JP2018034109A - Organic solvent recovery system - Google Patents
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Abstract
【課題】有機溶剤の分解物の発生を抑制し、純度の高い有機溶剤を回収可能であり、配管の腐食を抑制可能な、有機溶剤回収システムを提供する。【解決手段】本発明の有機溶剤回収システムは、吸着材を充填した処理槽を有し、吸着処理と脱着処理とを交互に繰り返す吸脱着処理装置と、前記脱着ガスを冷却凝縮し、有機溶剤を含む回収液と水を主成分とする分離液とに分離する凝縮分液装置と、分離膜を有し、前記凝縮分液装置から排出された回収液を導入することで、有機溶剤を主成分とする濃縮液と水を主成分とする透過液とに分離する膜分離装置と、前記吸脱着装置から排出された前記脱着ガスが前記凝縮分離装置に導入される前に、当該脱着ガスから潜熱を取り出し蓄熱する蓄熱部と、蓄熱部に蓄熱された熱を前記凝縮分液装置より排出された回収液へ与える熱付与部とを有する熱媒装置と、を備える。【選択図】図１An organic solvent recovery system capable of suppressing generation of decomposition products of an organic solvent, recovering a high purity organic solvent, and suppressing corrosion of piping. An organic solvent recovery system according to the present invention includes a treatment tank filled with an adsorbent, an adsorption / desorption treatment device that alternately repeats adsorption treatment and desorption treatment, cooling and condensing the desorption gas, and organic solvent. A separation liquid separator containing water and a separation liquid containing water as a main component, and a separation membrane, and by introducing the collection liquid discharged from the condensation liquid separation apparatus, the organic solvent is mainly used. A membrane separation device that separates the concentrated liquid as a component into a permeate containing water as a main component, and the desorption gas discharged from the adsorption / desorption device before the desorption gas is introduced into the condensation separation device. A heat storage device that includes a heat storage unit that extracts and stores latent heat and a heat application unit that applies heat stored in the heat storage unit to the recovered liquid discharged from the condensate separator. [Selection] Figure 1
Description
本発明は、有機溶剤含有ガスから有機溶剤を回収し、回収した有機溶剤を精製する有機溶剤回収システムに関する。 The present invention relates to an organic solvent recovery system that recovers an organic solvent from an organic solvent-containing gas and purifies the recovered organic solvent.
従来、有機溶剤含有ガスを清浄化するシステムとして、有機溶剤含有ガスから有機溶剤を除去し、除去した有機溶剤を高濃度に濃縮して回収する有機溶剤回収システムが知られている。この種の有機溶剤回収システムは、一般的に、吸着材として粒状活性炭或いは繊維状活性炭を充填した処理槽へ有機溶剤含有ガスを供給し、吸着材にて吸着させて清浄化した処理済ガスを排出する吸着処理と、処理槽へ水蒸気を導入して吸着材から有機溶剤を脱着する脱着処理とを交互に繰り返す吸脱着処理装置と、吸脱着処理装置より脱着された高濃度の有機溶剤を含む脱着ガスを凝縮させて高濃度の有機溶剤を含む回収液と水を主成分とする分離排水とに分離する凝縮回収装置と、の組み合わせにて構成されている（例えば、特許文献１、２参照）。 2. Description of the Related Art Conventionally, as a system for purifying an organic solvent-containing gas, an organic solvent recovery system that removes an organic solvent from an organic solvent-containing gas and concentrates and recovers the removed organic solvent at a high concentration is known. This type of organic solvent recovery system generally supplies an organic solvent-containing gas to a treatment tank filled with granular activated carbon or fibrous activated carbon as an adsorbent, and adsorbs the cleaned gas that has been cleaned by the adsorbent. Includes an adsorption / desorption treatment device that alternately repeats an adsorption treatment to be discharged and a desorption treatment in which water vapor is introduced into the treatment tank to desorb the organic solvent from the adsorbent, and a high-concentration organic solvent desorbed by the adsorption / desorption treatment device It is composed of a combination of a condensing and collecting device that condenses the desorbed gas and separates it into a recovered liquid containing a high concentration organic solvent and a separated waste water containing water as a main component (see, for example, Patent Documents 1 and 2). ).
上記有機溶剤回収システムにより回収された回収液中には、通常、有機溶剤の他に脱着処理に用いられる水蒸気に由来する水分、および有機溶剤の分解物等が含まれることがある。故に、純度の高い回収液を得る為には、一般的に回収液を蒸留処理によって有機溶剤とその他水分及び分解物とを分離する操作が必要となる。 In general, the recovered liquid recovered by the organic solvent recovery system may contain water derived from water vapor used for the desorption treatment, decomposition products of the organic solvent, and the like in addition to the organic solvent. Therefore, in order to obtain a high-purity recovered liquid, it is generally necessary to perform an operation for separating the recovered liquid from an organic solvent and other moisture and decomposition products by distillation treatment.
しかしながら、蒸留処理においては、蒸留塔等の高額な設備が必要となりイニシャルコストが嵩むばかりでなく、有機溶剤回収システム全体の設置スペースの増大、および莫大なエネルギーを要する為にランニングコストも嵩む。よって、コスト面から好ましいものではない。 However, in the distillation process, expensive equipment such as a distillation column is required, which increases the initial cost, as well as an increase in installation space for the entire organic solvent recovery system and a large amount of energy, which increases the running cost. Therefore, it is not preferable in terms of cost.
このような観点から、蒸留処理に代わる新たな回収液の精製方法として、浸透気化分離法（パーベーパレーション法）に基づく膜分離処理が注目されている。浸透気化分離法は混合物の分離に適した分離法であり、分離膜として、無機膜としてのゼオライト膜や高分子膜としてのポリスルホン膜、シリコン膜、ポリアミド膜、ポリイミド膜等が一般的に利用される。 From such a viewpoint, a membrane separation process based on a pervaporation separation method (pervaporation method) has attracted attention as a new method for purifying a recovered liquid in place of the distillation treatment. The pervaporation separation method is a separation method suitable for separating a mixture, and as a separation membrane, a zeolite membrane as an inorganic membrane, a polysulfone membrane as a polymer membrane, a silicon membrane, a polyamide membrane, a polyimide membrane, etc. are generally used. The
このような浸透気化分離法に基づいた膜分離装置を備えた有機溶剤回収システムとして、例えば、特許文献３、４に開示のものがある。当該特許文献３、４に開示の有機溶剤回収システムは、上述した従来の有機溶剤回収システムの凝縮回収装置の下流側にさらに浸透気化分離法に基づいた膜分離装置を追加した構成である。膜分離装置は、凝縮回収装置にて回収された高濃度の有機溶剤を含む回収液から水を分離して除去することにより、有機溶剤の精製を行う。さらに、特許文献４においては、膜分離装置へと供給される回収液と吸脱着処理装置より排出される脱着ガスとを熱交換させることにより、膜分離装置へと供給される回収液の熱源として脱着ガスを利用することによってランニングコストを下げる構成となっている。 As an organic solvent recovery system provided with a membrane separation apparatus based on such a pervaporation separation method, for example, there are those disclosed in Patent Documents 3 and 4. The organic solvent recovery system disclosed in Patent Documents 3 and 4 has a configuration in which a membrane separation device based on a pervaporation separation method is further added to the downstream side of the condensation recovery device of the conventional organic solvent recovery system described above. The membrane separator purifies the organic solvent by separating and removing water from the recovered liquid containing the high-concentration organic solvent recovered by the condensation recovery apparatus. Further, in Patent Document 4, as a heat source for the recovered liquid supplied to the membrane separation apparatus, the recovered liquid supplied to the membrane separation apparatus and the desorption gas discharged from the adsorption / desorption treatment apparatus are subjected to heat exchange. By using desorption gas, the running cost is reduced.
