶剤を精製する場合は多量の吸着剤が必要であり、吸着剤が破過状態になると吸着剤の交換が必要であることから、吸着剤が高価であるほどランニングコストが高くなるため、研究室レベルでは有効な手段であるが、工場や研究施設等から回収される多量の有機溶剤の精製を行うには満足できるものではなかった。   In order to solve such a problem, a method is known in which impurities are removed by passing an organic solvent through an adsorption tower packed with an adsorbent such as activated carbon, zeolite, ion exchange resin, molecular sieves, and activated alumina (for example, However, when refining a large amount of organic solvent, a large amount of adsorbent is required, and when the adsorbent is in a breakthrough state, the adsorbent must be replaced. The higher the cost, the higher the running cost. Therefore, it is an effective means at the laboratory level, but it is not satisfactory for purifying a large amount of organic solvent recovered from factories or research facilities.

また、前記有機溶剤分離装置で分離された排水は有機溶剤が含有しているため、そのまま河川等へ放流することができないことから、排水処理装置を設けて処理を行っている。排水処理装置として排水中の有機溶剤を揮発させて除去する曝気槽など有効な手法が開発されている(例えば、特許文献10参照)が、最終的には排水を河川等に放流する必要があった。   Moreover, since the wastewater separated by the organic solvent separation device contains an organic solvent, it cannot be discharged as it is to a river or the like, and therefore, a wastewater treatment device is provided for treatment. An effective method such as an aeration tank that volatilizes and removes the organic solvent in the wastewater has been developed as a wastewater treatment device (see, for example, Patent Document 10). However, it is necessary to finally discharge the wastewater to a river or the like. It was.

特開昭51−38278号公報Japanese Patent Laid-Open No. 51-38278 特公昭64−11326号公報Japanese Examined Patent Publication No. 64-11326 実公平7−2028号公報No. 7-2028 実公平7−2029号公報No. 7-2029 実公平7−2030号公報No. 7-2030 特開2001−300206号公報JP 2001-300206 A 特許第3832868号公報Japanese Patent No. 3832868 特開2000−225316号公報JP 2000-225316 A 特開平5−220303号公報JP-A-5-220303 特開平2−169085号公報JP-A-2-169085

本発明は、従来技術の課題を背景になされたもので、有機溶剤回収装置から分離された酸成分、水分等を含有している回収有機溶剤の連続精製を実現し、多量の回収有機溶剤中から酸成分、水分を安定に除去することができる装置を備え、
有機溶剤回収装置から分離排出される排水を河川等環境中に排出せずに有効利用することができる有機溶剤含有ガス処理システムを提供することを課題とするものである。 An object of the present invention is to provide an organic solvent-containing gas treatment system capable of effectively utilizing wastewater separated and discharged from an organic solvent recovery device without discharging it into an environment such as a river. The present invention has been made against the background of the problems of the prior art, and realizes continuous purification of a recovered organic solvent containing an acid component, moisture, etc. separated from an organic solvent recovery device, and a large amount of recovered organic solvent Equipped with a device that can stably remove acid components and moisture from The present invention has been made against the background of the problems of the prior art, and realizes continuous purification of a recovered organic solvent containing an acid component, moisture, etc. separated from an organic solvent recovery device, and a large amount of recovered organic solvent Equipped with a device that can stably remove acid components and moisture from
An object of the present invention is to provide an organic solvent-containing gas treatment system that can effectively use waste water separated and discharged from an organic solvent recovery device without discharging it into an environment such as a river. An object of the present invention is to provide an organic solvent-containing gas treatment system that can effectively use waste water separated and discharged from an organic solvent recovery device without efficiently it into an environment such as a river.

本発明は、従来技術の課題を解決するため、鋭意検討した結果、ついに本発明を完成するに至った。即ち本発明は以下の通りである。
1.吸着材を充填した吸着槽を備えた有機溶剤回収処理装置に、有機溶剤を含有する被処理ガスを導入し、有機溶剤を該吸着槽で吸着処理して有機溶剤濃度が減少した処理済みガスを排出し、該吸着槽における吸着処理が完了した後に、前記有機溶剤回収処理装置の吸着槽へスチームを導入し、吸着材から有機溶剤を脱着し、それによって吸着材を再生し、再生の際に発生する有機溶剤含有水蒸気を凝縮、分離する溶剤分離装置に導入し、有機溶剤を分離して回収する有機溶剤回収システムと、
酸成分除去剤を充填させた吸着槽を有する酸成分除去用溶剤精製装置に、該有機溶剤回収処理装置によって分離した回収有機溶剤を導入し、該回収有機溶剤を該酸成分除去用溶剤精製装置で吸着処理して有機溶剤中の酸成分の濃度が減少した処理済み有機溶剤を排出する酸成分除去用溶剤精製装置を備えた有機溶剤含有ガス処理システム。 A recovered organic solvent separated by the organic solvent recovery treatment device is introduced into an acid component removing solvent purification device having an adsorption tank filled with an acid component removing agent, and the recovered organic solvent is used as the acid component removing solvent purification device. An organic solvent-containing gas treatment system equipped with a solvent purification device for removing acid components that discharges a treated organic solvent whose concentration of acid components in the organic solvent has been reduced by adsorption treatment. In order to solve the problems of the prior art, the present invention has finally been completed as a result of intensive studies. That is, the present invention is as follows. In order to solve the problems of the prior art, the present invention has finally been completed as a result of intensive studies. That is, the present invention is as follows.
1. A gas to be treated containing an organic solvent is introduced into an organic solvent recovery treatment apparatus equipped with an adsorption tank filled with an adsorbent, and the treated gas having a reduced organic solvent concentration is obtained by adsorbing the organic solvent in the adsorption tank. After the discharge and the adsorption treatment in the adsorption tank are completed, steam is introduced into the adsorption tank of the organic solvent recovery treatment device, the organic solvent is desorbed from the adsorbent, thereby regenerating the adsorbent, and at the time of regeneration An organic solvent recovery system for separating and recovering the organic solvent by introducing it into a solvent separator for condensing and separating the generated organic solvent-containing water vapor; 1. A gas to be treated containing an organic solvent is introduced into an organic solvent recovery treatment apparatus equipped with an adsorption tank filled with an adsorbent, and the treated gas having a reduced organic solvent concentration is obtained by adsorbing the organic solvent in the adsorption after the discharge and the adsorption treatment in the adsorption tank are completed, steam is introduced into the adsorption tank of the organic solvent recovery treatment device, the organic solvent is desorbed from the adsorbent, thereby regenerating the adsorbent, and at the time of regeneration An organic solvent recovery system for separating and recovering the organic solvent by introducing it into a solvent separator for condensing and separating the generated organic solvent-containing water vapor;
The recovered organic solvent separated by the organic solvent recovery treatment device is introduced into an acid component removal solvent purification device having an adsorption tank filled with an acid component removal agent, and the recovered organic solvent is removed from the acid component removal solvent purification device. An organic solvent-containing gas treatment system equipped with an acid component removal solvent refining device that discharges the treated organic solvent in which the concentration of the acid component in the organic solvent has been reduced by adsorption treatment with an acid. The recovered organic solvent separated by the organic solvent recovery treatment device is introduced into an acid component removal solvent purification device having an adsorption tank filled with an acid component removal agent, and the recovered organic solvent is removed from the acid component removal solvent purification device. An organic solvent-containing gas treatment system equipped with an acid component removal solvent refining device that discharges the treated organic solvent in which the concentration of the acid component in the organic solvent has been reduced by adsorption treatment with an acid.

2.酸成分除去用溶剤精製装置において、酸成分除去剤が塩化マグネシウム、塩化カリウム、塩化カルシウム、塩化バリウム、炭酸マグネシウム、炭酸カリウム、炭酸カルシウム、炭酸バリウム等の内で1種類、または2種類以上を組み合わせたもので構成されている前記1に記載の有機溶剤含有ガス処理システム。 2. In the solvent refining equipment for acid component removal, the acid component remover is one of magnesium chloride, potassium chloride, calcium chloride, barium chloride, magnesium carbonate, potassium carbonate, calcium carbonate, barium carbonate, or a combination of two or more. 2. The organic solvent-containing gas treatment system as described in 1 above, wherein

3.有機溶剤回収システムと、
該有機溶剤回収システムで回収した回収有機溶剤から酸成分を除去する酸成分除去用溶剤精製装置と、
該酸成分除去用溶剤精製装置で酸成分を除去した回収有機溶剤から水分を除去する水分除去用溶剤精製装置を備えた上記1または2に記載の有機溶剤含有ガス処理システム。
3. An organic solvent recovery system;
A solvent refining device for removing an acid component from the recovered organic solvent recovered by the organic solvent recovery system;
3. The organic solvent-containing gas treatment system according to the above 1 or 2, comprising a water removal solvent purification device for removing water from the recovered organic solvent from which the acid component has been removed by the acid component removal solvent purification device.

4.水分除去用溶剤精製装置が、水分を含有する有機溶剤を吸着材に通流させて該吸着材に水分を吸着させる吸着工程と、該吸着材に乾燥空気を通流させて該吸着材に吸着された水分を脱着する脱着工程の間に、水の通流により吸着材に付着した有機溶剤を除去するパージ工程を有する水分除去用溶剤精製装置である上記3に記載の有機溶剤含有ガス処理システム。 4). A solvent purifier for removing moisture passes an adsorption process in which an organic solvent containing moisture is passed through the adsorbent to adsorb moisture onto the adsorbent, and adsorbs the adsorbent by passing dry air through the adsorbent. 4. The organic solvent-containing gas treatment system according to 3 above, wherein the organic solvent-containing gas treatment system has a purging step for removing the organic solvent adhering to the adsorbent by flowing water during the desorption step of desorbing the generated water. .

5.水分除去用溶剤精製装置において、パージ工程で排出された有機溶剤含有パージ水を曝気槽の入口に導入するラインを備える上記3または4に記載の有機溶剤含有ガス処理システム。 5. 5. The organic solvent-containing gas treatment system according to 3 or 4 above, comprising a line for introducing the organic solvent-containing purge water discharged in the purge step into the inlet of the aeration tank in the solvent purification apparatus for removing water.

6.有機溶剤を分離・回収する有機溶剤回収システムにおける溶剤分離装置により分離し排出される排水をクーリングタワーに導入し、クーリングタワーから該溶剤分離装置におけるコンデンサーに冷却水を導入し、使用した冷却水をクーリングタワーに戻すラインを備える上記1〜5のいずれかに記載の有機溶剤含有ガス処理システム。 6). Wastewater separated and discharged by the solvent separator in the organic solvent recovery system that separates and recovers the organic solvent is introduced into the cooling tower, cooling water is introduced from the cooling tower to the condenser in the solvent separator, and the used cooling water is supplied to the cooling tower. The organic solvent containing gas processing system in any one of said 1-5 provided with the line to return.

