JP2009273975A - System for treatment of gas containing organic solvent - Google Patents
System for treatment of gas containing organic solvent Download PDFInfo
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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 for recovering an organic solvent from a gas to be treated containing an organic solvent and treating the separated waste water, and particularly an industry containing an organic solvent discharged from various factories, research facilities, etc. The present invention relates to an organic solvent-containing gas treatment system used for exhaust gas purification.
従来、有機溶剤含有ガス処理システムにおける有機溶剤吸脱着装置としては、活性炭素材で被処理ガスの有機溶剤を吸着する１対の吸着槽と、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。 Conventionally, as an organic solvent adsorption / desorption device in an organic solvent-containing gas treatment system, a pair of adsorption tanks for adsorbing an organic solvent of a gas to be treated with an activated carbon material, gas treatment means for each adsorption tank, and desorption gas supply And a switching means for switching between an adsorption processing apparatus for supplying the gas to be processed to the adsorption tank and a desorption processing state for supplying the desorption gas.
また、上記の有機溶剤吸脱着装置の吸着材は、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。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提案されている（例えば、特許文献１〜５参照）。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装置から構成されている。 Moreover, granular activated carbon, activated carbon fiber, zeolite, silica gel, or the like is used as the adsorbent for the organic solvent adsorption / desorption device. 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. For example, an apparatus in which activated carbon fibers are fixed to a support or configured in a cylindrical shape by self-supporting and arranged in a vertical mold in a core material has been proposed (see, for example, Patent Documents 1 to 5). . 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 separation device and 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が（例えば特許文献６参照）、最終的には排水を河川等に放流する必要があった。 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 6), but finally it was necessary to discharge the wastewater to a river etc. .
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排出される排水を河川等環境中に排出しない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。 The present invention has been made against the background of the problems of the prior art, and it is an object of the present invention to provide an organic solvent-containing gas treatment system that does not discharge wastewater separated and discharged from an organic solvent recovery device into an environment such as a river. It is.
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。 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．吸着材を充填した吸着槽を備えた有機溶剤吸脱着装置に、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、前記有機溶剤吸脱着装置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する有機溶剤吸脱着装置と、有機溶剤吸脱着装置における吸着材の再生の際に発生する有機溶剤含有水蒸気を液化し、分離排水と有機溶剤に分離し、有機溶剤を回収する有機溶剤分離装置とからなる有機溶剤回収装置と、
該有機溶剤回収装置における有機溶剤分離装置により分離し排出される分離排水をクーリングタワーに導入し、該排水を冷却水として再利用する有機溶剤含有ガス処理システム。
1. A gas to be treated containing an organic solvent is introduced into an organic solvent adsorption / desorption device equipped with an adsorption tank filled with an adsorbent, and an organic solvent is adsorbed in the adsorption tank to produce a treated gas whose organic solvent concentration has been reduced. And after completion of the adsorption treatment in the adsorption tank, steam is introduced into the organic solvent adsorption / desorption device, the organic solvent is desorbed from the adsorbent, and thereby the organic solvent adsorption / desorption device that regenerates the adsorbent, and organic An organic solvent recovery device comprising an organic solvent separation device that liquefies organic solvent-containing water vapor generated during regeneration of the adsorbent in the solvent adsorption / desorption device, separates it into separated waste water and an organic solvent, and recovers the organic solvent;
An organic solvent-containing gas treatment system for introducing separated waste water separated and discharged by an organic solvent separation device in the organic solvent recovery device into a cooling tower and reusing the waste water as cooling water.
２．有機溶剤分離装置から排出された分離排水をクーリングタワーに導入する前に、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を備えた上記１に記載の有機溶剤含有ガス処理システム。 2. 2. The above-mentioned 1 equipped with an aeration tank that volatilizes and removes the organic solvent in the wastewater as a water treatment means for removing the organic solvent component in the wastewater before introducing the separated wastewater discharged from the organic solvent separator into the cooling tower. Organic solvent containing gas treatment system.