上記特許文献４に開示される有機溶剤回収システムは、膜分離装置へと供給される回収液と吸脱着処理装置より排出される脱着ガスとを熱交換部にて直接熱交換させている。ここで、吸脱着処理装置より排出される脱着ガスの温度は一定ではなく、脱着処理において通常使用される水蒸気温度の１００〜１２０℃まで到達することもある。そのため、膜分離装置へと供給される回収液と吸脱着装置より排出される脱着ガスとを直接熱交換させることにより、熱交換器内部で局所的に回収液の温度が高温になるという事態が発生することがわかった。その結果として、回収液中に含まれる有機溶剤の分解が促進され、分解物による膜分離性能の低下、および膜分離装置によって処理された透過液に含まれる分解物の処理が必要となってしまう。さらには、局所的に回収液の温度が高温になると有機溶剤の種類によっては酸が発生してしまい、配管などの腐食を促進する原因となってしまう。 In the organic solvent recovery system disclosed in Patent Document 4, the recovery liquid supplied to the membrane separation device and the desorption gas discharged from the adsorption / desorption treatment device are directly heat-exchanged at the heat exchange unit. Here, the temperature of the desorption gas discharged from the adsorption / desorption processing apparatus is not constant, and may reach the steam temperature of 100 to 120 ° C. that is normally used in the desorption process. Therefore, there is a situation in which the temperature of the recovered liquid locally becomes high inside the heat exchanger by directly exchanging heat between the recovered liquid supplied to the membrane separator and the desorption gas discharged from the adsorption / desorption apparatus. It was found to occur. As a result, the decomposition of the organic solvent contained in the recovered liquid is accelerated, the degradation of the membrane separation performance due to the degradation product, and the treatment of the degradation product contained in the permeate treated by the membrane separation apparatus are required. . Furthermore, when the temperature of the recovered liquid is locally high, an acid is generated depending on the type of the organic solvent, which causes corrosion of piping and the like.
そこで、本発明は、上述した問題点を解決すべくなされたものであり、有機溶剤を含有する被処理ガスから当該有機溶剤を回収するに際し、当該有機溶剤の分解物の発生を抑制し、純度の高い有機溶剤を回収可能であり、配管の腐食を抑制可能な、有機溶剤回収システムを提供することを目的とする。 Therefore, the present invention has been made to solve the above-mentioned problems, and when the organic solvent is recovered from the gas to be treated containing the organic solvent, the generation of decomposition products of the organic solvent is suppressed, and the purity is reduced. It is an object of the present invention to provide an organic solvent recovery system that can recover a high organic solvent and can suppress corrosion of piping.
本発明者らは、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 As a result of intensive studies to solve the problems of the prior art, the present inventors finally completed the present invention. That is, the present invention is as follows.
本発明に基づく有機溶剤回収システムは、有機溶剤を含有する被処理ガスから当該有機溶剤を回収する有機溶剤回収システムであって、吸着材を充填した処理槽を有し、処理槽に導入された前記被処理ガス中の有機溶剤を吸着材に吸着させ、有機溶剤の濃度が下げられた処理ガスを排出する吸着処理と、処理槽に導入された水蒸気にて吸着材から有機溶剤を脱着し、高濃度の有機溶剤を含む脱着ガスを排出する脱着処理と、を交互に繰り返す吸脱着処理装置と、前記脱着ガスを冷却凝縮し、有機溶剤を含む回収液と水を主成分とする分離液とに分離する凝縮分液装置と、回収液を接触させることで回収液に含有される水または有機溶剤の分解物が混入した水を選択的に透過して分離する分離膜を有し、前記凝縮分液装置から排出された回収液を導入することで、有機溶剤を主成分とする濃縮液と水を主成分とする透過液とに分離する膜分離装置と、前記吸脱着装置から排出された前記脱着ガスが前記凝縮分離装置に導入される前に、当該脱着ガスから潜熱を取り出し蓄熱する蓄熱部、および蓄熱部に蓄熱された熱を前記凝縮分液装置より排出された回収液へ与える熱付与部を有する熱媒装置と、を備える。 An organic solvent recovery system according to the present invention is an organic solvent recovery system for recovering an organic solvent from a gas to be processed containing an organic solvent, and has a processing tank filled with an adsorbent, and is introduced into the processing tank Adsorbing the organic solvent in the gas to be treated to the adsorbent, discharging the processing gas having a reduced concentration of the organic solvent, and desorbing the organic solvent from the adsorbent with water vapor introduced into the treatment tank, A desorption process for alternately discharging a desorption gas containing a high-concentration organic solvent, and an adsorption / desorption treatment apparatus that alternately repeats the cooling and condensation of the desorption gas, and a separation liquid containing an organic solvent and a separation liquid mainly composed of water. A separation / separation device for selectively permeating and separating water contained in the recovered liquid or water mixed with a decomposition product of the organic solvent by contacting the recovered liquid with Collected liquid discharged from the separator By introducing a membrane separation device that separates into a concentrate mainly composed of an organic solvent and a permeate mainly composed of water, the desorption gas discharged from the adsorption / desorption device is introduced into the condensation separation device. A heat storage device that takes out latent heat from the desorption gas and stores the heat, and a heat transfer device that has a heat application unit that applies heat stored in the heat storage unit to the recovered liquid discharged from the condensate separator. Prepare.
上記本発明に基づく有機溶剤回収システムにあっては、上記吸着材が活性炭素繊維であることが好ましい。 In the organic solvent recovery system according to the present invention, the adsorbent is preferably activated carbon fiber.
上記本発明に基づく有機溶剤回収システムにあっては、上記膜分離装置が浸透気化分離法に基づくものであることが好ましい。 In the organic solvent recovery system according to the present invention, the membrane separation device is preferably based on a pervaporation separation method.
上記本発明に基づく有機溶剤回収システムにあっては、上記分離膜が炭素膜であることが好ましい。 In the organic solvent recovery system according to the present invention, the separation membrane is preferably a carbon membrane.