7.有機溶剤を分離・回収する有機溶剤回収システムにおける溶剤分離装置から排出された排水中の有機溶剤成分を除去する水処理手段として、排水中の有機溶剤を揮発除去する曝気槽および/または排水中の有機溶剤を含有する水を吸着素子に通流させて該吸着素子に有機溶剤を吸着させる吸着工程と、該吸着素子に高温の加熱ガスを通気させて該吸着素子に吸着された有機溶剤を脱着する脱着工程とを交互に行う吸脱着式水処理装置を、有機溶剤を分離・回収する有機溶剤回収システムにおける該溶剤分離装置から排出された排水をクーリングタワーに導入する前に備える上記6に記載の有機溶剤含有ガス処理システム。 7). As a water treatment means to remove the organic solvent components in the wastewater discharged from the solvent separator in the organic solvent recovery system that separates and recovers the organic solvent, an aeration tank that volatilizes and removes the organic solvent in the wastewater and / or An adsorption process in which water containing an organic solvent is passed through the adsorption element to adsorb the organic solvent in the adsorption element, and a high-temperature heated gas is passed through the adsorption element to desorb the organic solvent adsorbed on the adsorption element. 6. The adsorption / desorption type water treatment apparatus that alternately performs the desorption step to be performed is provided before the waste water discharged from the solvent separation apparatus in the organic solvent recovery system for separating and recovering the organic solvent is introduced into the cooling tower. Organic solvent-containing gas treatment system.

8.水処理手段が、前段が曝気槽、後段が吸脱着式水処理装置であり、水処理手段により排水中から除去した有機溶剤ガスを、有機溶剤回収装置の入口に戻すラインを備える上記7に記載の有機溶剤含有ガス処理システム。 8). 8. The water treatment means according to 7 above, wherein the first stage is an aeration tank and the second stage is an adsorption / desorption type water treatment apparatus, and includes a line for returning the organic solvent gas removed from the waste water by the water treatment means to the inlet of the organic solvent recovery apparatus. Organic solvent containing gas treatment system.

9.水処理手段の後段にpH を調整するための中和槽を備える上記7または8に記載の有機溶剤含有ガス処理システム。 9. 9. The organic solvent-containing gas treatment system according to 7 or 8 above, further comprising a neutralization tank for adjusting the pH after the water treatment means.

本発明による有機溶剤含有ガス処理システムは、有機溶剤回収処理装置から分離された酸成分や水分を含有している回収有機溶剤を、吸着材を使用した連続精製装置に導入することで、多量の回収有機溶剤中から酸成分や水分を安定して除去することができる利点と、
有機溶剤回収処理装置から分離排出された有機溶剤含有排水を水処理装置で効果的に処理することで、排水中の有機溶剤を除去する利点と、 By effectively treating the organic solvent-containing wastewater separated and discharged from the organic solvent recovery treatment equipment with the water treatment equipment, the advantage of removing the organic solvent in the wastewater and
除去した有機溶剤を有機溶剤回収処理装置に戻すことで効果的に有機溶剤を回収できる利点と、 The advantage of being able to effectively recover the organic solvent by returning the removed organic solvent to the organic solvent recovery processing device,
さらには、有機溶剤回収処理装置から分離排出された排水を、または前記水処理装置で処理された排水をクーリングタワーに導入することで、排水を排出しないシステムとすることを実現しただけでなく、有機溶剤含有水蒸気を凝縮するための溶剤分離装置のコンデンサーに必要な冷却水を排水から製造することができる利点がある。 Furthermore, by introducing the wastewater separated and discharged from the organic solvent recovery treatment device or the wastewater treated by the water treatment device into the cooling tower, it is possible not only to realize a system that does not discharge the wastewater, but also to make it organic. There is an advantage that the cooling water required for the condenser of the solvent separator for condensing the solvent-containing steam can be produced from the waste water. The organic solvent-containing gas processing system according to the present invention introduces a recovered organic solvent containing an acid component and water separated from an organic solvent recovery processing device into a continuous purification device using an adsorbent, so that a large amount of The advantage that acid components and moisture can be stably removed from the recovered organic solvent, The organic solvent-containing gas processing system according to the present invention introduces a recovered organic solvent containing an acid component and water separated from an organic solvent recovery processing device into a continuous purification device using an adsorbent, so that a large amount of The advantage that acid components and moisture can be stably removed from the recovered organic solvent,
By effectively treating the organic solvent-containing wastewater separated and discharged from the organic solvent recovery treatment device with the water treatment device, the advantage of removing the organic solvent in the wastewater, By effectively treating the organic solvent-containing wastewater separated and discharged from the organic solvent recovery treatment device with the water treatment device, the advantage of removing the organic solvent in the wastewater,
The advantage that the organic solvent can be effectively recovered by returning the removed organic solvent to the organic solvent recovery processing device, The advantage that the organic solvent can be effectively recovered by returning the removed organic solvent to the organic solvent recovery processing device,
Furthermore, the wastewater separated and discharged from the organic solvent recovery treatment device or the wastewater treated by the water treatment device is introduced into the cooling tower to realize a system that does not discharge wastewater. There is an advantage that the cooling water required for the condenser of the solvent separator for condensing the solvent-containing water vapor can be produced from the waste water. There is an advantage that the cooling water required for the further, the wastewater separated and discharged from the organic solvent recovery treatment device or the wastewater treated by the water treatment device is introduced into the cooling tower to realize a system that does not discharge wastewater. condenser of the solvent separator for condensing the solvent-containing water vapor can be produced from the waste water.

本発明の実施形態の例を2つ挙げて説明する。
始めに図1にて説明する。 First, it will be described with reference to FIG. 被処理ガス11を吸着送風機12にて有機溶剤回収処理装置10に導入する。 The gas to be treated 11 is introduced into the organic solvent recovery treatment device 10 by the adsorption blower 12. 導入された被処理ガス11は吸着槽13に送られ、吸着材14を通過する際に被処理ガス中の有機溶剤を吸着除去して処理出口16から清浄空気として排出される。 The introduced gas 11 to be treated is sent to the adsorption tank 13, and when passing through the adsorbent 14, the organic solvent in the gas to be treated is adsorbed and removed and discharged as clean air from the treatment outlet 16. 一方で吸着材14に脱着用スチーム15を供給することにより吸着材14から脱着された有機溶剤を含有した有機溶剤含有水蒸気17は、溶剤分離装置20に送られ、コンデンサー21で液化され、分離排水22と回収有機溶剤23に分離される。 On the other hand, the organic solvent-containing steam 17 containing the organic solvent desorbed from the adsorbent 14 by supplying the desorption steam 15 to the adsorbent 14 is sent to the solvent separation device 20, liquefied by the condenser 21, and separated and discharged. It is separated into 22 and the recovered organic solvent 23. 分離された回収有機溶剤23は酸成分除去用溶剤精製装置40に導入される。 The separated recovered organic solvent 23 is introduced into the solvent purification device 40 for removing the acid component. 一方、分離排水22は曝気槽31に導入されて曝気処理し、中和槽32に導入されて中和処理後、クーリングタワー33に導入されるシステムである。 On the other hand, the separated wastewater 22 is a system that is introduced into the aeration tank 31 for aeration treatment, introduced into the neutralization tank 32 for neutralization treatment, and then introduced into the cooling tower 33. Two examples of embodiments of the present invention will be described. Two examples of embodiments of the present invention will be described.
First, a description will be given with reference to FIG. The gas to be treated 11 is introduced into the organic solvent recovery treatment apparatus 10 by the adsorption blower 12. The introduced gas 11 to be treated is sent to the adsorption tank 13, and when passing through the adsorbent 14, the organic solvent in the gas to be treated is adsorbed and removed and discharged from the treatment outlet 16 as clean air. On the other hand, the organic solvent-containing water vapor 17 containing the organic solvent desorbed from the adsorbent 14 by supplying the desorbing steam 15 to the adsorbent 14 is sent to the solvent separator 20, liquefied by the condenser 21, and separated waste water. 22 and recovered organic solvent 23. The separated recovered organic solvent 23 is introduced into an acid component removing solvent purifier 40. On the other hand, the separated drainage 22 is a system that is introduced into the aeration tank 31 and aerated, introduced into the neutralization t First, a description will be given with reference to FIG. The gas to be treated 11 is introduced into the organic solvent recovery treatment apparatus 10 by the adsorption blower 12. The introduced gas 11 to be treated is sent to the adsorption tank 13, and When passing through the adsorbent 14, the organic solvent in the gas to be treated is adsorbed and removed and discharged from the treatment outlet 16 as clean air. On the other hand, the organic solvent-containing water vapor 17 containing the organic solvent desorbed from the adsorbent 14 by supplying the desorbing steam 15 to the adsorbent 14 is sent to the solvent separator 20, liquefied by the glycol 21, and separated waste water. 22 and recovered organic solvent 23. The separated recovered organic solvent 23 is introduced into an acid component removing solvent purifier 40. On the other hand, the separated drainage 22 is a system that is introduced into the aeration tank 31 and aerated, introduced into the neutralization t ank 32, neutralized, and then introduced into the cooling tower 33. ank 32, neutralized, and then introduced into the cooling tower 33.