３．有機溶剤分離装置から排出された分離排水をクーリングタワーに導入する前に、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である上記１に記載の有機溶剤含有ガス処理システム。 3. Before introducing the separated waste water discharged from the organic solvent separator into the cooling tower, water containing the organic solvent in the waste water is passed through the adsorption element as a water treatment means for removing the organic solvent component in the waste water. An adsorption / desorption type water treatment apparatus that alternately performs an adsorption step of adsorbing an organic solvent on the adsorption element and a desorption step of desorbing the organic solvent adsorbed on the adsorption element by passing a high-temperature heated gas through the adsorption element. 2. The organic solvent-containing gas treatment system according to 1 above.
４．有機溶剤分離装置から排出された分離排水をクーリングタワーに導入する前に、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の下流に、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備える上記１に記載の有機溶剤含有ガス処理システム。 4). Before introducing the separated effluent discharged from the organic solvent separator into the cooling tower, as a water treatment means to remove the organic solvent component in the effluent, the wastewater in the effluent is removed downstream of the aeration tank that volatilizes and removes the organic solvent in the effluent. 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. 2. The organic solvent-containing gas treatment system according to 1 above, comprising an adsorption / desorption type water treatment device that alternately performs the desorption step.
５．前記水処理手段において、排水中から除去した有機溶剤ガスを該有機溶剤吸脱着装置の入口に戻すラインを備える上記２〜４のいずれか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 any one of 2 to 4, wherein the water treatment means includes a line for returning the organic solvent gas removed from the waste water to the inlet of the organic solvent adsorption / desorption device.
６．前記水処理手段の下流にｐＨ を調整するための中和槽を備える上記２〜５のいずれかに記載の有機溶剤含有ガス処理システム。
6). 6. The organic solvent-containing gas treatment system according to any one of 2 to 5 above, further comprising a neutralization tank for adjusting pH downstream of 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、有機溶剤回収装置から分離排出される有機溶剤含有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有機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。 The organic solvent-containing gas treatment system according to the present invention not only realizes a system that does not discharge wastewater by introducing organic solvent-containing wastewater separated and discharged from the organic solvent recovery device into the cooling tower, but also contains organic solvent. There is an advantage that the cooling water required for the condenser of the organic solvent separator for condensing 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。被処理ガス１１を吸着送風機１２にて有機溶剤吸脱着装置１０に導入する。導入された被処理ガスは吸着槽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から清浄空気１６として排出される。
一方で、脱着用スチーム１５により脱着された有機溶剤含有水蒸気１７は、有機溶剤分離装置２０に送られコンデンサー２１で液化され分離排水２２と回収液（有機溶剤）２３に分離される。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、揮発除去後の排水は中和槽３２に導入されて中和し、最後にクーリングタワー３３に導入され、排水から冷却水を製造し、冷却水導入ライン３５を通してコンデンサー２１に冷却水を導入する。
さらに、曝気槽から揮発した有機溶剤含有空気を戻りガスライン３４を通じて有機溶剤吸脱着装置１０の入口である被処理ガス１１に戻すシステムである。
Two examples of the embodiment of the present invention will be described. First, a description will be given with reference to FIG. The gas 11 to be treated is introduced into the organic solvent adsorption / desorption device 10 by the adsorption blower 12. The introduced gas 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 16 from the treatment outlet.
On the other hand, the organic solvent-containing water vapor 17 desorbed by the desorption steam 15 is sent to the organic solvent separation device 20 and liquefied by the condenser 21 and separated into the separated waste water 22 and the recovered liquid (organic solvent) 23. The separated waste water 22 containing the separated organic solvent is introduced into the aeration tank 31 to volatilize and remove the organic solvent, and the waste water after the volatilization removal is introduced into the neutralization tank 32 for neutralization, and finally to the cooling tower 33. Then, the cooling water is produced from the waste water, and the cooling water is introduced into the condenser 21 through the cooling water introduction line 35.
Further, the organic solvent-containing air volatilized from the aeration tank is returned to the gas 11 to be treated which is the inlet of the organic solvent adsorption / desorption device 10 through the return gas line 34.