上記本発明に基づく有機溶剤回収システムにあっては、上記分離膜が中空糸構造を有していることが好ましい。 In the organic solvent recovery system according to the present invention, the separation membrane preferably has a hollow fiber structure.
上記本発明に基づく有機溶剤回収システムにあっては、上記被処理ガス中に含まれる有機溶剤が水と反応することで酸を発生する成分を含んでいる場合に特に好適に利用される。ここで、水と反応することで酸を発生する成分としては、例えば、酢酸エステルまたは塩基性化合物が挙げられる。 The organic solvent recovery system according to the present invention is particularly preferably used when the organic solvent contained in the gas to be treated contains a component that generates an acid by reacting with water. Here, as a component which generate | occur | produces an acid by reacting with water, an acetate ester or a basic compound is mentioned, for example.
本発明に基づく有機溶剤回収システムによれば、吸脱着処理装置が脱着処理時に排出する高濃度の有機溶剤を含む脱着ガスから潜熱を取り出し蓄熱する蓄熱部と、蓄熱部に蓄熱された熱を凝縮分液装置より排出された回収液へ与える熱付与部とを有する熱媒装置を備えている。よって、脱着ガスの潜熱を一旦する蓄積してから回収液に与えることで、回収液が部分的に高温になり有機溶剤が分解することを防げる。また、高温で酸が発生する有機溶剤が含まれていても、酸の発生を抑制できる。 According to the organic solvent recovery system based on the present invention, the adsorption / desorption processing device extracts latent heat from the desorption gas containing the high concentration organic solvent discharged during the desorption process, and stores the heat, and condenses the heat stored in the heat storage unit. And a heat transfer device having a heat applying unit for giving the recovered liquid discharged from the liquid separator. Therefore, once the latent heat of the desorption gas is accumulated and applied to the recovered liquid, it is possible to prevent the recovered liquid from being partially heated to decompose the organic solvent. Moreover, even if the organic solvent which generate | occur | produces an acid at high temperature is contained, generation | occurrence | production of an acid can be suppressed.
このように、本発明によれば、被処理ガスから有機溶剤を回収するに際し、有機溶剤の分解物の発生を抑制し、純度の高い有機溶剤を回収可能であり、配管などの腐食を抑制可能な、省エネルギー化が図られた有機溶剤回収システムを提供することができる。 Thus, according to the present invention, when recovering the organic solvent from the gas to be treated, it is possible to suppress the generation of decomposition products of the organic solvent, recover the high-purity organic solvent, and suppress the corrosion of piping and the like. In addition, an organic solvent recovery system that can save energy can be provided.
本発明の一実施形態の有機溶剤回収システム１００について図１を用いて説明する。図１に示すように、本実施形態の有機溶剤回収システム１００は、吸脱着処理装置１、凝縮分液装置２、膜分離装置３、熱媒装置４を備えている。 An organic solvent recovery system 100 according to an embodiment of the present invention will be described with reference to FIG. As shown in FIG. 1, the organic solvent recovery system 100 of this embodiment includes an adsorption / desorption treatment device 1, a condensate / separation device 2, a membrane separation device 3, and a heat medium device 4.
吸脱着処理装置１は、被処理ガス（有機溶剤含有ガス）を処理して清浄ガス（処理済ガス）を排出する装置であり、図１に示すように、それぞれ吸着材１４が充填された処理槽１３を備えている。本実施形態では２つの処理槽１３を備えているが、備える数に限定はなく、１つでも、３つ以上でもよい。 The adsorption / desorption treatment apparatus 1 is an apparatus for treating a gas to be treated (organic solvent-containing gas) and discharging a clean gas (treated gas). As shown in FIG. 1, each of the treatments is filled with an adsorbent 14. A tank 13 is provided. In the present embodiment, two treatment tanks 13 are provided, but the number of treatment tanks is not limited, and may be one or three or more.
吸着材１４は、粒状、粉体状、繊維状、ハニカム状の活性炭、ゼオライト、シリカゲルや活性アルミナなどを用いることができる。特に活性炭素繊維を用いることが好ましい。活性炭素繊維は表面にミクロ孔を有することと繊維状構造であることより、被吸着物質の吸着速度及び脱着速度が速い為、被処理ガスを効率よく処理することができる為である。 The adsorbent 14 may be granular, powder, fiber, honeycomb activated carbon, zeolite, silica gel, activated alumina, or the like. In particular, it is preferable to use activated carbon fibers. This is because the activated carbon fiber has micropores on the surface and has a fibrous structure, so that the adsorption rate and desorption rate of the substance to be adsorbed are high, so that the gas to be treated can be treated efficiently.
吸着材１４として活性炭素繊維を用いる場合、そのＢＥＴ比表面積は、１５００〜２０００ｍ２／ｇ、平均細孔径は、１５〜１８Å、細孔容積は、０．５〜０．８ｃｍ３／ｇであるのが好ましい。この数値範囲であると、被処理ガスを効率よく処理することができる。 When activated carbon fiber is used as the adsorbent 14, the BET specific surface area is 1500 to 2000 m 2 / g, the average pore diameter is 15 to 18 mm, and the pore volume is 0.5 to 0.8 cm 3 / g. Is preferred. Within this numerical range, the gas to be processed can be processed efficiently.
吸脱着処理装置１は、処理槽１３に有機溶剤含有の被処理ガスを導入して有機溶剤を吸着材１４に吸着させて清浄ガスを排出する吸着処理を実施する。また、処理槽１３に脱着用ガスを導入して吸着材１４から有機溶剤を脱着する脱着処理を実施する。本実施形態では、脱着用ガスとして水蒸気を用いる。 The adsorption / desorption treatment apparatus 1 performs an adsorption process in which a gas to be treated containing an organic solvent is introduced into a treatment tank 13 to adsorb the organic solvent to the adsorbent 14 and exhaust a clean gas. Further, a desorption process is performed in which a desorption gas is introduced into the treatment tank 13 to desorb the organic solvent from the adsorbent 14. In this embodiment, water vapor is used as the desorption gas.
処理槽１３には上ダンパー１６および下ダンパー１５が取付けられており、これらダンパーの開閉によりガスの流路を切替えることができる。 An upper damper 16 and a lower damper 15 are attached to the treatment tank 13, and the gas flow path can be switched by opening and closing these dampers.
被処理ガスは、被処理ガス供給ダクト１１より原ガス送風機１２へ送り込まれ、下ダンパー１５及び上ダンパー１６が開いて吸着処理できる状態となっている処理槽１３（処理槽）に導入される。処理槽１３での吸着処理により、被処理ガスは、有機溶剤が処理槽１３の吸着材１４にて吸着されて、清浄ガスとなってと処理槽１３に接続された清浄ガス排出ダクト１７より排出される。 The gas to be processed is fed from the gas supply duct 11 to the raw gas blower 12 and is introduced into the processing tank 13 (processing tank) in which the lower damper 15 and the upper damper 16 are opened and can be subjected to an adsorption process. By the adsorption treatment in the treatment tank 13, the gas to be treated is discharged from the clean gas discharge duct 17 connected to the treatment tank 13 when the organic solvent is adsorbed by the adsorbent 14 in the treatment tank 13 and becomes a clean gas. Is done.