次に図2について説明する。被処理ガス11を吸着送風機12にて有機溶剤回収処理装置10に導入する。導入された被処理ガス11は吸着槽13に送られ、吸着材14を通過する際に被処理ガス中の有機溶剤を吸着除去して処理出口16から清浄空気として排出される。一方で吸着材14に脱着用スチーム15を供給することによりに吸着材14から脱着された有機溶剤を含有した有機溶剤含有水蒸気17は、溶剤分離装置20に送られ、コンデンサー21で液化され、分離排水22と回収有機溶剤23に分離される。分離された回収有機溶剤23は酸成分除去用溶剤精製装置40に導入され、被処理回収有機溶剤タンク51に導入される。被処理回収有機溶剤タンク51から吸着材が充填された水分吸着塔52に回収有機溶剤が導入され、吸着材が回収有機溶剤中の水分を吸着除去し、回収有機溶剤タンク53導入される。一方、パージ用水タンク54から水用ポンプ55を用いて、水分吸着塔52に水を導入し、水分吸着塔52内の吸着材に付着している残存有機溶剤をパージさせて、パージ水曝気槽導入ライン58を通って曝気槽31に導入される。その後、コンプレッサー56から乾燥空気を水分吸着塔52に導入し、吸着材に吸着した水分を脱着する。このときの使用済み乾燥空気はパージ水曝気槽導入ライン58を通じて曝気槽31に導入される。また、溶剤分離装置20で分離された有機溶剤を含有した分離排水22は、曝気槽31に導入されて有機溶剤を揮発除去し、戻りガス導入ライン34を通じて有機溶剤回収処理装置10の入口である被処理ガス11に戻す。曝気槽31で処理後の排水は、吸脱着式有機溶剤含有水処理装置60に導入され、吸着材61に導入され有機溶剤を吸着除去し、処理した排水は中和槽32に導入され、中和後クーリングタワー33に導入される。クーリングタワーで排水から製造した冷却水は溶剤分離装置20におけるコンデンサー21に供給する。一方で、パージ空気供給送風機64で空気を供給して、吸着後の吸着材61に付着している水をパージ処理し、その水は戻り水ライン65を通じて吸着材61の入口に戻す。パージ処理後に脱着ガス供給送風機62から供給した空気を脱着ガス用ヒーター63にて加熱した加熱空気で有機溶剤を脱着する。曝気槽31で揮発された有機溶剤含有空気と吸脱着式有機溶剤含有水処理装置60で脱着された有機溶剤含有空気は戻りガスライン66を通じて有機溶剤回収処理装置10の入口である被処理ガス11に戻すシステムである。   Next, FIG. 2 will be described. The gas to be treated 11 is introduced into the organic solvent recovery treatment apparatus 10 by the adsorption blower 12. The introduced gas 11 to be treated is sent to the adsorption tank 13, and when passing through the adsorbent 14, the organic solvent in the gas to be treated is adsorbed and removed and discharged from the treatment outlet 16 as clean air. On the other hand, the organic solvent-containing water vapor 17 containing the organic solvent desorbed from the adsorbent 14 by supplying the desorption steam 15 to the adsorbent 14 is sent to the solvent separator 20, liquefied by the condenser 21, and separated. The waste water 22 and the recovered organic solvent 23 are separated. The separated recovered organic solvent 23 is introduced into an acid component removing solvent refining apparatus 40 and introduced into a treated recovered organic solvent tank 51. The recovered organic solvent is introduced from the treated recovered organic solvent tank 51 into the moisture adsorption tower 52 filled with the adsorbent, and the adsorbent adsorbs and removes moisture in the recovered organic solvent, and is then introduced into the recovered organic solvent tank 53. On the other hand, water is introduced from the purge water tank 54 to the moisture adsorption tower 52 using the water pump 55, and the residual organic solvent adhering to the adsorbent in the moisture adsorption tower 52 is purged, and a purge water aeration tank It is introduced into the aeration tank 31 through the introduction line 58. Thereafter, dry air is introduced from the compressor 56 into the moisture adsorption tower 52, and moisture adsorbed on the adsorbent is desorbed. The used dry air at this time is introduced into the aeration tank 31 through the purge water aeration tank introduction line 58. Further, the separated waste water 22 containing the organic solvent separated by the solvent separation device 20 is introduced into the aeration tank 31 to volatilize and remove the organic solvent, and is an inlet of the organic solvent recovery processing device 10 through the return gas introduction line 34. Return to the gas 11 to be treated. Wastewater after treatment in the aeration tank 31 is introduced into an adsorption / desorption type organic solvent-containing water treatment device 60, introduced into the adsorbent 61, and adsorbed and removed, and the treated wastewater is introduced into the neutralization tank 32. It is introduced into the Wago Cooling Tower 33. The cooling water produced from the waste water in the cooling tower is supplied to the condenser 21 in the solvent separator 20. On the other hand, air is supplied by the purge air supply blower 64 to purge the water adhering to the adsorbent 61 after adsorption, and the water is returned to the inlet of the adsorbent 61 through the return water line 65. After the purge process, the organic solvent is desorbed with heated air in which the air supplied from the desorption gas supply blower 62 is heated by the desorption gas heater 63. The organic solvent-containing air volatilized in the aeration tank 31 and the organic solvent-containing air desorbed in the adsorption / desorption-type organic solvent-containing water treatment device 60 pass through the return gas line 66 to be treated gas 11 as an inlet of the organic solvent recovery treatment device 10. It is a system to return to.

本発明にかかる有機溶剤回処理収装置の吸着材は、粒状活性炭、活性炭素繊維、ゼオライト、シリカゲルなど特に限定されるものではないが、特に活性炭素繊維が好ましい。かかる吸着材における活性炭素繊維は粒状活性炭と比較して吸着速度が速く、低濃度の有機ガスを吸着する機能に優れているためである。   The adsorbent of the organic solvent recovery apparatus according to the present invention is not particularly limited, such as granular activated carbon, activated carbon fiber, zeolite, silica gel, etc., but activated carbon fiber is particularly preferable. This is because the activated carbon fiber in such an adsorbent has a higher adsorption speed than granular activated carbon and is excellent in the function of adsorbing low-concentration organic gas.

本発明にかかる酸成分除去用溶剤精製装置は、安価な吸着剤を充填させた吸着交換フィルターユニット式の精製装置が好ましい。該吸着剤は、塩化マグネシウム、塩化カリウム、塩化カルシウム、塩化バリウム、炭酸マグネシウム、炭酸カリウム、炭酸カルシウム、炭酸バリウム等の内で1種類、または2種類以上の組み合わせが好ましい。該吸着剤の形状は、粒状、粉体状、ハニカム状等特に限定されるものではないが、成形が容易で、液体状の溶剤を流入させるときに圧損が低く、吸着剤の系外への流出がほとんどない粒状が好ましい。粒形の大きさは吸着剤が流出しにくいように0.3mm以上であることが好ましい。また、例えば粒状の炭酸カルシウムを用いる場合、粉末状の炭酸カルシウムを造粒する方法もあるが、炭酸カルシウム成分が90%以上を占める石灰石や寒水石等の自然石を破砕したものを用いることも安価で効果的である。   The solvent purification apparatus for removing acid components according to the present invention is preferably an adsorption exchange filter unit type purification apparatus filled with an inexpensive adsorbent. The adsorbent is preferably one or a combination of two or more of magnesium chloride, potassium chloride, calcium chloride, barium chloride, magnesium carbonate, potassium carbonate, calcium carbonate, barium carbonate and the like. The shape of the adsorbent is not particularly limited, such as granular, powder, honeycomb, etc., but it is easy to mold and has a low pressure loss when flowing a liquid solvent, so that the adsorbent can be removed from the system. Granules with little outflow are preferred. The size of the particle shape is preferably 0.3 mm or more so that the adsorbent hardly flows out. For example, when granular calcium carbonate is used, there is a method of granulating powdered calcium carbonate, but it is also possible to use a crushed natural stone such as limestone or cold water stone in which the calcium carbonate component accounts for 90% or more. Inexpensive and effective.

酸成分除去用溶剤精製装置において除去可能な酸成分は、強酸である塩酸、硫酸、過塩素酸、弱酸である硝酸、酢酸、ギ酸、炭酸等であり、特に限定されるものではないが、コストを勘案しつつ酸成分によって適した吸着剤を選定することが好ましく、酢酸を除去するためには安価な炭酸カルシウムを選定することが好ましい。   The acid components that can be removed in the solvent refining apparatus for removing acid components are strong acids such as hydrochloric acid, sulfuric acid, perchloric acid, weak acids such as nitric acid, acetic acid, formic acid, and carbonic acid. In consideration of the above, it is preferable to select an adsorbent suitable for the acid component. In order to remove acetic acid, it is preferable to select inexpensive calcium carbonate.

本発明にかかる水分除去用溶剤精製装置としては、吸着材を用いた連続吸脱着式が好ましい。ワンパスの吸着交換フィルターユニット式と比較して、吸着材の寿命が飛躍的に長く、吸着材の交換によるランニングコストを大幅に抑えることが可能である。該吸着材として、ゼオライト、シリカゲル、活性アルミナを用いても良いが、陽イオン交換樹脂を用いることが好ましい。陽イオン交換樹脂は有機溶剤を吸着せず水分だけを吸収可能であるだけでなく、その水分の吸着保持量が他の吸着材と比較して2〜20倍と高く、粒状または繊維状であることから吸着槽への充填量を多くでき、液体状の有機溶剤と吸着材との接触効率が高く効率的に水分吸着できるからである。   As the solvent purification apparatus for removing water according to the present invention, a continuous adsorption / desorption method using an adsorbent is preferable. Compared to the one-pass adsorption exchange filter unit type, the life of the adsorbent is dramatically increased, and the running cost due to the exchange of the adsorbent can be greatly reduced. As the adsorbent, zeolite, silica gel or activated alumina may be used, but a cation exchange resin is preferably used. The cation exchange resin not only adsorbs organic solvents but can absorb only moisture, and its moisture retention is 2 to 20 times higher than other adsorbents, and is granular or fibrous. This is because the amount of filling into the adsorption tank can be increased, and the contact efficiency between the liquid organic solvent and the adsorbent is high, and moisture can be adsorbed efficiently.

水分除去用有機溶剤精製装置において、有機溶剤を吸着材に導入して水分を吸着させる吸着工程と、乾燥空気を吸着材に導入して吸着材中の水分を脱着させる脱着工程の間に、吸着材に付着した有機溶剤を水でパージするパージ工程を入れることが好ましい。つまり、パージ工程で吸着材に付着した有機溶剤を除去することで、その後の脱着工程において吸着材の乾燥が容易になるだけでなく、付着した有機溶剤を回収することができるため、効率的だからである。   In an organic solvent refining device for removing moisture, adsorption is performed between an adsorption process in which an organic solvent is introduced into the adsorbent to adsorb moisture and a desorption process in which dry air is introduced into the adsorbent and moisture in the adsorbent is desorbed. It is preferable to add a purge step of purging the organic solvent adhering to the material with water. In other words, by removing the organic solvent adhering to the adsorbent in the purge process, not only can the adsorbent be easily dried in the subsequent desorption process, but also the adhering organic solvent can be recovered, which is efficient. It is.

水分除去用有機溶剤精製装置にかかる吸着材の運転は、吸着槽を2つ以上設けた連続除去可能なシステムを採用することが好ましいが、除去すべき含有水分量、被処理有機溶剤の量等を勘案して、間欠運転としてもよい。含有水分の量あるいは被処理有機溶剤の量が少ない条件では、連続運転であることまで要求されず、運転コストを削減できるからである。   The operation of the adsorbent for the organic solvent refining apparatus for removing water preferably employs a system capable of continuous removal provided with two or more adsorption tanks, but the amount of water to be removed, the amount of organic solvent to be treated, etc. Considering this, intermittent operation may be used. This is because, under conditions where the amount of moisture contained or the amount of the organic solvent to be treated is small, it is not required that the operation is continuous, and the operation cost can be reduced.