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にて有機溶剤吸脱着装置１０に導入する。導入された被処理ガスは吸着槽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から清浄空気１６として排出される。
一方で、脱着用スチーム１５により脱着された有機溶剤含有水蒸気１７は、有機溶剤分離装置２０に送られコンデンサー２１で液化され分離排水２２と回収液（有機溶剤）２３に分離される。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する。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４０に導入され、吸着材４１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冷却水導入ライン３５を通じて有機溶剤分離装置２０におけるコンデンサー２１に供給する。
他方、パージ空気供給送風機４４で空気を供給して、吸着後の吸着材４１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を通じて吸着材４１の入口に戻す。パージ処理後に脱着ガス供給送風機４２と脱着ガス用ヒーター４３にて加熱空気で脱着する。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４０で脱着された有機溶剤含有空気は戻りガスラインを通じて有機溶剤吸脱着装置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 11 to be treated is introduced into the organic solvent adsorption / desorption device 10 by the adsorption blower 12. The introduced gas 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 16 from the treatment outlet.
On the other hand, the organic solvent-containing water vapor 17 desorbed by the desorption steam 15 is sent to the organic solvent separation device 20 and liquefied by the condenser 21 and separated into the separated waste water 22 and the recovered liquid (organic solvent) 23. The separated waste water 22 containing the separated organic solvent is introduced into the aeration tank 31 to volatilize and remove the organic solvent. The wastewater after treatment in the aeration tank 31 is introduced into an adsorption / desorption type organic solvent-containing water treatment apparatus 40, introduced into the adsorbent 41 and adsorbed and removed, and the treated wastewater is introduced into the neutralization tank 32 for neutralization. It is introduced into the rear cooling tower 33. The cooling water produced from the waste water in the cooling tower is supplied to the condenser 21 in the organic solvent separator 20 through the cooling water introduction line 35.
On the other hand, air is supplied by the purge air supply blower 44 to purge water adhering to the adsorbent 41 after adsorption, and the water is returned to the inlet of the adsorbent 41 through a return water line. After the purge process, the desorption gas supply blower 42 and the desorption gas heater 43 are used for desorption with heated air. The organic solvent-containing air volatilized in the aeration tank 31 and the organic solvent-containing air desorbed by the adsorption / desorption type organic solvent-containing water treatment device 40 are returned to the gas 11 to be treated which is the inlet of the organic solvent adsorption / desorption device 10 through the return gas line. It is a system to return.
本発明にかかる有機溶剤吸脱着装置の吸着材は、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 adsorption / desorption device according to the present invention is not particularly limited, such as granular activated carbon, activated carbon fiber, zeolite, silica gel and the like, 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 by the cooling tower, It is preferable to use for the condenser in an organic-solvent separation apparatus.
本発明にかかる有機溶剤回収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 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. An adsorption / desorption treatment 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より好ましい。 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, 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 device by using a heat exchanger or the like as a heating source of 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、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ためで、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 apparatus include granular activated carbon, zeolite activated carbon, zeolite, silica gel, activated alumina, and the like, but particularly a continuous adsorption / desorption type wastewater treatment apparatus using activated carbon fibers. It is preferable that In other words, activated carbon fibers have a microporous structure on the surface and a fibrous structure, so the contact efficiency with water is high. In particular, the adsorption rate of organic solvents 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.
有機溶剤回収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 wastewater treatment device installed between the organic solvent recovery device and the cooling tower, it is preferable to provide a neutralization tank downstream of the aeration type and / or adsorption / desorption type water treatment device. 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.
前記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吸脱着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, the organic solvent-containing air that has been volatilized or desorbed through the return gas line is preferably returned to the inlet of the organic solvent adsorption / desorption 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、ＰＧＭＥＡ、ＰＧＭＥ、メタノール、エタノール、プロパノール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 treatment system according to the present invention, the organic solvent that can be treated is ethyl acetate, methyl acetate, butyl acetate, methyl ethyl ketone, methyl butyl ketone, heptanone, acetone, toluene, xylene, PGMEA, PGME, methanol, ethanol, propanol, etc. It is not limited, and even a mixture thereof is no exception.