本実施形態では、被処理ガスに含まれる有機溶剤は、水と反応することで酸を発生させる成分を含むものとする。水と反応することで酸を発生させる成分とは、一般的には酢酸エステル及び塩基性化合物が挙げられる。例えば、酢酸エチル、酢酸ブチル、塩化メチレン、トリクレンなどが挙げられるが、これらに限定されるものではない。 In this embodiment, the organic solvent contained in the gas to be treated includes a component that generates an acid by reacting with water. The component that generates an acid by reacting with water generally includes acetates and basic compounds. Examples include, but are not limited to, ethyl acetate, butyl acetate, methylene chloride, trichlene and the like.
一方、下ダンパー１５及び上ダンパー１６が閉じられて脱着処理できる状態となっている処理槽１３（脱着槽）には、その処理槽１３に設けられた水蒸気供給口１８から脱着用ガスとして水蒸気が導入される。この水蒸気は、水蒸気供給ライン２０より水蒸気ライン切替弁２１を経由して水蒸気供給口１８へ供給される。処理槽１３への水蒸気の導入により吸着材１４に吸着された有機溶剤の脱着処理が行われる。 On the other hand, in the treatment tank 13 (desorption tank) in which the lower damper 15 and the upper damper 16 are closed and can be desorbed, water vapor is removed as desorption gas from the water vapor supply port 18 provided in the treatment tank 13. be introduced. The steam is supplied from the steam supply line 20 to the steam supply port 18 via the steam line switching valve 21. The desorption process of the organic solvent adsorbed on the adsorbent 14 by the introduction of water vapor into the treatment tank 13 is performed.
ここで、被処理ガスを処理槽１３に導入し吸着材１４に有機溶剤を吸着させる吸着処理と、処理槽１３に脱着用ガスを導入し吸着材１４から有機溶剤を脱着させる脱着処理とを、下ダンパー１５及び上ダンパー１６の開閉操作によって交互に繰り返し行うことで、連続して有機溶剤含有ガスを清浄化することができる。 Here, an adsorption process for introducing the gas to be treated into the treatment tank 13 and adsorbing the organic solvent to the adsorbent 14, and a desorption process for introducing the desorption gas into the treatment tank 13 and desorbing the organic solvent from the adsorbent 14, By alternately repeating the opening / closing operation of the lower damper 15 and the upper damper 16, the organic solvent-containing gas can be continuously cleaned.
処理槽１３から脱着された有機溶剤を含む水蒸気は、処理槽１３に設けられた脱着水蒸気排出口１９より脱着水蒸気ライン３１を経由して第一熱交換器３２へ供給される。第一熱交換器３２は、処理槽１３から脱着された有機溶剤を含む水蒸気の熱と後述のように熱媒装置４を循環する熱媒との熱を交換する機器である。本実施形態では、第一熱交換器３２は、後述のように熱媒装置４が備えているが、例えば、凝縮分離装置２が備えていてもよいし、設置場所は問わない。 The water vapor containing the organic solvent desorbed from the treatment tank 13 is supplied to the first heat exchanger 32 via the desorption water vapor line 31 from the desorption water vapor outlet 19 provided in the treatment tank 13. The first heat exchanger 32 is a device that exchanges heat between water vapor containing the organic solvent desorbed from the treatment tank 13 and heat medium circulating in the heat medium device 4 as described later. In the present embodiment, the first heat exchanger 32 is provided in the heat medium device 4 as described later. However, for example, the condensing and separating device 2 may be provided, and the installation location is not limited.
処理槽１３から脱着された有機溶剤を含む水蒸気は、第一熱交換器３２において潜熱が奪われ、配管ライン４４を介して凝縮分液装置２へと供給される。凝縮分離装置２は、凝縮器３３、凝縮液タンク３４を備える。処理槽１３から脱着された有機溶剤を含む水蒸気は、凝縮器３３にて冷却され液化し、配管ライン４５を通って凝縮液タンク３４へと供給され、比重差により有機溶剤を含む回収液と水を主成分とする分離液とに分離される。凝縮器３３では、冷水を用いて冷却するものとするが、これに限定されない。 The steam containing the organic solvent desorbed from the treatment tank 13 is deprived of latent heat in the first heat exchanger 32 and is supplied to the condensing / separating apparatus 2 via the piping line 44. The condensing and separating apparatus 2 includes a condenser 33 and a condensate tank 34. The water vapor containing the organic solvent desorbed from the treatment tank 13 is cooled and liquefied by the condenser 33, supplied to the condensate tank 34 through the piping line 45, and the recovered liquid and water containing the organic solvent due to the specific gravity difference. Is separated into a separation liquid containing as a main component. The condenser 33 is cooled using cold water, but is not limited to this.
凝縮分液装置２にて得られた有機溶剤を含む回収液は、配管ライン４６を通って膜分離装置３へと供給される。膜分離装置３は、回収液タンク３８、送液ポンプ３９、ヒーター４０、膜分離器４１を備えている。配管ライン４６を通って供給された有機溶剤を含む回収液は、回収液タンク３８に供給され、送液ポンプ３９によって配送ライン４６を通って第二熱交換器３６、ヒーター４０、膜分離器４１へと順に送られる。第二熱交換器３６とヒーター４０との間は配管ライン４８、ヒーター４０と膜分離器４１との間は配管ライン４９で接続している。第二熱交換器３６は、回収液の熱と後述のように熱媒装置４を循環する熱媒との熱を交換する機器である。本実施形態では、第二熱交換器３６は、後述のように熱媒装置４が備えているが、例えば、膜分離装置３が備えていてもよいし、設置場所は問わない。 The recovered liquid containing the organic solvent obtained by the condensing / separating apparatus 2 is supplied to the membrane separation apparatus 3 through the piping line 46. The membrane separation device 3 includes a recovery liquid tank 38, a liquid feed pump 39, a heater 40, and a membrane separator 41. The recovered liquid containing the organic solvent supplied through the piping line 46 is supplied to the recovered liquid tank 38, and the second heat exchanger 36, the heater 40, and the membrane separator 41 through the distribution line 46 by the liquid feed pump 39. Are sent in order. A pipe line 48 is connected between the second heat exchanger 36 and the heater 40, and a pipe line 49 is connected between the heater 40 and the membrane separator 41. The second heat exchanger 36 is a device that exchanges the heat of the recovered liquid and the heat medium circulating in the heat medium device 4 as described later. In the present embodiment, the second heat exchanger 36 is provided in the heat medium device 4 as described later. However, for example, the membrane separation device 3 may be provided, and the installation location is not limited.