本発明にかかるクーリングタワーは、開放式、密閉式と特に限定されるものではないが、排水量によって最適なクーリングタワーを選定することが好ましい。また、開放式を採用したときのクーリングタワーの構造も然りで、排水量によって角型か丸型か最適な形状を選定することが好ましい。更に、クーリングタワーによって排水から製造された冷却水の使用に関して特に限定されるものではないが、有機溶剤分離装置におけるコンデンサーに使用することがより好ましい。   The cooling tower according to the present invention is not particularly limited to an open type and a closed type, but it is preferable to select an optimal cooling tower according to the amount of drainage. In addition, the structure of the cooling tower when the open type is adopted is also the same, and it is preferable to select an optimal shape, square or round, depending on the amount of drainage. Furthermore, although it does not specifically limit regarding the use of the cooling water manufactured from the waste_water | drain with the cooling tower, It is more preferable to use it for the condenser in an organic solvent separation apparatus.

本発明にかかる有機溶剤回収処理装置とクーリングタワーの中間に設置する排水処理装置は、曝気式、吸着交換フィルターユニット式、吸脱着処理式、活性汚泥式と特に限定されるものではないが、曝気式および/または吸脱着処理式水処理装置が好ましい。有機溶剤を高濃度で含有する場合が多いため、吸着交換フィルターユニットは交換頻度が多くなり、活性汚泥式では設置スペースを広く必要になるからである。   The wastewater treatment device installed between the organic solvent recovery treatment device and the cooling tower according to the present invention is not particularly limited to an aeration type, an adsorption exchange filter unit type, an adsorption / desorption treatment type, and an activated sludge type, but an aeration type An adsorption / desorption type water treatment device is preferred. This is because, since the organic solvent is often contained at a high concentration, the adsorption exchange filter unit is frequently replaced, and the activated sludge type requires a large installation space.

曝気式排水処理装置において、有機溶剤の揮発を促進させるために加熱することが好ましい。このとき、熱交換器等を使用することで、有機溶剤回収処理装置から脱着した有機溶剤含有水蒸気の潜熱または顕熱を曝気槽中の排水の加熱源として利用することが経済的に更に好ましい。   In the aeration type waste water treatment apparatus, it is preferable to heat the organic solvent to promote the volatilization of the organic solvent. At this time, by using a heat exchanger or the like, it is more economically preferable to use the latent heat or sensible heat of the organic solvent-containing water vapor desorbed from the organic solvent recovery treatment apparatus as a heat source for the waste water in the aeration tank.

吸脱着処理式排水処理装置の吸着材は、粒状、粉体状、繊維状、ハニカム状の活性炭やゼオライトやシリカゲルや活性アルミナ等が挙げられるが、特に活性炭素繊維を用いた連続吸脱着方式の排水処理装置であることが好ましい。つまり、活性炭素繊維は表面にミクロ孔を有する事と繊維状構造であることで水との接触効率が高いことで、特に水中の有機溶剤の吸着速度が速くなり、他の構造に比べて極めて高い除去効率を発現でき、更に高効率処理のために導入するパージ工程においてガスの流通により吸着素子表面の水滴を除去する際にも、容易に水滴の除去が可能となるからである。   Examples of the adsorbent of the adsorption / desorption treatment type wastewater treatment equipment include granular, powder, fiber, and honeycomb activated carbon, zeolite, silica gel, activated alumina, and the like, and in particular, a continuous adsorption / desorption method using activated carbon fibers. A waste water treatment device is preferred. In other words, the activated carbon fiber has micropores on the surface and a fibrous structure, so the contact efficiency with water is high, and in particular, the adsorption rate of the organic solvent in water is increased, which is extremely high compared to other structures. This is because high removal efficiency can be exhibited, and even when water droplets on the surface of the adsorption element are removed by gas flow in a purge process introduced for high-efficiency processing, water droplets can be easily removed.

排水処理装置において、曝気式および/または吸脱着式水処理装置の下流に中和槽を設けることが好ましい。曝気式および/または吸脱着式水処理装置から排出される排水のpH は酸性であることから、中和することでクーリングタワーや配管の腐食を抑制することができるためである。   In the waste water treatment apparatus, it is preferable to provide a neutralization tank downstream of the aeration type and / or adsorption / desorption type water treatment apparatus. This is because the pH of the waste water discharged from the aeration type and / or the adsorption / desorption type water treatment device is acidic, so that the corrosion of the cooling tower and piping can be suppressed by neutralization.

排水処理装置において、戻りガスラインを通じて揮発または脱着された有機溶剤含有空気を有機溶剤回収処理装置の入口に戻すことが好ましい。発生した有機溶剤含有空気から更に有機溶剤を回収することができ効率的だからである。   In the wastewater treatment apparatus, it is preferable to return the organic solvent-containing air that has been volatilized or desorbed through the return gas line to the inlet of the organic solvent recovery treatment apparatus. This is because the organic solvent can be further recovered from the generated organic solvent-containing air, which is efficient.

本発明にかかる有機溶剤含有ガス処理システムにおいて、処理可能な有機溶剤は酢酸エチル、酢酸メチル、酢酸ブチル、メチルエチルケトン、メチルブチルケトン、ヘプタノン、アセトン、トルエン、キシレン、ベンゼン、PGMEA、PGME、メタノール、エタノール、プロパノール、クロロホルム、塩化メチレン、四塩化炭素等特に限定されるものではなく、その混合物であっても例外ではない。   In the organic solvent-containing gas treatment system according to the present invention, the organic solvents that can be treated are ethyl acetate, methyl acetate, butyl acetate, methyl ethyl ketone, methyl butyl ketone, heptanone, acetone, toluene, xylene, benzene, PGMEA, PGME, methanol, ethanol. , Propanol, chloroform, methylene chloride, carbon tetrachloride and the like are not particularly limited, and a mixture thereof is no exception.

本発明にかかる有機溶剤含有ガス処理システムにおけるクーリングタワーから排出される空気において、微量濃度の有機溶剤が含有している場合、有機溶剤含有ガス濃縮処理装置を用いてクーリングタワーから排出される空気中の有機溶剤を濃縮し、有機溶剤回収処理装置の入口に戻すことが好ましい。図3は有機溶剤含有ガス濃縮処理装置の原理を示したものである。同図において、大風量・低濃度の揮発性有機化合物(VOC)含有ガス中の有機溶剤を吸着するための有機溶剤含有ガス濃縮処理装置90は、回転中心軸96まわりに回転可能な円筒形のケース91を有しており、このケース91内にVOCを吸着するためのハニカム構造(連通路を中心軸方向に向けている)からなる吸着材95が収納され全体として筒状吸着体を構成している。吸着材95はVOC含有ガスの成分に応じて活性炭素繊維やゼオライトペーパー等が適宜選択される。筒状吸着体が回転する移動経路上には吸着部93と脱着部97が区画されており、吸着材95がそれら吸着部93と脱着部97とを交互に通過するようになっている。上記吸着部93には、例えば工場内で発生したVOC含有ガスを導入するためのVOC含有ガス供給管92と、有機溶剤含有ガス濃縮処理装置90の吸着材95によって浄化された清浄空気を工場へ送り出すための浄化空気送出管94が設けられている。また、脱着部97には、VOCを吸着した吸着材95に対し例えば180℃の高温乾燥空気、すなわち脱着用加熱空気を吹き付けるための脱着用空気供給管98が設けられており、脱着用加熱空気の風量がVOC含有ガスの風量の1/2〜1/50程度に設定されていることにより脱着されるガスが濃縮されるようになっている。   In the air exhausted from the cooling tower in the organic solvent-containing gas treatment system according to the present invention, when a trace amount of organic solvent is contained, the organic matter in the air exhausted from the cooling tower using the organic solvent-containing gas concentration treatment device is used. It is preferable to concentrate the solvent and return it to the inlet of the organic solvent recovery processor. FIG. 3 shows the principle of the organic solvent-containing gas concentration treatment apparatus. In the drawing, an organic solvent-containing gas concentration treatment device 90 for adsorbing an organic solvent in a gas containing a large amount of air and a low concentration volatile organic compound (VOC) is a cylindrical shape that can rotate around a rotation center axis 96. The case 91 has an adsorbent 95 made of a honeycomb structure (with the communication path oriented in the central axis direction) for adsorbing VOC in the case 91, and forms a cylindrical adsorbent as a whole. ing. For the adsorbent 95, activated carbon fiber, zeolite paper, or the like is appropriately selected according to the components of the VOC-containing gas. An adsorbing portion 93 and a desorbing portion 97 are partitioned on a moving path along which the cylindrical adsorbing body rotates, and an adsorbent 95 passes through the adsorbing portion 93 and the desorbing portion 97 alternately. In the adsorbing section 93, for example, clean air purified by the VOC-containing gas supply pipe 92 for introducing the VOC-containing gas generated in the factory and the adsorbent 95 of the organic solvent-containing gas concentration treatment apparatus 90 is sent to the factory. A purified air delivery pipe 94 is provided for delivery. In addition, the desorption part 97 is provided with a desorption air supply pipe 98 for blowing high-temperature dry air at 180 ° C., that is, desorption heating air, to the adsorbent 95 that has adsorbed VOC. Is set to be about 1/2 to 1/50 of the volume of the VOC-containing gas, so that the desorbed gas is concentrated.

以下、実施例によりさらに本発明を詳細に説明するが、本発明はこれら実施例に限定されるものではない。
なお、評価は下記の方法によりおこなった。
EXAMPLES Hereinafter, although an Example demonstrates this invention further in detail, this invention is not limited to these Examples.
The evaluation was performed by the following method.

(酢酸エチル、酢酸、エタノール、塩化メチレン溶剤濃度評価)
入口・出口の濃度をガスクロマトグラフ法により分析し測定した。
(Ethyl acetate, acetic acid, ethanol, methylene chloride solvent concentration evaluation)
The concentrations at the inlet and outlet were analyzed and measured by gas chromatography.

(溶剤中の水分濃度評価)
回収した有機溶剤の水分濃度をカールフィッシャ―水分濃度計を用いて分析した。
(Evaluation of water concentration in solvent)
The water concentration of the recovered organic solvent was analyzed using a Karl Fischer-water concentration meter.