本発明にかかる有機溶剤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、有機溶剤濃縮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、有機溶剤吸脱着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システム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ＶＯＣ含有ガス中の有機溶剤を吸着するための有機溶剤濃縮処理装置５０は、回転中心軸５６まわりに回転可能な円筒形のケース５１を有しており、このケース５１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５５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５５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５３と脱着部５７が区画されており、吸着材５５がそれら吸着部５３と脱着部５７とを交互に通過するようになっている。上記吸着部５３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５２と、濃縮処理装置５０の吸着材５５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５４が設けられている。また、脱着部５７には、ＶＯＣを吸着した吸着材５５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５８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 discharged from the cooling tower in the organic solvent treatment system according to the present invention, when a trace amount of organic solvent is contained, the organic solvent in the air discharged from the cooling tower is concentrated using an organic solvent concentrator, It is preferable to return to the inlet of the organic solvent adsorption / desorption device. FIG. 3 shows the principle of the organic solvent-containing gas concentration treatment system. In the figure, an organic solvent concentration treatment apparatus 50 for adsorbing an organic solvent in a VOC-containing gas having a large air volume and low concentration has a cylindrical case 51 that can rotate around a rotation center axis 56. An adsorbent 55 having a honeycomb structure for adsorbing VOC (with the communication path oriented in the central axis direction) is accommodated in the case 51 to constitute a tubular adsorbent as a whole. For the adsorbent 55, activated carbon fiber, zeolite paper, or the like is appropriately selected according to the components of the VOC-containing gas. An adsorbing portion 53 and a desorbing portion 57 are partitioned on a moving path along which the cylindrical adsorbent rotates, and an adsorbing material 55 passes through the adsorbing portion 53 and the desorbing portion 57 alternately. For example, a VOC-containing gas supply pipe 52 for introducing a VOC-containing gas generated in the factory and a purified air for sending the purified air purified by the adsorbent 55 of the concentration treatment device 50 to the factory. An air delivery pipe 54 is provided. In addition, the desorption part 57 is provided with a desorption air supply pipe 58 for blowing high-temperature dry air at 180 ° C., that is, desorption heating air, to the adsorbent 55 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。
（酢酸エチル、酢酸、エタノール、トルエン溶剤濃度評価）
入口・出口の水濃度をガスクロマトグラフ法により分析し測定した。
（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
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.
(Ethyl acetate, acetic acid, ethanol, toluene solvent concentration evaluation)
The water concentration at the inlet / outlet was analyzed and measured by gas chromatography.
(Exclusion rate)
Removal rate (%) = (device inlet gas concentration−device outlet gas concentration) / device inlet gas concentration × 100
＜実施例１＞
酢酸エチル２０００ｐｐｍ含む４０℃の被処理ガス１１を、有機溶剤吸脱着装置１０に導入した。その際に風量１００Ｎｍ３／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１６５０ｍ２／ｇ、全細孔容積０．６６ｃｍ３／ｇの活性炭素繊維を使用し、９分間吸着を行い、清浄空気１６を排出した。その際の清浄空気１６の酢酸エチル濃度は２０ｐｐｍであり、９９％の除去率で処理できた。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。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。この吸着と脱着の操作を繰り返し実施した。
<Example 1>
A gas to be treated 11 containing 2000 ppm of ethyl acetate at 40 ° C. was introduced into the organic solvent adsorption / desorption apparatus 10. At that time it was blown into the suction tank 13 from the suction blower 12 in air flow 100 Nm 3 / min, an average pore diameter of 17.4A, BET specific surface area of 1650 m 2 / g, total pore volume 0.66 cm 3 as an adsorbent 14 in the adsorption vessel / G of activated carbon fiber was used for adsorption for 9 minutes, and clean air 16 was discharged. At that time, the concentration of ethyl acetate in the clean air 16 was 20 ppm, and could be treated 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 automatic 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.
有機溶剤吸脱着装置１０から得られた有機溶剤含有水蒸気１７を、有機溶剤分離装置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液２３と酢酸エチルが微量に含まれた分離排水２２を得た。分離排水の酢酸エチル濃度は６９００ｐｐｍ、酢酸濃度は２４００ｐｐｍ、エタノール濃度は１９００ｐｐｍで水量は３１０ｋｇ／ｈｒの量であった。 The organic solvent-containing water vapor 17 obtained from the organic solvent adsorption / desorption device 10 is sent to the organic solvent separation device 20 and cooled by the condenser 21, and the recovered liquid 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 separated wastewater was 6900 ppm, the acetic acid concentration was 2400 ppm, the ethanol concentration was 1900 ppm, and the amount of water was 310 kg / hr.