膜分離器４１は、有機溶剤を含む回収液中の水分などの不純物を浸透気化分離法に基づいて分離する。膜分離器４１にて不純物が取り除かれた回収液は、濃縮液ライン４２を経由し回収液タンク３８に再び供給される。分離された不純物は排出ライン５０から排出される。 The membrane separator 41 separates impurities such as moisture in the collected liquid containing the organic solvent based on the pervaporation separation method. The recovered liquid from which impurities have been removed by the membrane separator 41 is supplied again to the recovered liquid tank 38 via the concentrated liquid line 42. The separated impurities are discharged from the discharge line 50.
膜分離装置３では、上記処理が繰り返されて、回収タンク３８中の回収液の不純物が徐々に減らされる。そして所定時間上記処理が繰り返された後、回収タンクに接続した回収ライン４３から回収液が排出され回収される。 In the membrane separation device 3, the above process is repeated, and the impurities of the recovered liquid in the recovery tank 38 are gradually reduced. Then, after the above process is repeated for a predetermined time, the recovered liquid is discharged and recovered from the recovery line 43 connected to the recovery tank.
ここで、膜分離器４１に使用する分離膜は、例えば、各種の無機膜や高分子膜が利用可能ではあるが、特に炭素膜を使用することが好ましい。これは、浸透気化分離法にて分離する有機溶剤を含んだ回収液は比較的高温にて使用し、且つ酸成分が含まれる可能性があるからである。耐熱性や耐酸性等に優れた炭素膜を使用することで高寿命化を図ることができる。例えば、高分子膜を使用した場合においては、有機溶剤を含む回収液によって高分子膜が大きく膨潤してしまい、膜分離器４１から高分子膜が離脱されてしまう可能性があり、ゼオライト膜を使用した場合においては、有機溶剤を含む回収液中の酸成分によって、膜構造が破壊されてしまう可能性があるためである。 Here, as the separation membrane used in the membrane separator 41, for example, various inorganic membranes and polymer membranes can be used, but it is particularly preferable to use a carbon membrane. This is because the recovered liquid containing the organic solvent separated by the pervaporation separation method is used at a relatively high temperature and may contain an acid component. By using a carbon film having excellent heat resistance and acid resistance, the life can be extended. For example, when a polymer membrane is used, the polymer membrane may be greatly swollen by the recovery liquid containing the organic solvent, and the polymer membrane may be detached from the membrane separator 41. This is because when used, the film structure may be destroyed by the acid component in the recovered liquid containing the organic solvent.
また、膜分離器４１に使用する分離膜は、中空糸構造を有していることが好ましい。分離膜の構造を中空糸にすることで、単位体積当たりの分離膜充填量を増加させることができ、結果としてシステムの小型化、低コスト化及び省エネルギー化を図ることができるためである。 Moreover, it is preferable that the separation membrane used for the membrane separator 41 has a hollow fiber structure. This is because by using a hollow fiber as the structure of the separation membrane, the amount of separation membrane filling per unit volume can be increased, and as a result, the system can be reduced in size, cost, and energy can be reduced.
なお、中空糸構造を有する炭素膜の原料としては、アクリル系樹脂、ポリイミド系樹脂、セルロース系樹脂、ポリフェニレンオキシド系樹脂、ポリフルフリルアルコール、フェノール樹脂等が挙げられるが、特にその原料が限定されるものではない。 Examples of the raw material for the carbon membrane having a hollow fiber structure include acrylic resins, polyimide resins, cellulose resins, polyphenylene oxide resins, polyfurfuryl alcohol, and phenol resins, but the raw materials are particularly limited. It is not a thing.
また、中空糸構造を有する炭素膜とは、上述の樹脂原料などを中空状に加工し、さらにそれを不活性雰囲気下で熱処理したものである。熱処理温度としては、樹脂原料の熱分解開始温度以上であり、一般的には２５０℃以上である。不活性雰囲気下の熱処理温度は、膜分離性能に直結するため、最適な温度を選定することができる。しかし、温度が高すぎる場合、熱収縮により炭素膜の膜孔が閉塞してしまうため、上限としては１３００℃程度が望ましい。 The carbon membrane having a hollow fiber structure is obtained by processing the above-mentioned resin raw material or the like into a hollow shape and further heat-treating it in an inert atmosphere. The heat treatment temperature is equal to or higher than the thermal decomposition start temperature of the resin raw material, and is generally 250 ° C. or higher. Since the heat treatment temperature in the inert atmosphere is directly related to the membrane separation performance, an optimum temperature can be selected. However, if the temperature is too high, the pores of the carbon film are blocked by heat shrinkage, so the upper limit is preferably about 1300 ° C.
更に、不活性雰囲気下での熱処理の前に、空気中での熱処理（耐炎化、不融化、熱安定化ともいう）や、樹脂に難燃剤などを付与することも可能である。また、不活性雰囲気下での熱処理の後に、薬品による処理や、熱処理による表面処理を加えてもよい。炭素膜は、炭素、水素、酸素、窒素、硫黄などの元素と、前述の金属成分で構成され、主成分としては炭素であり、その含有率は６０％以上である。炭素の含有量の上限としては、特に制限はないが、９９．９％程度が事実上の上限である。 Furthermore, before the heat treatment under an inert atmosphere, heat treatment in air (also referred to as flame resistance, infusibilization, or heat stabilization) or a flame retardant can be imparted to the resin. Further, a chemical treatment or a surface treatment by heat treatment may be added after the heat treatment in an inert atmosphere. The carbon film is composed of elements such as carbon, hydrogen, oxygen, nitrogen, sulfur, and the above-described metal components, the main component is carbon, and the content is 60% or more. The upper limit of the carbon content is not particularly limited, but about 99.9% is a practical upper limit.
熱媒装置４は、第一熱交換器３２と第二熱交換器３６と熱媒タンク３５とを備えている。熱媒タンク３５には熱媒が蓄えられており、その一部が、第一熱交換装置３２、熱媒タンク３５、および第二熱交換器３６を循環する。第一熱交換装置３２、熱媒タンク３５、および第二熱交換器３６は、循環ライン３７で接続されており、熱媒は循環ライン３７を通る。 The heat medium device 4 includes a first heat exchanger 32, a second heat exchanger 36, and a heat medium tank 35. A heat medium is stored in the heat medium tank 35, and a part of the heat medium circulates through the first heat exchange device 32, the heat medium tank 35, and the second heat exchanger 36. The first heat exchange device 32, the heat medium tank 35, and the second heat exchanger 36 are connected by a circulation line 37, and the heat medium passes through the circulation line 37.