(除去率)
除去率(%)=(装置入口ガス濃度−装置出口ガス濃度)/装置入口ガス濃度×100
(Exclusion rate)
Removal rate (%) = (device inlet gas concentration−device outlet gas concentration) / device inlet gas concentration × 100

[実施例1]
図2に示す有機溶剤含有ガス処理システムを使用し、酢酸エチル2000ppmを含む40℃の被処理ガス11を、有機溶剤回収処理装置10に導入した。 Using the organic solvent-containing gas treatment system shown in FIG. 2, the gas to be treated 11 at 40 ° C. containing 2000 ppm of ethyl acetate was introduced into the organic solvent recovery treatment apparatus 10. その際に風量100Nm /分で吸着送風機12より吸着槽13に送風し、吸着槽13で吸着材14として平均細孔径17.4Å、BET比表面積1650m /g、全細孔容積0.66cm /gの活性炭素繊維を使用し、9分間吸着を行い、清浄空気を排出した。 At that time, air is blown from the adsorption blower 12 to the adsorption tank 13 with an air volume of 100 Nm 3 / min, and the average pore diameter of the adsorbent 14 is 17.4 Å, the BET specific surface area is 1650 m 2 / g, and the total pore volume is 0.66 cm. Using 3 / g of activated carbon fiber, adsorption was performed for 9 minutes, and clean air was discharged. その際の清浄空気の酢酸エチル濃度は20ppm以下であり、99%の除去率で処理をした。 At that time, the ethyl acetate concentration of the clean air was 20 ppm or less, and the treatment was performed with a removal rate of 99%. その後自動ダンパーで吸着槽13への送風を封鎖し、次に吸着槽の活性炭素繊維に脱着用スチーム15を噴出した。 After that, the air blown to the adsorption tank 13 was blocked by an automatic damper, and then the desorption steam 15 was ejected onto the activated carbon fibers of the adsorption tank. この処置と同時に別の吸着槽の自動ダンパーを開放し、今度はこの吸着槽で酢酸エチルガスの吸着処理を行った。 At the same time as this treatment, the automatic damper of another adsorption tank was opened, and this time, the adsorption treatment of ethyl acetate gas was performed in this adsorption tank. この吸着と脱着の操作を繰り返し実施した。 This adsorption and desorption operation was repeated. [Example 1] [Example 1]
Using the organic solvent-containing gas treatment system shown in FIG. 2, a gas to be treated 11 containing 2000 ppm of ethyl acetate was introduced into the organic solvent recovery treatment apparatus 10. At that time, the air flow is blown from the adsorption blower 12 to the adsorption tank 13 at an air flow rate of 100 Nm 3 / min, and the adsorption tank 13 serves as an adsorbent 14 with an average pore diameter of 17.4 mm, a BET specific surface area of 1650 m 2 / g, and a total pore volume of 0.66 cm. 3 / g of activated carbon fiber was used, adsorption was performed for 9 minutes, and clean air was discharged. The ethyl acetate concentration of the clean air at that time was 20 ppm or less, and the treatment was performed with a removal rate of 99%. Thereafter, the air blown to the adsorption tank 13 was blocked with an automatic damper, and then the desorption steam 15 was jetted onto the activated carbon fiber of the adsorption tank. Simultaneously with this treatment, the a Using the organic solvent-containing gas treatment system shown in FIG. 2, a gas to be treated 11 containing 2000 ppm of ethyl acetate was introduced into the organic solvent recovery treatment apparatus 10. At that time, the air flow is blown from the adsorption blower 12 to the adsorption tank 13 at an air flow rate of 100 Nm 3 / min, and the adsorption tank 13 serves as an adsorbent 14 with an average pore diameter of 17.4 mm, a BET specific surface area of ​​1650 m 2 / g, and a total pore volume of 0.66 cm. 3 / g of activated carbon fiber was used, adsorption was performed for 9 minutes, and clean air was solvent. The ethyl acetate concentration of the clean air at that time was 20 ppm or less, and The treatment was performed with a removal rate of 99%. Meaning, the air blown to the adsorption tank 13 was blocked with an automatic damper, and then the desorption steam 15 was jetted onto the activated carbon fiber of the adsorption tank. Simultaneously with this treatment, the a utomatic damper of another adsorption tank was opened, and this time the adsorption process of ethyl acetate gas was performed in this adsorption tank. This adsorption and desorption operation was repeated. utomatic damper of another adsorption tank was opened, and this time the adsorption process of ethyl acetate gas was performed in this adsorption tank. This adsorption and desorption operation was repeated.

有機溶剤回収処理装置10から得られた有機溶剤含有水蒸気17を、溶剤分離装置20に送りコンデンサー21で冷却し、酢酸エチル主体の回収有機溶剤23と酢酸エチルが微量に含まれた分離排水22を得た。回収有機溶剤中の酢酸エチル濃度は96.8重量%、水分濃度は3.1重量%、エタノール濃度は400ppm、酢酸濃度は600ppmであり、分離排水の酢酸エチル濃度は40000ppm、酢酸濃度は2000ppm、エタノール濃度は2000ppmで、水量は310kg/hrの量であった。   The organic solvent-containing water vapor 17 obtained from the organic solvent recovery treatment device 10 is sent to the solvent separation device 20 and cooled by the condenser 21, and the recovered organic solvent 23 mainly composed of ethyl acetate and the separated waste water 22 containing a small amount of ethyl acetate are obtained. Obtained. The ethyl acetate concentration in the recovered organic solvent is 96.8% by weight, the water concentration is 3.1% by weight, the ethanol concentration is 400 ppm, and the acetic acid concentration is 600 ppm. The ethyl acetate concentration in the separated wastewater is 40000 ppm, the acetic acid concentration is 2000 ppm, The ethanol concentration was 2000 ppm, and the amount of water was 310 kg / hr.

前記回収有機溶剤を、平均粒形1.5mmの寒水石(新見化学工業株式会社製)の吸着剤を重量1000g充填させた酸成分除去用溶剤精製装置40に導入した。その際の出口酢酸濃度の経時変化を確認した結果、SV=10(1/h)のとき出口酢酸濃度は60ppm以下、出口水分濃度3.1重量%を示した。酢酸を除去処理した回収有機溶剤を、平均粒形0.7mmの陽イオン交換樹脂(Na型、スルホン酸基、MuromacDW2−1、ムロマチテクノス株式会社製)の吸着材を30重量kg充填させた水分吸着塔52に導入した。その際の出口水分濃度の経時変化を確認した結果、SV=5(1/h)のとき水分濃度が0.5重量%以下の回収有機溶剤を360kg/day得た。次に、水パージ工程として、パージ用水タンク54から水用ポンプ55を使用しパージ水を水分吸着塔52に導入した際の出口水中の酢酸エチル濃度を測定した。その結果、SV=20(1/h)のとき吸着材体積の4倍量の水量で吸着材に付着している酢酸エチルを95%以上除去可能と良好な除去性能を示した。このときの酢酸エチル含有パージ水は溶剤分離装置20へ導入した。続いて、脱着工程における脱着ガスとして、20℃、−10℃DPの乾燥空気を使用し、脱着のSVを2000(1/h)とした。吸着工程における吸着時間は1h、水パージ工程における時間を10min、脱着工程における脱着時間は23hとして吸脱着サイクルとした。   The recovered organic solvent was introduced into an acid component removing solvent refining apparatus 40 filled with 1000 g of an adsorbent of cold water stone (manufactured by Niimi Chemical Industry Co., Ltd.) having an average particle size of 1.5 mm. As a result of confirming the time-dependent change of the outlet acetic acid concentration at that time, the outlet acetic acid concentration was 60 ppm or less and the outlet water concentration was 3.1 wt% when SV = 10 (1 / h). Moisture filled with 30 weight kg of an adsorbent of a cation exchange resin (Na type, sulfonic acid group, Muromac DW2-1, manufactured by Muromachi Technos Co., Ltd.) having an average particle size of 0.7 mm with the recovered organic solvent from which acetic acid has been removed. It was introduced into the adsorption tower 52. As a result of confirming the time-dependent change in the outlet moisture concentration at that time, 360 kg / day of a recovered organic solvent having a moisture concentration of 0.5% by weight or less was obtained when SV = 5 (1 / h). Next, as a water purge step, the concentration of ethyl acetate in the outlet water when the purge water was introduced into the moisture adsorption tower 52 from the purge water tank 54 using the water pump 55 was measured. As a result, when SV = 20 (1 / h), it was possible to remove 95% or more of ethyl acetate adhering to the adsorbent with an amount of water 4 times the volume of the adsorbent. At this time, the purge water containing ethyl acetate was introduced into the solvent separator 20. Subsequently, dry air at 20 ° C. and −10 ° C. DP was used as the desorption gas in the desorption step, and the desorption SV was 2000 (1 / h). The adsorption time in the adsorption process was 1 h, the time in the water purge process was 10 min, the desorption time in the desorption process was 23 h, and the adsorption / desorption cycle was established.

前記分離排水22を曝気槽31に導入した。曝気槽中の排水は40℃から70℃に加温し、エアレーションを行った。曝気槽31で処理した排水の濃度は酢酸エチル40ppm以下であり、除去率99%以上にて処理できた。また、酢酸100ppm、エタノール50ppmの濃度まで低下することができた。また、この際に揮発した溶剤ガスは戻りガス導入ライン34を通じて有機溶剤回収処理装置10の入口である被処理ガス11に戻した。次に、曝気槽31に導入された排水を吸脱着式有機溶剤含有水処理装置60に導入し、吸着材61で排水中の溶剤を吸着させた。このときの排水の濃度は酢酸エチル3ppm以下、酢酸5ppm以下、エタノール3ppm以下であった。パージ、加熱脱着させた溶剤含有ガスは戻りガスライン66を通じて有機溶剤回収処理装置10の入口である被処理ガス11に戻した。その後、処理した排水を中和槽32に導入し、pHを7に中和した。このときの排水のBODは30mg/L以下、CODは10mg/L以下であった。その後、クーリングタワー33に排水を導入し、排水から冷却水を製造し、コンデンサー21に製造した冷却水を導入した。このとき、コンデンサー21に必要な冷却水19m/hrの内、補給冷却水1m/hr中における28%の280kg/hrをクーリングタワーから供給することができた。 The separated waste water 22 was introduced into the aeration tank 31. The waste water in the aeration tank was heated from 40 ° C. to 70 ° C. and aerated. The concentration of the wastewater treated in the aeration tank 31 was 40 ppm or less of ethyl acetate, and could be treated at a removal rate of 99% or more. Moreover, it was able to be reduced to a concentration of 100 ppm acetic acid and 50 ppm ethanol. Further, the solvent gas volatilized at this time was returned to the gas 11 to be processed which is the inlet of the organic solvent recovery processing apparatus 10 through the return gas introduction line 34. Next, the wastewater introduced into the aeration tank 31 was introduced into the adsorption / desorption type organic solvent-containing water treatment device 60, and the adsorbent 61 adsorbed the solvent in the wastewater. The concentration of the waste water at this time was 3 ppm or less of ethyl acetate, 5 ppm or less of acetic acid, and 3 ppm or less of ethanol. The purged and heat-desorbed solvent-containing gas was returned to the gas to be processed 11 which is the inlet of the organic solvent recovery processing apparatus 10 through the return gas line 66. Thereafter, the treated waste water was introduced into the neutralization tank 32 and the pH was neutralized to 7. The BOD of the waste water at this time was 30 mg / L or less, and the COD was 10 mg / L or less. Thereafter, waste water was introduced into the cooling tower 33, cooling water was produced from the waste water, and the produced cooling water was introduced into the condenser 21. At this time, 28% of 280 kg / hr in the supplementary cooling water 1 m 3 / hr out of the cooling water 19 m 3 / hr necessary for the condenser 21 could be supplied from the cooling tower.

