JP2020146668A - Operation method of vacuum desorption type volatile organic compound recovery device - Google Patents

Operation method of vacuum desorption type volatile organic compound recovery device Download PDF

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JP2020146668A
JP2020146668A JP2019048665A JP2019048665A JP2020146668A JP 2020146668 A JP2020146668 A JP 2020146668A JP 2019048665 A JP2019048665 A JP 2019048665A JP 2019048665 A JP2019048665 A JP 2019048665A JP 2020146668 A JP2020146668 A JP 2020146668A
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彰夫 松岡
Akio Matsuoka
彰夫 松岡
晃弘 塔本
Akihiro Tomoto
晃弘 塔本
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Abstract

To reduce a load of a condenser for sucking and then condensing, in a volatile organic compound treatment device for allowing an adsorbent in an adsorption tower to adsorb a volatile organic compound, and then vacuum sucking by a vacuum pump and desorbing it.SOLUTION: A parallel section having two or more routes having each different passing air volume is provided between an adsorption tower 11 and a vacuum pump 17, and each route has operable valves 23, 24 independently. When starting desorption, after opening a valve 24 of the route having a comparatively small passing air volume, a valve 23 of the route having a comparatively large passing air volume is opened.SELECTED DRAWING: Figure 1

Description

この発明は、揮発性有機化合物を含むガスを排出する前に、ガスから揮発性有機化合物を処理する装置に関する。 The present invention relates to an apparatus for treating a volatile organic compound from the gas before discharging the gas containing the volatile organic compound.

工場から発生する排ガスには、そのまま大気中に排出すると問題を起こす溶剤などの揮発性有機化合物が含まれる場合がある。この場合、排ガスを大気中に排出する前に、含有している揮発性有機化合物を処理しなければならない。その方法として、活性炭等の吸着剤を内蔵した吸着塔で、排ガス中に含まれる揮発性有機化合物を吸着剤に吸着させ、ガス中の濃度を低減させて大気へ排出する。 Exhaust gas generated from factories may contain volatile organic compounds such as solvents that cause problems if they are discharged into the atmosphere as they are. In this case, the volatile organic compounds contained must be treated before the exhaust gas is discharged into the atmosphere. As a method, a volatile organic compound contained in the exhaust gas is adsorbed on the adsorbent by an adsorbent tower containing an adsorbent such as activated carbon, the concentration in the gas is reduced, and the gas is discharged to the atmosphere.

その後、吸着剤に吸着された揮発性有機化合物を脱離させて、吸着塔を再利用可能にする。この脱離作業をしている間は当然に吸着ができないため、通常は複数の吸着塔を並列に設置し、一つの吸着塔が吸着をしている間に、他の吸着塔で脱離を行うという工程を循環して運用する。 After that, the volatile organic compounds adsorbed on the adsorbent are desorbed to make the adsorption tower reusable. Naturally, adsorption is not possible during this desorption work, so normally multiple adsorption towers are installed in parallel, and while one adsorption tower is adsorbing, desorption is performed by another adsorption tower. Operate by circulating the process of performing.

吸着剤から揮発性有機化合物を脱離させる方法としては、加熱した水蒸気を接触して脱離させる方法や（例えば特許文献１）、吸着塔を真空吸引して脱離させる方法（例えば特許文献２）などがある。 Examples of the method for desorbing the volatile organic compound from the adsorbent include a method of contacting and desorbing heated steam (for example, Patent Document 1) and a method of vacuum-sucking the adsorption tower for desorption (for example, Patent Document 2). )and so on.

吸着塔の吸着剤に吸着させた揮発性有機化合物を真空吸引により脱着させる場合の運用例を図４を用いて説明する。吸着塔１１ａ、１１ｂ（まとめて１１という）が二基並列に設けられ、それぞれの内部には揮発性有機化合物である溶剤を吸着する吸着剤が充填された吸着剤収容部１２ａ，１２ｂ（まとめて１２という）が設けられている。吸着塔１１ａ，１１ｂの上部には、内部へ揮発性有機化合物含有ガスＡを導入する導入口バルブ２１ａ，２１ｂと、塔内の気体を真空吸引するための吸引口バルブ２３ａ，２３ｂが設けられている。一方、吸着塔１１ａ，１１ｂの下部には、溶剤を吸着された後の処理後ガスＢが排出される排出口バルブ２２ａ，２２ｂが設けてある。排出口バルブ２２ａ，２２ｂの先には原ガスブロワ１６が設けてある。原ガスブロワ１６によって生じた圧力により、揮発性有機化合物含有ガスＡは吸着塔１１ａ、１１ｂに導入され、処理後ガスＢが排出される。一方、吸引口バルブ２３ａ，２３ｂの先には真空ポンプ１７が設けてあり、脱離された溶剤のガスを含む減圧された有機化合物同伴ガスＤが真空吸引される。真空吸引されて大気圧に戻された高濃度ガスＥは、コンデンサ１８ｂで冷却水Ｇにより冷却される。これにより、高濃度ガスＥに含まれた溶剤は液化した回収有機化合物Ｆとして回収される。 An operation example in which the volatile organic compound adsorbed on the adsorbent of the adsorption tower is desorbed by vacuum suction will be described with reference to FIG. Two adsorption towers 11a and 11b (collectively referred to as 11) are provided in parallel, and the adsorbent accommodating portions 12a and 12b (collectively referred to as 11) are filled with an adsorbent for adsorbing a solvent which is a volatile organic compound. 12) is provided. Introductory valves 21a and 21b for introducing the volatile organic compound-containing gas A into the suction towers 11a and 11b, and suction port valves 23a and 23b for vacuum-sucking the gas in the tower are provided. There is. On the other hand, discharge port valves 22a and 22b are provided below the adsorption towers 11a and 11b to discharge the treated gas B after the solvent is adsorbed. A raw gas blower 16 is provided at the tip of the outlet valves 22a and 22b. Due to the pressure generated by the raw gas blower 16, the volatile organic compound-containing gas A is introduced into the adsorption towers 11a and 11b, and the treated gas B is discharged. On the other hand, a vacuum pump 17 is provided at the tip of the suction port valves 23a and 23b, and the decompressed organic compound-accompanied gas D containing the desorbed solvent gas is vacuum-sucked. The high-concentration gas E that has been evacuated and returned to atmospheric pressure is cooled by the cooling water G in the condenser 18b. As a result, the solvent contained in the high-concentration gas E is recovered as the liquefied recovered organic compound F.