熱媒は、第一熱交換器３２を通過する際、吸脱着処理装置１より脱着された有機溶剤を含む水蒸気から受熱する。このとき水蒸気は熱を奪われ温度が下がり、熱媒は温度が上がる。受熱した熱媒は熱媒タンク３５内に導入され、熱媒タンク３５内の温度を平準化させる。熱媒タンク３５から排出された熱媒は、第二熱交換機３６を通過する際、回収液タンク３８より送液ポンプ３９によって第二熱交換器３６に供給された有機溶剤を含む回収液を加熱する。このとき回収液の温度は上がり、熱媒の温度は下がる。温度が下がった熱媒は再び第一熱交換器３２にて受熱して温度が上がる。これらを繰り返す。 When passing through the first heat exchanger 32, the heat medium receives heat from water vapor containing the organic solvent desorbed from the adsorption / desorption treatment apparatus 1. At this time, the water vapor is deprived of heat and the temperature is lowered, and the temperature of the heating medium is raised. The received heat medium is introduced into the heat medium tank 35, and the temperature in the heat medium tank 35 is leveled. When the heat medium discharged from the heat medium tank 35 passes through the second heat exchanger 36, the recovered liquid containing the organic solvent supplied to the second heat exchanger 36 by the liquid feed pump 39 from the recovered liquid tank 38 is heated. To do. At this time, the temperature of the recovered liquid increases and the temperature of the heat medium decreases. The heat medium whose temperature has been lowered receives heat again in the first heat exchanger 32 and the temperature rises. Repeat these.
熱媒タンク３５の熱媒容量は、熱媒の循環ライン３７及び第一熱交換器３２及び第二熱交換器３６の容量に対して十分大きくすることが望ましい。こうすることで、熱媒タンク３５内で熱媒の温度を平準化することができ、第二熱交換器３６にて熱媒によって有機溶剤を含む回収液を加熱する際に、有機溶剤の分解物が生成されるのを抑制することができる。 It is desirable that the heat medium capacity of the heat medium tank 35 be sufficiently larger than the capacity of the heat medium circulation line 37, the first heat exchanger 32, and the second heat exchanger 36. In this way, the temperature of the heat medium can be leveled in the heat medium tank 35, and the organic solvent is decomposed when the recovered liquid containing the organic solvent is heated by the heat medium in the second heat exchanger 36. It can suppress that a thing is produced | generated.
熱媒装置４に使用される熱媒は、熱による安定性及び比熱容量が高い流体であればどのようなものでもよいが、特に水を使用することが好ましい。 The heating medium used in the heating medium device 4 may be any fluid as long as it has high heat stability and high specific heat capacity, but it is particularly preferable to use water.
熱媒タンク３５内の熱媒温度は、５０〜７０℃の温度領域で安定させるのが望ましい。熱媒温度が５０℃を下回ると、処理槽１３から脱着された有機溶剤を含む水蒸気の熱を十分に第二熱交換器３６に供給される有機溶剤を含む回収液に伝えることができず、結果として膜分離装置３に設置したヒーター４０にて加熱する為のエネルギーが多くなってしまう。また、熱媒温度が８０℃を上回ると、第二熱交換器３６において有機溶剤を含む回収液の分解を促進させてしまい、結果として膜分離器４１の膜性能の低下、及び膜分離により得られる濃縮液の品質を低下させてしまう。 The temperature of the heat medium in the heat medium tank 35 is desirably stabilized in a temperature range of 50 to 70 ° C. If the heat medium temperature is lower than 50 ° C., the heat of water vapor containing the organic solvent desorbed from the treatment tank 13 cannot be sufficiently transferred to the recovered liquid containing the organic solvent supplied to the second heat exchanger 36, As a result, the energy for heating with the heater 40 installed in the membrane separator 3 increases. Further, when the temperature of the heat medium exceeds 80 ° C., the decomposition of the recovered liquid containing the organic solvent is promoted in the second heat exchanger 36. As a result, the membrane performance of the membrane separator 41 is deteriorated and obtained by membrane separation. The quality of the resulting concentrate is reduced.
以上のように、有機溶剤回収システム１００は、熱媒装置４を備えることで、吸脱着処理装置１から排出される脱着された有機溶剤を含む水蒸気と、膜分離装置３を循環する有機溶剤を含む回収液とを、熱媒を通じて間接的に熱交換させることができる。吸脱着処理装置１より排出される脱着された有機溶剤を含む水蒸気が一時的に高温となった場合においても、膜分離装置３を循環する回収液に直接高温熱源を触れさせることが無いため、回収液の熱による分解物生成を大きく抑制することができ、結果として膜分離装置３の性能を高めることが可能となり、かつ濃縮液の純度を高めることができる。 As described above, the organic solvent recovery system 100 includes the heat medium device 4 so that the water vapor containing the desorbed organic solvent discharged from the adsorption / desorption treatment device 1 and the organic solvent circulating in the membrane separation device 3 are collected. The collected liquid can be indirectly heat-exchanged through the heat medium. Even when the water vapor containing the desorbed organic solvent discharged from the adsorption / desorption treatment device 1 is temporarily at a high temperature, the recovered liquid circulating through the membrane separation device 3 is not directly brought into contact with the high-temperature heat source, Generation of decomposition products due to the heat of the recovered liquid can be greatly suppressed. As a result, the performance of the membrane separation device 3 can be improved, and the purity of the concentrated liquid can be increased.
以下に本実施形態の有機溶剤回収システム１００を用いた実施例を示して本発明を具体的に説明するが、本発明は以下の内容に限定されるものではない。 Hereinafter, the present invention will be specifically described with reference to examples using the organic solvent recovery system 100 of the present embodiment, but the present invention is not limited to the following contents.
（実施例）
実施例では、有機溶剤回収システム１００を用いて、吸着材１３として、活性炭素繊維の不織布を用いた。また、膜分離器４１として、中空糸炭素膜を用いた。
(Example)
In the examples, the organic solvent recovery system 100 was used, and an activated carbon fiber nonwoven fabric was used as the adsorbent 13. A hollow fiber carbon membrane was used as the membrane separator 41.
被処理ガスとして酢酸エチル３０００ｐｐｍを含む４５℃の混合ガスを、風量４．０Ｎｍ３／分で原ガス送風機１２にて処理槽１３に導入し、処理槽１３の吸着材１４にて１０分間吸着処理を行った。次に有機溶剤を吸着した吸着材１４に水蒸気を用いて８分間脱着処理を行った。有機溶剤を含んだ脱着ガスは、脱着水蒸気排出口１９より脱着水蒸気ライン３１を経由して第一熱交換器３２へ供給され、熱媒装置４を循環させている温水と熱交換した後に凝縮器３３へ供給され液化凝縮され、凝縮液タンク３４にて分離水と酢酸エチルを主成分とする回収液とに分液された。 A mixed gas at 45 ° C. containing 3000 ppm of ethyl acetate as the gas to be treated is introduced into the treatment tank 13 by the raw gas blower 12 at an air volume of 4.0 Nm 3 / min, and is adsorbed by the adsorbent 14 of the treatment tank 13 for 10 minutes. Went. Next, the adsorbent 14 having adsorbed the organic solvent was subjected to desorption treatment using water vapor for 8 minutes. The desorption gas containing the organic solvent is supplied from the desorption water vapor outlet 19 to the first heat exchanger 32 via the desorption water vapor line 31 and exchanges heat with the hot water circulating through the heat medium device 4, and then the condenser. The solution was supplied to 33 and liquefied and condensed, and separated into separated water and a recovered liquid mainly composed of ethyl acetate in a condensate tank 34.