本実施例の有機溶剤含有ガス処理システムは、100時間後でも有機溶剤回収装置の除去率、溶剤精製装置の性能、水処理装置除去率共に90〜99%の効率で処理が可能であった。吸着と脱着を連続して行い処理するため、性能低下がなく安定して高い効率で処理ができる。更に、排水を冷却水として利用することができるため、経済的に効率的であるだけでなく、排水を環境中に排出しない利点も付加することができた。   The organic solvent-containing gas treatment system of this example was capable of treating with an efficiency of 90 to 99% for both the removal rate of the organic solvent recovery device, the performance of the solvent purification device, and the water treatment device removal rate even after 100 hours. Since adsorption and desorption are performed continuously, processing is stable and highly efficient with no performance degradation. Furthermore, since the wastewater can be used as cooling water, not only is it economically efficient, but also the advantage of not discharging the wastewater into the environment can be added.

[実施例2]
図1に示す有機溶剤含有ガス処理システムを使用し、塩化メチレン2000ppm、酢酸5ppm含む30℃の被処理ガス11を、有機溶剤回収処理装置10に導入した。 Using the organic solvent-containing gas treatment system shown in FIG. 1, the gas to be treated 11 at 30 ° C. containing 2000 ppm of methylene chloride and 5 ppm of acetic acid was introduced into the organic solvent recovery treatment apparatus 10. その際に風量100Nm /分で吸着送風機12より吸着槽13に送風し、吸着槽で吸着材14として平均細孔径17.4Å、BET比表面積1650m /g、全細孔容積0.66cm /gの活性炭素繊維14を使用し、9分間吸着を行い、清浄空気を排出した。 At that time, air is blown from the adsorption blower 12 to the adsorption tank 13 with an air volume of 100 Nm 3 / min, and the average pore diameter is 17.4 Å, the BET specific surface area is 1650 m 2 / g, and the total pore volume is 0.66 cm 3 as the adsorbent 14 in the adsorption tank. Using / g of activated carbon fiber 14, adsorption was performed for 9 minutes, and clean air was discharged. その際の清浄空気の塩化メチレン濃度は20ppm以下であり、99%以上の除去率で処理をした。 At that time, the methylene chloride concentration of the clean air was 20 ppm or less, and the treatment was performed with a removal rate of 99% or more. その後自動ダンパーで吸着槽13への送風を封鎖し、次に吸着槽の活性炭素繊維に脱着用スチーム15を噴出した。 After that, the air blown to the adsorption tank 13 was blocked by an automatic damper, and then the desorption steam 15 was ejected onto the activated carbon fibers of the adsorption tank. この処置と同時に別の吸着槽の自動ダンパーを開放し、今度はこの吸着槽で塩化メチレンガスの吸着処理を行った。 At the same time as this treatment, the automatic damper of another adsorption tank was opened, and this time, the adsorption treatment of methylene chloride gas was performed in this adsorption tank. この吸着と脱着の操作を繰り返し実施した。 This adsorption and desorption operation was repeated. [Example 2] [Example 2]
Using the organic solvent-containing gas treatment system shown in FIG. 1, a gas to be treated 11 containing 2000 ppm of methylene chloride and 5 ppm of acetic acid at 30 ° C. was introduced into the organic solvent recovery treatment apparatus 10. At that time, the air flow was blown from the adsorption blower 12 to the adsorption tank 13 at an air flow of 100 Nm 3 / min, and the average fine pore diameter of 17.4 mm, the BET specific surface area of 1650 m 2 / g, and the total pore volume of 0.66 cm 3 as the adsorbent 14 in the adsorption tank. / G of activated carbon fiber 14 was used for adsorption for 9 minutes, and clean air was discharged. The methylene chloride concentration of the clean air at that time was 20 ppm or less, and the treatment was performed with a removal rate of 99% or more. Thereafter, the air blown to the adsorption tank 13 was blocked with an automatic damper, and then the desorption steam 15 was jetted onto the activated carbon fiber of the adsorption tank. Using the organic solvent-containing gas treatment system shown in FIG. 1, a gas to be treated 11 containing 2000 ppm of methylene chloride and 5 ppm of acetic acid at 30 ° C. was introduced into the organic solvent recovery treatment apparatus 10. At that time, the air flow was blown from the adsorption blower 12 to the adsorption tank 13 at an air flow of 100 Nm 3 / min, and the average fine pore diameter of 17.4 mm, the BET specific surface area of ​​1650 m 2 / g , and the total pore volume of 0.66 cm 3 as the adsorbent 14 in the adsorption tank. / G of activated carbon fiber 14 was used for adsorption for 9 minutes, and clean air was discharged. The methylene chloride concentration of the clean air at that time was 20 ppm or less, and the treatment was performed with a removal rate of 99% or more. dichloromethane, the air blown to the adsorption tank 13 was blocked with an automatic damper, and then the desorption steam 15 was jetted onto the activated carbon fiber of the adsorption tank. Simultaneously with this treatment, the automatic damper of another adsorption tank was opened, and this time the adsorption treatment of methylene chloride gas was performed in this adsorption tank. This adsorption and desorption operation was repeated. Simultaneously with this treatment, the automatic damper of another adsorption tank was opened, and this time the adsorption treatment of methylene chloride gas was performed in this adsorption tank. This adsorption and desorption operation was repeated.

有機溶剤回収処理装置10から得られた有機溶剤含有水蒸気17を、溶剤分離装置20に送りコンデンサー21で冷却し、塩化メチレン主体の回収有機溶剤23と塩化メチレンが微量に含まれた分離排水22を得た。回収有機溶剤中の塩化メチレン濃度は99.5重量%、酢酸濃度は2500ppmであった。   The organic solvent-containing water vapor 17 obtained from the organic solvent recovery treatment device 10 is sent to the solvent separation device 20 and cooled by the condenser 21, and the recovered organic solvent 23 mainly composed of methylene chloride and the separated waste water 22 containing a small amount of methylene chloride are obtained. Obtained. The methylene chloride concentration in the recovered organic solvent was 99.5% by weight, and the acetic acid concentration was 2500 ppm.

前記回収有機溶剤を、平均粒形1.5mmの寒水石(新見化学工業株式会社製)の吸着剤を重量1000g充填させた酸成分除去用溶剤精製装置40に導入した。その際の出口酢酸濃度の経時変化を確認した結果、SV=10(1/h)のとき出口酢酸濃度は250ppm以下を示した。   The recovered organic solvent was introduced into an acid component removing solvent refining apparatus 40 filled with 1000 g of an adsorbent of cold water stone (manufactured by Niimi Chemical Industry Co., Ltd.) having an average particle size of 1.5 mm. As a result of confirming the change with time in the outlet acetic acid concentration, the outlet acetic acid concentration was 250 ppm or less when SV = 10 (1 / h).

本実施例の有機溶剤含有ガス処理システムは、100時間後でも有機溶剤回収装置の除去率、溶剤精製装置の性能共に90〜99%の効率で処理が可能であった。   The organic solvent-containing gas treatment system of this example was capable of treating with an efficiency of 90 to 99% in both the removal rate of the organic solvent recovery device and the performance of the solvent purification device even after 100 hours.

本発明の有機溶剤含有ガス処理システムは、有機溶剤回収処理装置から回収される有機溶剤の簡便且つ高効率な精製、排出される分離排水の連続浄化、並びに排水の冷却水化による無排水システムを実現した。多量有害有機物質を高効率且つ安定に除去することができる処理装置であるため、設備増大を必要とせずに、コスト低減でき、有害物質安定除去でき、特に研究所や工場等の幅広い分野に利用することができ、産業界に寄与するところ大である。   The organic solvent-containing gas treatment system of the present invention includes a simple and highly efficient purification of an organic solvent recovered from an organic solvent recovery treatment device, continuous purification of discharged separated waste water, and a non-drainage system by cooling the waste water. It was realized. Because it is a processing device that can remove large amounts of harmful organic substances with high efficiency and stability, it can reduce costs without the need for additional equipment, and can stably remove harmful substances, especially in a wide range of fields such as laboratories and factories. It is a great place to contribute to the industry.

本発明の好ましい形態の例である有機溶剤含有ガス処理システムである。 It is an organic-solvent containing gas processing system which is an example of the preferable form of this invention. 本発明の好ましい形態の例である有機溶剤含有ガス処理システムである。 It is an organic-solvent containing gas processing system which is an example of the preferable form of this invention. 有機溶剤濃縮処理システムの一例である。 It is an example of the organic solvent concentration processing system.