この分離排水２２を曝気槽３１に導入した。曝気槽中の排水は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１５ｐｐｍ、酢酸５０ｐｐｍ、エタノール２５ｐｐｍと除去率９９％以上にて処理できた。また、この際に揮発した溶剤ガスは戻りガスライン３４を通じて有機溶剤吸脱着装置１０の入口である被処理ガス１１に戻した。 This separated waste water 22 was introduced into the aeration tank 31. The waste water in the aeration tank was heated to 70 ° C. and aerated. The concentration of waste water treated in the aeration tank 31 was 15 ppm ethyl acetate, 50 ppm acetic acid, 25 ppm ethanol, and a removal rate of 99% or more. Further, the solvent gas volatilized at this time was returned to the gas 11 to be treated which is the inlet of the organic solvent adsorption / desorption device 10 through the return gas line 34.
次に、曝気槽３１に導入された排水を中和槽３２に導入し、ｐＨを３．５から７まで中和した。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冷却水導入ライン３５より導入した。このとき、コンデンサー２１に必要な冷却水１９ｍ３／ｈｒの内で、補給冷却水として必要な１ｍ３／ｈｒの冷却水の２８％にあたる２８０ｋｇ／ｈｒをクーリングタワーから供給することができた。 Next, the wastewater introduced into the aeration tank 31 was introduced into the neutralization tank 32 to neutralize the pH from 3.5 to 7. Thereafter, waste water was introduced into the cooling tower 33, cooling water was produced from the waste water, and the cooling water produced in the condenser 21 was introduced from the cooling water introduction line 35. In this case, among the cooling water 19 m 3 / hr required to condenser 21, a 280 kg / hr corresponding to 28% of the cooling water of the required 1 m 3 / hr as makeup coolant could be fed 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、水処理装置の除去率共に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 and the removal rate of the water treatment device 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＞
トルエン２５００ｐｐｍ含む３０℃の被処理ガス１１を、有機溶剤吸脱着装置１０に導入した。その際に風量１００Ｎｍ３／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１６５０ｍ２／ｇ、全細孔容積０．６６ｃｍ３／ｇの活性炭素繊維を使用し、８分間吸着を行い、清浄空気１６を排出した。その際の清浄空気１６のトルエン濃度は２５ｐｐｍであり、９９％の除去率で処理できた。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。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トルエンガスの吸着処理を行った。この吸着と脱着の操作を繰り返し実施した。
<Example 2>
A gas to be treated 11 containing 2500 ppm of toluene at 30 ° C. was introduced into the organic solvent adsorption / desorption apparatus 10. At that time it was blown into the suction tank 13 from the suction blower 12 in air flow 100 Nm 3 / min, an average pore diameter of 17.4A, BET specific surface area of 1650 m 2 / g, total pore volume 0.66 cm 3 as an adsorbent 14 in the adsorption vessel / G of activated carbon fiber was used for adsorption for 8 minutes, and clean air 16 was discharged. At that time, the toluene concentration of the clean air 16 was 25 ppm, and could be treated 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 automatic damper of another adsorption tank was opened, and this time the adsorption treatment of toluene gas was performed in this adsorption tank. This adsorption and desorption operation was repeated.
有機溶剤吸脱着装置１０から得られた有機溶剤含有水蒸気１７を、有機溶剤分離装置２０に送りコンデンサー２１で冷却し、トルエン主体の回収液２３とトルエンが微量に含まれた分離排水２２を得た。分離排水の酢酸エチル濃度は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 adsorption / desorption device 10 was sent to the organic solvent separation device 20 and cooled by the condenser 21 to obtain a separation liquid 22 containing a toluene-based recovered liquid 23 and a small amount of toluene. . The ethyl acetate concentration in the separated wastewater was 2000 ppm, and the amount of water was 310 kg / hr.