凝縮液タンク３４内の酢酸エチルを主成分とする回収液を回収液タンク３８に移送し、送液ポンプ３９にて第二熱交換器３６に供給し、熱媒装置４を循環させている温水により熱交換後、ヒーター４０にて７０℃まで加温させた後に膜分離器４１に導入して膜分離処理を行った。 Warm water in which the recovered liquid mainly composed of ethyl acetate in the condensate tank 34 is transferred to the recovered liquid tank 38, supplied to the second heat exchanger 36 by the liquid feed pump 39, and the heat medium device 4 is circulated. After the heat exchange, the heater 40 was heated to 70 ° C. and then introduced into the membrane separator 41 to perform a membrane separation treatment.
本実施例においては、凝縮液タンクにて分離された酢酸エチルを主成分とする回収液の酢酸エチル濃度は９６．５ｗｔ％であり、膜分離器４１にて膜分離された濃縮液の酢酸エチル濃度は９９．９ｗｔ％であり、当該濃縮液の水分濃度は０．１ｗｔ％、酢酸濃度は１０ｐｐｍ以下であることが確認された。この結果は、被処理ガスから有機溶剤を回収することで得られる回収液の濃度および収率としては、十分に高濃度で高収率なものであると言える。 In this embodiment, the concentration of ethyl acetate in the recovered liquid mainly composed of ethyl acetate separated in the condensate tank is 96.5 wt%, and the ethyl acetate in the concentrated liquid separated in the membrane separator 41 is used. It was confirmed that the concentration was 99.9 wt%, the water concentration of the concentrate was 0.1 wt%, and the acetic acid concentration was 10 ppm or less. This result can be said to be a sufficiently high concentration and high yield as the concentration and yield of the recovered liquid obtained by recovering the organic solvent from the gas to be treated.
（比較例）
比較例では、有機溶剤回収システム１００の熱媒装置４の代わりに熱交換器３０を用いた、図２に示す有機溶剤回収システム１００ｃを用いた。熱交換器３０は、回収液と吸脱着処理装置より排出される脱着ガスの熱と、回収液タンク３８より送液ポンプ３９によって第二熱交換器３６に供給された有機溶剤を含む回収液とを、直接熱交換させる機器である。有機溶剤回収システム１００ｃにおいて熱交換器３０以外の構成は有機溶剤回収システム１００と同様である。比較例において、吸着材１４は、実施例と同じものを用いた。また、膜分離器４１には、実施例１と同じ中空糸炭素膜を用いた。
(Comparative example)
In the comparative example, the organic solvent recovery system 100c shown in FIG. 2 using the heat exchanger 30 instead of the heat medium device 4 of the organic solvent recovery system 100 was used. The heat exchanger 30 includes the recovered liquid and the heat of the desorption gas discharged from the adsorption / desorption processing device, and the recovered liquid containing the organic solvent supplied from the recovered liquid tank 38 to the second heat exchanger 36 by the liquid feed pump 39. Is a device for directly exchanging heat. In the organic solvent recovery system 100c, the configuration other than the heat exchanger 30 is the same as that of the organic solvent recovery system 100. In the comparative example, the same adsorbent 14 as in the example was used. The membrane separator 41 was the same hollow fiber carbon membrane as that used in Example 1.
被処理ガスとして酢酸エチル３０００ｐｐｍを含む４５℃の混合ガスを、風量４．０Ｎｍ３／分で原ガス送風機１２にて処理槽１３に導入し、処理槽１３の吸着材１４にて１０分間吸着処理を行った。次に有機溶剤を吸着した吸着材１４に水蒸気を用いて８分間脱着処理を行った。有機溶剤を含んだ脱着ガスは、脱着水蒸気排出口１９より脱着水蒸気ライン３１を経由して熱交換器３０へ供給され、回収液タンク３８より送液ポンプ３９にて熱交換器３０へ供給される回収液と熱交換した後に凝縮器３３へ供給され液化凝縮され、凝縮液タンク３４にて分離水と酢酸エチルを主成分とする回収液とに分液された。 A mixed gas at 45 ° C. containing 3000 ppm of ethyl acetate as the gas to be treated is introduced into the treatment tank 13 by the raw gas blower 12 at an air volume of 4.0 Nm 3 / min, and is adsorbed by the adsorbent 14 of the treatment tank 13 for 10 minutes. Went. Next, the adsorbent 14 having adsorbed the organic solvent was subjected to desorption treatment using water vapor for 8 minutes. The desorption gas containing the organic solvent is supplied from the desorption water vapor outlet 19 to the heat exchanger 30 via the desorption water vapor line 31, and is supplied from the recovery liquid tank 38 to the heat exchanger 30 by the liquid feed pump 39. After exchanging heat with the recovered liquid, it was supplied to the condenser 33 to be liquefied and condensed, and separated in the condensate tank 34 into separated water and a recovered liquid mainly composed of ethyl acetate.
凝縮液タンク３４内の酢酸エチルを主成分とする回収液を回収液タンク３８に移送し、送液ポンプ３９にて熱交換器３０に供給し、有機溶剤を含んだ脱着ガスと熱交換後、ヒーター４０にて７０℃まで加温させた後に膜分離器４１に導入して膜分離処理を行った。 The recovered liquid mainly composed of ethyl acetate in the condensate tank 34 is transferred to the recovered liquid tank 38, supplied to the heat exchanger 30 by the liquid feed pump 39, and after heat exchange with the desorption gas containing the organic solvent, After heating to 70 ° C. with the heater 40, the membrane was introduced into the membrane separator 41 and subjected to membrane separation treatment.
上記比較例においては、凝縮液タンクにて分離された酢酸エチルを主成分とする回収液の酢酸エチル濃度は９６．５ｗｔ％であり、膜分離器４１にて膜分離された濃縮液の酢酸エチル濃度は９９．９ｗｔ％であり、当該濃縮液の水分濃度は０．１ｗｔ％であることが確認された。この結果は、被処理ガスから有機溶剤を回収することで得られる回収液の濃度および収率としては、十分に高濃度で高収率なものであると言える。 In the above comparative example, the ethyl acetate concentration of the recovered liquid mainly composed of ethyl acetate separated in the condensate tank is 96.5 wt%, and the ethyl acetate in the concentrated liquid separated by the membrane separator 41 is used. The concentration was 99.9 wt%, and it was confirmed that the water concentration of the concentrate was 0.1 wt%. This result can be said to be a sufficiently high concentration and high yield as the concentration and yield of the recovered liquid obtained by recovering the organic solvent from the gas to be treated.