符号の説明Explanation of symbols

10 有機溶剤回収処理装置
11 被処理ガス
12 吸着送風機
13 吸着槽
14 吸着材(活性炭素繊維)
15 脱着用スチーム 16 処理出口 17 有機溶剤含有水蒸気 20 溶剤分離装置 21 コンデンサー 22 分離水 23 回収有機溶剤 31 曝気槽 32 中和槽 33 クーリングタワー 34 戻りガス導入ライン 35 コンデンサー導入ライン 36 コンデンサー排出ライン 40 酸成分除去用溶剤精製装置 50 水分除去用吸脱着式溶剤精製装置 51 被処理有機回収溶剤タンク 52 水分吸着塔 53 回収有機溶剤タンク 54 パージ用水タンク 55 水用ポンプ 56 コンプレッサー 57 戻りライン 58 パージ水曝気槽導入ライン 60 吸脱着式有機溶剤含有水処理装置 61 吸着材(活性炭素繊維) 15 Detachable steam 16 Treatment outlet 17 Organic solvent-containing steam 20 Solvent separator 21 Condenser 22 Separation water 23 Recovered organic solvent 31 Air exposure tank 32 Neutralization tank 33 Cooling tower 34 Return gas introduction line 35 Condenser introduction line 36 Condenser discharge line 40 Acid component Solvent purification device for removal 50 Absorption-removable solvent purification device for water removal 51 Organic recovery solvent tank to be treated 52 Moisture adsorption tower 53 Recovery organic solvent tank 54 Purge water tank 55 Water pump 56 Compressor 57 Return line 58 Purge water exposure tank introduction Line 60 Adsorption type organic solvent-containing water treatment device 61 Adsorbent (activated carbon fiber)
62 脱着ガス供給送風機 63 脱着ガス用ヒーター 64 パージ空気供給送風機 65 戻り水ライン 66 戻りガスライン 90 有機溶剤含有ガス濃縮処理装置 91 回転可能な円筒形のケース 92 VOC含有ガス供給管 93 吸着部 94 浄化空気送出管 95 吸着剤 96 回転中心軸 97 脱着部 98 脱着用空気供給管DESCRIPTION OF SYMBOLS 10 Organic solvent collection | recovery processing apparatus 11 Gas to be processed 12 Adsorption fan 13 Adsorption tank 14 Adsorbent (activated carbon fiber) 62 Desorption gas supply blower 63 Desorption gas heater 64 Purge air supply blower 65 Return water line 66 Return gas line 90 Organic solvent-containing gas concentrator 91 Rotatable cylindrical case 92 VOC-containing gas supply pipe 93 Adsorption part 94 Purification Air delivery pipe 95 Adsorbent 96 Rotation center axis 97 Desorption part 98 Desorption air supply pipe DECRIPTION OF SYMBOLS 10 Organic solvent collection | recovery processing apparatus 11 Gas to be processed 12 Adsorption fan 13 Adsorption tank 14 Adsorbent (activated carbon fiber)
DESCRIPTION OF SYMBOLS 15 Desorption steam 16 Process outlet 17 Organic solvent containing water vapor | steam 20 Solvent separation apparatus 21 Condenser 22 Separation water 23 Collect | recovered organic solvent 31 Aeration tank 32 Neutralization tank 33 Cooling tower 34 Return gas introduction line 35 Condenser introduction line 36 Condenser discharge line 40 Acid component Removal solvent refining equipment 50 Water removal adsorption / desorption type solvent refining equipment 51 Organic recovery solvent tank to be treated 52 Water adsorption tower 53 Recovered organic solvent tank 54 Purge water tank 55 Water pump 56 Compressor 57 Return line 58 Introduction of purge water aeration tank Line 60 Adsorption / desorption type organic solvent-containing water treatment device 61 Adsorbent (activated carbon fiber) DESCRIPTION OF SYMBOLS 15 Desorption steam 16 Process outlet 17 Organic solvent containing water vapor | steam 20 Solvent separation apparatus 21 Condenser 22 Separation water 23 Collect | recovered organic solvent 31 Aeration tank 32 Neutralization tank 33 Cooling tower 34 Return gas introduction line 35 Condenser introduction line 36 Condenser discharge line 40 Acid component Removal solvent refining equipment 50 Water removal adsorption / desorption type solvent refining equipment 51 Organic recovery solvent tank to be treated 52 Water adsorption tower 53 Recovered organic solvent tank 54 Purge water tank 55 Water pump 56 Compressor 57 Return line 58 Introduction of purge water aeration tank Line 60 Adsorption / desorption type organic solvent-containing water treatment device 61 Adsorbent (activated carbon fiber)
62 Desorption gas supply blower 63 Desorption gas heater 64 Purge air supply blower 65 Return water line 66 Return gas line 90 Organic solvent-containing gas concentration treatment device 91 Rotating cylindrical case 92 VOC-containing gas supply pipe 93 Adsorption part 94 Purification Air delivery pipe 95 Adsorbent 96 Rotation center shaft 97 Desorption part 98 Desorption air supply pipe 62 Desorption gas supply blower 63 Desorption gas heater 64 Purge air supply blower 65 Return water line 66 Return gas line 90 Organic solvent-containing gas concentration treatment device 91 Rotating cylindrical case 92 VOC-containing gas supply pipe 93 Adsorption part 94 Purification Air delivery pipe 95 Adsorbent 96 Rotation center shaft 97 Desorption part 98 Desorption air supply pipe

Claims (9)

  1. 吸着材を充填した吸着槽を備えた有機溶剤回収処理装置に、有機溶剤を含有する被処理ガスを導入し、有機溶剤を該吸着槽で吸着処理して有機溶剤濃度が減少した処理済みガスを排出し、該吸着槽における吸着処理が完了した後に、前記有機溶剤回収処理装置の吸着槽へスチームを導入し、吸着材から有機溶剤を脱着し、それによって吸着材を再生し、再生の際に発生する有機溶剤含有水蒸気を凝縮、分離する溶剤分離装置に導入し、有機溶剤を分離して回収する有機溶剤回収システムと、
    酸成分除去剤を充填させた吸着槽を有する酸成分除去用溶剤精製装置に、該有機溶剤回収処理装置によって分離した回収有機溶剤を導入し、該回収有機溶剤を該酸成分除去用溶剤精製装置で吸着処理して有機溶剤中の酸成分の濃度が減少した処理済み有機溶剤を排出する酸成分除去用溶剤精製装置を備えた有機溶剤含有ガス処理システム。 A recovered organic solvent separated by the organic solvent recovery treatment device is introduced into an acid component removing solvent purification device having an adsorption tank filled with an acid component removing agent, and the recovered organic solvent is used as the acid component removing solvent purification device. An organic solvent-containing gas treatment system equipped with a solvent purification device for removing acid components that discharges a treated organic solvent whose concentration of acid components in the organic solvent has been reduced by adsorption treatment. A gas to be treated containing an organic solvent is introduced into an organic solvent recovery treatment apparatus equipped with an adsorption tank filled with an adsorbent, and the treated gas having a reduced organic solvent concentration is obtained by adsorbing the organic solvent in the adsorption tank. After the discharge and the adsorption treatment in the adsorption tank are completed, steam is introduced into the adsorption tank of the organic solvent recovery treatment device, the organic solvent is desorbed from the adsorbent, thereby regenerating the adsorbent, and at the time of regeneration An organic solvent recovery system for separating and recovering the organic solvent by introducing it into a solvent separator for condensing and separating the generated organic solvent-containing water vapor; A gas to be treated containing an organic solvent is introduced into an organic solvent recovery treatment apparatus equipped with an adsorption tank filled with an adsorbent, and the treated gas having a reduced organic solvent concentration is obtained by adsorbing the organic solvent in the adsorption tank. After the discharge and the adsorption treatment in the adsorption tank are completed, steam is introduced into the adsorption tank of the organic solvent recovery treatment device, the organic solvent is desorbed from the adsorbent, thereby regenerating the adsorbent, and at the time of regeneration An organic solvent recovery system for separating and recovering the organic solvent by introducing it into a solvent separator for condensing and separating the generated organic solvent-containing water vapor;
    The recovered organic solvent separated by the organic solvent recovery treatment device is introduced into an acid component removal solvent purification device having an adsorption tank filled with an acid component removal agent, and the recovered organic solvent is removed from the acid component removal solvent purification device. An organic solvent-containing gas treatment system equipped with an acid component removal solvent refining device that discharges the treated organic solvent in which the concentration of the acid component in the organic solvent has been reduced by adsorption treatment with an acid. The recovered organic solvent separated by the organic solvent recovery treatment device is introduced into an acid component removal solvent purification device having an adsorption tank filled with an acid component removal agent, and the recovered organic solvent is removed from the acid component removal solvent purification device. An organic solvent-containing gas treatment system equipped with an acid component removal solvent refining device that discharges the treated organic solvent in which the concentration of the acid component in the organic solvent has been reduced by adsorption treatment with an acid.
  2. 酸成分除去用溶剤精製装置において、酸成分除去剤が塩化マグネシウム、塩化カリウム、塩化カルシウム、塩化バリウム、炭酸マグネシウム、炭酸カリウム、炭酸カルシウム、炭酸バリウム等の内で1種類、または2種類以上を組み合わせたもので構成されている請求項1に記載の有機溶剤含有ガス処理システム。   In the solvent refining equipment for acid component removal, the acid component remover is one of magnesium chloride, potassium chloride, calcium chloride, barium chloride, magnesium carbonate, potassium carbonate, calcium carbonate, barium carbonate, or a combination of two or more. The organic-solvent containing gas processing system of Claim 1 comprised by the thing.
  3. 有機溶剤回収システムと、
    該有機溶剤回収システムで回収した回収有機溶剤から酸成分を除去する酸成分除去用溶剤精製装置と、
    該酸成分除去用溶剤精製装置で酸成分を除去した回収有機溶剤から水分を除去する水分除去用溶剤精製装置を備えた請求項1または2に記載の有機溶剤含有ガス処理システム。
    An organic solvent recovery system;
    A solvent refining device for removing an acid component from the recovered organic solvent recovered by the organic solvent recovery system;
    The organic solvent-containing gas treatment system according to claim 1 or 2, further comprising a water removal solvent purification device that removes water from the recovered organic solvent from which the acid component has been removed by the acid component removal solvent purification device.
  4. 水分除去用溶剤精製装置が、水分を含有する有機溶剤を吸着材に通流させて該吸着材に水分を吸着させる吸着工程と、該吸着材に乾燥空気を通流させて該吸着材に吸着された水分を脱着する脱着工程の間に、水の通流により吸着材に付着した有機溶剤を除去するパージ工程を有する水分除去用溶剤精製装置である請求項3に記載の有機溶剤含有ガス処理システム。   A solvent purifier for removing moisture passes an adsorption process in which an organic solvent containing moisture is passed through the adsorbent to adsorb moisture onto the adsorbent, and adsorbs the adsorbent by passing dry air through the adsorbent. The organic solvent-containing gas treatment according to claim 3, wherein the organic solvent-containing gas treatment device has a purging step for removing the organic solvent adhering to the adsorbent by flowing water during the desorption step of desorbing the dehydrated water. system.
  5. 水分除去用溶剤精製装置において、パージ工程で排出された有機溶剤含有パージ水を曝気槽の入口に導入するラインを備える請求項3または4に記載の有機溶剤含有ガス処理システム。   5. The organic solvent-containing gas processing system according to claim 3, further comprising a line for introducing the organic solvent-containing purge water discharged in the purge step into an inlet of the aeration tank in the solvent purification apparatus for removing water.
  6. 有機溶剤を分離・回収する有機溶剤回収システムにおける溶剤分離装置により分離し排出される排水をクーリングタワーに導入し、クーリングタワーから該溶剤分離装置におけるコンデンサーに冷却水を導入し、使用した冷却水をクーリングタワーに戻すラインを備える請求項1〜5のいずれかに記載の有機溶剤含有ガス処理システム。   Wastewater separated and discharged by the solvent separator in the organic solvent recovery system that separates and recovers the organic solvent is introduced into the cooling tower, cooling water is introduced from the cooling tower to the condenser in the solvent separator, and the used cooling water is supplied to the cooling tower. The organic solvent containing gas processing system in any one of Claims 1-5 provided with the return line.
  7. 有機溶剤を分離・回収する有機溶剤回収システムにおける溶剤分離装置から排出された排水中の有機溶剤成分を除去する水処理手段として、排水中の有機溶剤を揮発除去する曝気槽および/または排水中の有機溶剤を含有する水を吸着素子に通流させて該吸着素子に有機溶剤を吸着させる吸着工程と、該吸着素子に高温の加熱ガスを通気させて該吸着素子に吸着された有機溶剤を脱着する脱着工程とを交互に行う吸脱着式水処理装置を、有機溶剤を分離・回収する有機溶剤回収システムにおける該溶剤分離装置から排出された排水をクーリングタワーに導入する前に備える請求項6に記載の有機溶剤含有ガス処理システム。   As a water treatment means to remove the organic solvent components in the wastewater discharged from the solvent separator in the organic solvent recovery system that separates and recovers the organic solvent, an aeration tank that volatilizes and removes the organic solvent in the wastewater and / or An adsorption process in which water containing an organic solvent is passed through the adsorption element to adsorb the organic solvent in the adsorption element, and a high-temperature heated gas is passed through the adsorption element to desorb the organic solvent adsorbed on the adsorption element. 7. The adsorption / desorption type water treatment device that alternately performs the desorption step is provided before the waste water discharged from the solvent separation device in the organic solvent recovery system for separating and recovering the organic solvent is introduced into the cooling tower. Organic solvent containing gas treatment system.
  8. 水処理手段が、前段が曝気槽、後段が吸脱着式水処理装置であり、水処理手段により排水中から除去した有機溶剤ガスを、有機溶剤回収装置の入口に戻すラインを備える請求項7に記載の有機溶剤含有ガス処理システム。   The water treatment means comprises an aeration tank at the front stage and an adsorption / desorption type water treatment apparatus at the rear stage, and a line for returning the organic solvent gas removed from the waste water by the water treatment means to the inlet of the organic solvent recovery apparatus. The organic solvent containing gas processing system of description.
  9. 水処理手段の後段にpH を調整するための中和槽を備える請求項7または8に記載の有機溶剤含有ガス処理システム。   The organic solvent-containing gas treatment system according to claim 7 or 8, further comprising a neutralization tank for adjusting the pH after the water treatment means.
JP2008329582A 2008-12-25 2008-12-25 Organic solvent-containing gas treating system Pending JP2010149040A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP2008329582A JP2010149040A (en) 2008-12-25 2008-12-25 Organic solvent-containing gas treating system