この分離排水２２を曝気槽３１に導入した。曝気槽中の排水は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トルエン２０ｐｐｍ以下と除去率９９％以上にて処理できた。また、この際に揮発した溶剤ガスは戻りガスライン３４を通じて有機溶剤吸脱着装置１０の入口である被処理ガス１１に戻した。 This separated waste water 22 was introduced into the aeration tank 31. The waste water in the aeration tank was heated to 70 ° C. and aerated. The concentration of the wastewater treated in the aeration tank 31 was 20 ppm or less of toluene and the removal rate was 99% or more. Further, the solvent gas volatilized at this time was returned to the gas 11 to be treated which is the inlet of the organic solvent adsorption / desorption device 10 through the return gas line 34.
次に、曝気槽３１に導入された排水を中和槽３２に導入し、ｐＨを７に中和した。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冷却水導入ライン３５より導入した。このとき、コンデンサー２１に必要な冷却水１９ｍ３／ｈｒの内で、補給冷却水として必要な１ｍ３／ｈｒの冷却水の２８％にあたる２８０ｋｇ／ｈｒをクーリングタワーから供給することができた。 Next, the wastewater introduced into the aeration tank 31 was introduced into the neutralization tank 32 to neutralize the pH to 7. Thereafter, waste water was introduced into the cooling tower 33, cooling water was produced from the waste water, and the cooling water produced in the condenser 21 was introduced from the cooling water introduction line 35. In this case, among the cooling water 19 m 3 / hr required to condenser 21, a 280 kg / hr corresponding to 28% of the cooling water of the required 1 m 3 / hr as makeup coolant could be fed 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、水処理装置の除去率共に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 and the removal rate of the water treatment device 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.
本発明の有機溶剤含有ガス処理システムは、有機溶剤回収装置から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。基本的に吸着材の交換が必要なく、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、吸着材交換作業を省略でき、コスト低減、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、産業界に寄与することが大である。 The organic solvent-containing gas treatment system of the present invention has realized a non-drainage system through continuous purification of separated wastewater discharged from an organic solvent recovery device and cooling of the wastewater. Since it is basically a treatment device that does not require replacement of the adsorbent and can remove a large amount of harmful organic substances with high efficiency and stability, the adsorbent replacement work can be omitted without the need for additional facilities, and the cost can be reduced. It can stably remove harmful substances, and can be used in a wide range of fields such as laboratories and factories, and contributes to the industry.
１０ 有機溶剤吸脱着装置
１１ 被処理ガス
１２ 吸着送風機
１３ 吸着槽
１４ 吸着材
１５ 脱着用スチーム
１６ 清浄空気
１７ 脱着後の有機溶剤含有水蒸気
２０ 有機溶剤分離装置
２１ コンデンサー
２２ 分離排水
２３ 回収液（有機溶剤）
３１ 曝気槽
３２ 中和槽
３３ クーリングタワー
３４ 戻りガスライン
３５ 冷却水導入ライン
３６ 戻り冷却水ライン
４０ 吸脱着式有機溶剤含有排水処理装置
４１ 吸着材
４２ 脱着ガス供給送風機
４３ 脱着ガス用ヒーター
４４ パージ空気供給送風機
４５ 戻り水ライン
５０ 有機溶剤濃縮処理装置
５１ 回転可能な円筒形のケース
５２ ＶＯＣ含有ガス供給管
５３ 吸着部
５４ 浄化空気送出管
５５ 吸着材
５６ 回転中心軸
５７ 脱着部
５８ 脱着用空気供給管
DESCRIPTION OF SYMBOLS 10 Organic solvent adsorption / desorption apparatus 11 Processed gas 12 Adsorption fan 13 Adsorption tank 14 Adsorbent 15 Desorption steam 16 Clean air 17 Organic solvent containing water vapor | steam after desorption 20 Organic solvent separator 21 Capacitor 22 Separation wastewater 23 Recovery liquid (Organic solvent) )
DESCRIPTION OF SYMBOLS 31 Aeration tank 32 Neutralization tank 33 Cooling tower 34 Return gas line 35 Cooling water introduction line 36 Return cooling water line 40 Adsorption / desorption type organic solvent containing waste water treatment equipment 41 Adsorbent 42 Desorption gas supply blower 43 Desorption gas heater 44 Purge air supply Blower 45 Return water line 50 Organic solvent concentration processing device 51 Rotating cylindrical case 52 VOC-containing gas supply pipe 53 Adsorption part 54 Purified air delivery pipe 55 Adsorbent 56 Rotation center shaft 57 Desorption part 58 Desorption air supply pipe