しかしながら比較例においては、膜分離装置３において膜分離処理を行う回収液と吸脱着装置から排出される高温の脱着ガスとを直接熱交換させることにより、膜分離された濃縮液中の酢酸濃度が１００ｐｐｍ以上となっていることが確認された。これは、回収液が高温に晒されることにより酢酸エチルが加水分解され酢酸が発生したことを示している。 However, in the comparative example, the acetic acid concentration in the concentrated solution separated by membrane is obtained by directly exchanging heat between the recovered liquid for performing the membrane separation process in the membrane separation device 3 and the high temperature desorption gas discharged from the adsorption / desorption device. It was confirmed that it was 100 ppm or more. This indicates that ethyl acetate was hydrolyzed and acetic acid was generated by exposing the recovered liquid to high temperature.
以上において説明した結果から、上述した本実施の形態の如くの有機溶剤回収システム１００を用いることで、膜分離された溶剤中の酸成分の量を抑制することができ、配管の腐食や濃縮液再利用時の酸成分による不具合を減らすことができる。 From the results described above, by using the organic solvent recovery system 100 as in the present embodiment described above, the amount of the acid component in the solvent separated from the membrane can be suppressed, and pipe corrosion and concentrated liquid can be suppressed. Problems due to acid components during reuse can be reduced.
なお、上記開示した各実施形態および各実施例はすべて例示であり制限的なものではない。また、各実施形態および各実施例に開示された内容を組み合わせた実施形態および実施例も本発明の範囲に含まれる。本発明の技術的範囲は、特許請求の範囲によって有効であり、特許請求の範囲の記載と均等の意味および範囲内のすべての変更・修正・置き換え等を含むものである。 It should be noted that each of the disclosed embodiments and examples is illustrative and not restrictive. In addition, embodiments and examples obtained by combining the contents disclosed in each embodiment and each example are also included in the scope of the present invention. The technical scope of the present invention is effective according to the scope of the claims, and includes the meanings equivalent to the description of the scope of claims and all changes, modifications, and substitutions within the scope.
１ 吸脱着処理装置
２ 凝縮分液装置
３ 膜分離装置
４ 熱媒装置
１３ 処理槽
３１ 脱着水蒸気ライン
３２ 第一熱交換器（蓄熱部）
３３ 凝縮器
３４ 凝縮液タンク
３５ 熱媒タンク（蓄熱部）
３６ 第二熱交換器（熱付与部）
３７ 循環ライン
３８ 回収液タンク
１００ 有機溶剤回収システム
DESCRIPTION OF SYMBOLS 1 Adsorption / desorption processing apparatus 2 Condensation / separation apparatus 3 Membrane separation apparatus 4 Heat medium apparatus 13 Treatment tank 31 Desorption water vapor line 32 1st heat exchanger (heat storage part)
33 Condenser 34 Condensate Tank 35 Heat Medium Tank (Heat Storage Unit)
36 Second heat exchanger (heat application part)
37 Circulation line 38 Recovery liquid tank 100 Organic solvent recovery system
Claims (7)
吸着材を充填した処理槽を有し、処理槽に導入された前記被処理ガス中の有機溶剤を吸着材に吸着させ、有機溶剤の濃度が下げられた処理ガスを排出する吸着処理と、処理槽に導入された水蒸気にて吸着材から有機溶剤を脱着し、高濃度の有機溶剤を含む脱着ガスを排出する脱着処理と、を交互に繰り返す吸脱着処理装置と、
前記脱着ガスを冷却凝縮し、有機溶剤を含む回収液と水を主成分とする分離液とに分離する凝縮分液装置と、
回収液を接触させることで回収液に含有される水または有機溶剤の分解物が混入した水を選択的に透過して分離する分離膜を有し、前記凝縮分液装置から排出された回収液を導入することで、有機溶剤を主成分とする濃縮液と水を主成分とする透過液とに分離する膜分離装置と、
前記吸脱着装置から排出された前記脱着ガスが前記凝縮分離装置に導入される前に、当該脱着ガスから潜熱を取り出し蓄熱する蓄熱部、および蓄熱部に蓄熱された熱を前記凝縮分液装置より排出された回収液へ与える熱付与部を有する熱媒装置と、
を備えた有機溶剤回収システム。 An organic solvent recovery system for recovering the organic solvent from the gas to be treated containing the organic solvent,
An adsorption process having a treatment tank filled with an adsorbent, adsorbing the organic solvent in the gas to be treated introduced into the treatment tank to the adsorbent, and discharging the treatment gas having a reduced concentration of the organic solvent; An adsorption / desorption treatment device that alternately repeats a desorption process that desorbs an organic solvent from an adsorbent with water vapor introduced into a tank and discharges a desorption gas containing a high concentration organic solvent;
A condensing / separating device for cooling and condensing the desorption gas and separating it into a recovered liquid containing an organic solvent and a separated liquid mainly composed of water;
Recovered liquid discharged from the condensate separator, having a separation membrane that selectively permeates and separates water contained in the recovered liquid or water mixed with decomposition products of organic solvents by contacting the recovered liquid A membrane separation device that separates into a concentrate mainly composed of an organic solvent and a permeate mainly composed of water,
Before the desorption gas discharged from the adsorption / desorption device is introduced into the condensing / separating device, the latent heat is extracted from the desorption gas and heat is stored, and the heat stored in the heat storage unit is transferred from the condensing / separating device. A heat medium device having a heat applying unit for giving to the discharged recovered liquid;
Organic solvent recovery system equipped with.
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| CN117138517A (en) * | 2023-07-19 | 2023-12-01 | 江苏九天高科技股份有限公司 | A process for recovering low water-soluble VOCs gas and refining organic solvents |
| WO2024247642A1 (en) * | 2023-05-31 | 2024-12-05 | 東洋紡エムシー株式会社 | Organic solvent recovery system |
| WO2024247641A1 (en) * | 2023-05-31 | 2024-12-05 | 東洋紡エムシー株式会社 | Organic solvent recovery system |
| WO2025135145A1 (en) * | 2023-12-22 | 2025-06-26 | 国立研究開発法人産業技術総合研究所 | Method for producing separation/concentration product of volatile substance, and system for producing separation/concentration product of volatile substance |
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| CN110302629A (en) * | 2019-06-12 | 2019-10-08 | 苏州工业园区瑞丰源环保科技有限公司 | Intelligent activated carbon adsorption recyclable device |
| WO2024247642A1 (en) * | 2023-05-31 | 2024-12-05 | 東洋紡エムシー株式会社 | Organic solvent recovery system |
| WO2024247641A1 (en) * | 2023-05-31 | 2024-12-05 | 東洋紡エムシー株式会社 | Organic solvent recovery system |
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