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP2008329582A JP2010149040A (en) 2008-12-25 2008-12-25 Organic solvent-containing gas treating system

Publications (1)

Publication Number Publication Date
JP2010149040A true JP2010149040A (en) 2010-07-08

Family

ID=42568744

Family Applications (1)

Application Number Title Priority Date Filing Date
JP2008329582A Pending JP2010149040A (en) 2008-12-25 2008-12-25 Organic solvent-containing gas treating system

Country Status (1)

Country Link
JP (1) JP2010149040A (en)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012020755A1 (en) * 2010-08-11 2012-02-16 東洋紡績株式会社 Waste water treatment system
JP2012040534A (en) * 2010-08-23 2012-03-01 Toyobo Co Ltd Wastewater treatment system
JP2012040479A (en) * 2010-08-17 2012-03-01 Toyobo Co Ltd Wastewater treatment system
JP2012055822A (en) * 2010-09-08 2012-03-22 Toyobo Co Ltd System for treating organic solvent-containing gas
JP2013158666A (en) * 2012-02-02 2013-08-19 Toyobo Co Ltd Organic solvent recovery system
JP2014012246A (en) * 2012-07-04 2014-01-23 Toyobo Co Ltd Wastewater treatment system
CN105797421A (en) * 2016-04-15 2016-07-27 淮安市春光机械有限公司 Torch waste gas recycling device
WO2018179864A1 (en) * 2017-03-29 2018-10-04 富士フイルム株式会社 Gas-adsorbing material, method for producing same, and packaging material

Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS52117883A (en) * 1976-03-30 1977-10-03 Matsushita Electric Ind Co Ltd Device for absorbing and recovering organic solvents
JPS5620632U (en) * 1979-07-25 1981-02-24
JPS62443A (en) * 1985-06-25 1987-01-06 Mitsubishi Heavy Ind Ltd Recovery of purifying solvent
JPS62501615A (en) * 1984-12-20 1987-07-02
JPS6394528U (en) * 1986-12-08 1988-06-18
JPH05220303A (en) * 1992-02-13 1993-08-31 Central Glass Co Ltd Equipment for adsorptive separation of water and acid content in organic solvent
JPH0671167A (en) * 1992-08-28 1994-03-15 Murakashi Sekkai Kogyo Kk Adsorbent
JPH1133304A (en) * 1997-07-17 1999-02-09 Komatsu Ltd Method and apparatus for separating and recovering hydrophilic solvent
JP2004276021A (en) * 2003-02-25 2004-10-07 Tamuraya:Kk Method and apparatus for treating waste water
JP2006055712A (en) * 2004-08-18 2006-03-02 Toyobo Co Ltd Water treatment apparatus
JP2008237988A (en) * 2007-03-26 2008-10-09 Toyobo Co Ltd Regeneration method of organic solvent
JP2008237989A (en) * 2007-03-26 2008-10-09 Toyobo Co Ltd Organic solvent treatment apparatus
JP2010029739A (en) * 2008-06-25 2010-02-12 Toyobo Co Ltd Organic solvent-containing gas treatment system

Patent Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS52117883A (en) * 1976-03-30 1977-10-03 Matsushita Electric Ind Co Ltd Device for absorbing and recovering organic solvents
JPS5620632U (en) * 1979-07-25 1981-02-24
JPS62501615A (en) * 1984-12-20 1987-07-02
JPS62443A (en) * 1985-06-25 1987-01-06 Mitsubishi Heavy Ind Ltd Recovery of purifying solvent
JPS6394528U (en) * 1986-12-08 1988-06-18
JPH05220303A (en) * 1992-02-13 1993-08-31 Central Glass Co Ltd Equipment for adsorptive separation of water and acid content in organic solvent
JPH0671167A (en) * 1992-08-28 1994-03-15 Murakashi Sekkai Kogyo Kk Adsorbent
JPH1133304A (en) * 1997-07-17 1999-02-09 Komatsu Ltd Method and apparatus for separating and recovering hydrophilic solvent
JP2004276021A (en) * 2003-02-25 2004-10-07 Tamuraya:Kk Method and apparatus for treating waste water
JP2006055712A (en) * 2004-08-18 2006-03-02 Toyobo Co Ltd Water treatment apparatus
JP2008237988A (en) * 2007-03-26 2008-10-09 Toyobo Co Ltd Regeneration method of organic solvent
JP2008237989A (en) * 2007-03-26 2008-10-09 Toyobo Co Ltd Organic solvent treatment apparatus
JP2010029739A (en) * 2008-06-25 2010-02-12 Toyobo Co Ltd Organic solvent-containing gas treatment system

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012020755A1 (en) * 2010-08-11 2012-02-16 東洋紡績株式会社 Waste water treatment system
CN104649448A (en) * 2010-08-11 2015-05-27 东洋纺株式会社 Waste water treatment system
CN103068740A (en) * 2010-08-11 2013-04-24 东洋纺株式会社 Waste water treatment system
JP2012040479A (en) * 2010-08-17 2012-03-01 Toyobo Co Ltd Wastewater treatment system
JP2012040534A (en) * 2010-08-23 2012-03-01 Toyobo Co Ltd Wastewater treatment system
JP2012055822A (en) * 2010-09-08 2012-03-22 Toyobo Co Ltd System for treating organic solvent-containing gas
JP2013158666A (en) * 2012-02-02 2013-08-19 Toyobo Co Ltd Organic solvent recovery system
JP2014012246A (en) * 2012-07-04 2014-01-23 Toyobo Co Ltd Wastewater treatment system
CN105797421A (en) * 2016-04-15 2016-07-27 淮安市春光机械有限公司 Torch waste gas recycling device
CN105797421B (en) * 2016-04-15 2018-01-30 淮安市春光机械有限公司 Torch device for recycling exhaust gas
WO2018179864A1 (en) * 2017-03-29 2018-10-04 富士フイルム株式会社 Gas-adsorbing material, method for producing same, and packaging material

Similar Documents

Publication Publication Date Title
US9969638B2 (en) Water treatment systems and associated methods
US6929680B2 (en) CO2 separator method and apparatus
US5409522A (en) Mercury removal apparatus and method
US4775484A (en) Method and apparatus for the continuous separation of contaminants from a fluid mixture
US5122165A (en) Removal of volatile compounds and surfactants from liquid
US5531902A (en) Method for water remediation
US4421532A (en) Process for removing and recovering volatile organic substances from industrial waste gases
CN105664883B (en) System and method for gas treatment
AU2008348658B2 (en) Fuel cleaning for gas fired engines
US6296823B1 (en) Method and installation for eliminating gaseous organic substances in the air
EP2134446B1 (en) Biogas upgrading
KR100266344B1 (en) How to recover volatile organics
JP2009061450A (en) Method for removing mercury from flue gas after combustion
US5176798A (en) System for removal and disposal of minor amounts of organics from contaminated water
CA2865871C (en) Method of treatment of amine waste water and a system for accomplishing the same
US6117328A (en) Adsorbent-filled membranes for pervaporation
CN102458610A (en) Method for reclaiming of co2 absorbent and a reclaimer
US20040187685A1 (en) Method of and apparatus for regenerating adsorbent
TW200808432A (en) Ozone production processes and its use in industrial processes
EP2931663B1 (en) Counterflow adsorption filter column for water treatment
US5472613A (en) Removing volatile and non-volatile organic in a thick film equilibrium process and device
CN101362076B (en) Regeneration method of active carbon absorbent
KR20090113360A (en) Method and apparatus for the recovery and re-use of process gases
TWI519469B (en) Recovery of xe and other high value compounds
US8460434B2 (en) Methane recovery from a landfill gas

Legal Events

Date Code Title Description
A621 Written request for application examination

Free format text: JAPANESE INTERMEDIATE CODE: A621

Effective date: 20111128

A977 Report on retrieval

Free format text: JAPANESE INTERMEDIATE CODE: A971007

Effective date: 20120625

A131 Notification of reasons for refusal

Free format text: JAPANESE INTERMEDIATE CODE: A131

Effective date: 20120724

A02 Decision of refusal

Free format text: JAPANESE INTERMEDIATE CODE: A02

Effective date: 20121120