Claims (6)
該有機溶剤回収装置における有機溶剤分離装置により分離し排出される分離排水をクーリングタワーに導入し、該排水を冷却水として再利用する有機溶剤含有ガス処理システム。 A gas to be treated containing an organic solvent is introduced into an organic solvent adsorption / desorption device equipped with an adsorption tank filled with an adsorbent, and an organic solvent is adsorbed in the adsorption tank to produce a treated gas whose organic solvent concentration has been reduced. And after completion of the adsorption treatment in the adsorption tank, steam is introduced into the organic solvent adsorption / desorption device, the organic solvent is desorbed from the adsorbent, and thereby the organic solvent adsorption / desorption device that regenerates the adsorbent, and organic An organic solvent recovery device comprising an organic solvent separation device that liquefies organic solvent-containing water vapor generated during regeneration of the adsorbent in the solvent adsorption / desorption device, separates it into separated waste water and an organic solvent, and recovers the organic solvent;
An organic solvent-containing gas treatment system for introducing separated waste water separated and discharged by an organic solvent separation device in the organic solvent recovery device into a cooling tower and reusing the waste water as cooling water.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7954254B2 (en) * | 2002-05-15 | 2011-06-07 | Nederlandse Organisatie Voor Toegepast-Natuurwetenschappelijk Onderzoek Tno | Method for drying a product using a regenerative adsorbent |
| JP2014012246A (en) * | 2012-07-04 | 2014-01-23 | Toyobo Co Ltd | Wastewater treatment system |
| JP2020505229A (en) * | 2017-01-10 | 2020-02-20 | エマージング・コンパウンズ・トリートメント・テクノロジーズ・インコーポレイテッド | Systems and methods for improving the adsorption of contaminated vapors to increase the capacity of the adsorption media |
| WO2020093584A1 (en) * | 2018-11-06 | 2020-05-14 | 无锡四方集团有限公司 | Process for adsorption treatment of organic waste gas and desorption regeneration of adsorbent |
| WO2020093583A1 (en) * | 2018-11-06 | 2020-05-14 | 无锡四方集团有限公司 | Desorption regeneration process for adsorbent adsorbing organics in water, and tail gas treatment process therefor |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7954254B2 (en) * | 2002-05-15 | 2011-06-07 | Nederlandse Organisatie Voor Toegepast-Natuurwetenschappelijk Onderzoek Tno | Method for drying a product using a regenerative adsorbent |
| JP2014012246A (en) * | 2012-07-04 | 2014-01-23 | Toyobo Co Ltd | Wastewater treatment system |
| JP2020505229A (en) * | 2017-01-10 | 2020-02-20 | エマージング・コンパウンズ・トリートメント・テクノロジーズ・インコーポレイテッド | Systems and methods for improving the adsorption of contaminated vapors to increase the capacity of the adsorption media |
| JP2022037225A (en) * | 2017-01-10 | 2022-03-08 | エマージング・コンパウンズ・トリートメント・テクノロジーズ・インコーポレイテッド | System and method for enhancing adsorption of contaminated vapors to increase treatment capacity of regenerable synthetic adsorptive media |
| JP7100223B2 (en) | 2017-01-10 | 2022-07-13 | エマージング・コンパウンズ・トリートメント・テクノロジーズ・インコーポレイテッド | Systems and methods for improving the adsorption of contaminated vapors to increase the processing capacity of renewable synthetic adsorption media |
| WO2020093584A1 (en) * | 2018-11-06 | 2020-05-14 | 无锡四方集团有限公司 | Process for adsorption treatment of organic waste gas and desorption regeneration of adsorbent |
| WO2020093583A1 (en) * | 2018-11-06 | 2020-05-14 | 无锡四方集团有限公司 | Desorption regeneration process for adsorbent adsorbing organics in water, and tail gas treatment process therefor |
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