それぞれの導入口バルブ２１ａ，２１ｂ（まとめて２１という）、排出口バルブ２２ａ，２２ｂ（まとめて２２という）、吸引口バルブ２３ａ，２３ｂ（まとめて２３という）は、独立して開閉可能である。これらを、吸着を行う吸着塔１１と、脱離を行う吸着塔１１とで切り替える。吸着を担当する方の吸着塔１１では、導入口バルブ２１と排出口バルブ２２とが開放され、吸引口バルブ２３が閉鎖される。導入口２１から導入された揮発性有機化合物含有ガスＡは吸着剤収容部１２の吸着剤に溶剤を吸収されて、溶剤含有量を抑制され、原ガスブロワ１６から大気へ放出される。一方、脱離して再生させている方の吸着塔１１では、導入口バルブ２１と排出口バルブ２２とが閉鎖され、吸引口バルブ２３が開放される。吸着塔１１内は減圧されて、吸着剤収容部１２の吸着剤に吸着していた溶剤が脱離されて吸引され、コンデンサ１８ｂで凝縮されて回収される。 The inlet valves 21a and 21b (collectively referred to as 21), the outlet valves 22a and 22b (collectively referred to as 22), and the suction port valves 23a and 23b (collectively referred to as 23) can be opened and closed independently. These are switched between the adsorption tower 11 for adsorption and the adsorption tower 11 for desorption. In the suction tower 11 which is in charge of suction, the introduction port valve 21 and the discharge port valve 22 are opened, and the suction port valve 23 is closed. The volatile organic compound-containing gas A introduced from the introduction port 21 is absorbed by the adsorbent in the adsorbent accommodating portion 12, the solvent content is suppressed, and the gas A is released from the raw gas blower 16 into the atmosphere. On the other hand, in the suction tower 11 that is detached and regenerated, the introduction port valve 21 and the discharge port valve 22 are closed, and the suction port valve 23 is opened. The pressure inside the adsorption tower 11 is reduced, the solvent adsorbed on the adsorbent in the adsorbent accommodating portion 12 is desorbed and sucked, and the solvent is condensed and recovered by the capacitor 18b.

当然のことながら、吸着塔１１の吸着能力を十全に再生させるためには、十分に揮発性有機化合物を脱離させる必要がある。そのためには減圧させる真空ポンプ１７には十分な能力が求められる。 As a matter of course, in order to fully regenerate the adsorption capacity of the adsorption tower 11, it is necessary to sufficiently desorb the volatile organic compounds. For that purpose, the vacuum pump 17 for depressurizing is required to have sufficient capacity.

特開２０１４−１６８７４１号公報Japanese Unexamined Patent Publication No. 2014-168741 特開平６−６３３５０号公報Japanese Unexamined Patent Publication No. 6-63350

しかしながら、脱離開始時には吸着塔内の圧力は大気圧であり、真空ポンプから排気されるガス量は開始直後に極端に大きくなる。このピークのガス量を処理可能とするには、処理能力が特に大きなコンデンサを設置しなければならなかった。だが、ピークを経過した後はそれほど大きな処理能力を必要としないため、コンデンサの運用能力には無駄が多かった。 However, at the start of desorption, the pressure inside the adsorption tower is atmospheric pressure, and the amount of gas exhausted from the vacuum pump becomes extremely large immediately after the start. In order to be able to process this peak gas volume, it was necessary to install a capacitor with a particularly large processing capacity. However, after the peak, the operating capacity of the capacitor was wasteful because it did not require so much processing power.

そこでこの発明は、減圧によって脱離させる揮発性有機化合物の処理装置において、処理に必要な負荷を低減させることを目的とする。 Therefore, an object of the present invention is to reduce the load required for treatment in a volatile organic compound processing apparatus that is desorbed by reduced pressure.

この発明は、
揮発性有機化合物を吸着する活性炭を充填する吸着剤収容部を有する吸着塔により、揮発性有機化合物含有ガスの揮発性有機化合物濃度を前記活性炭に吸着させることで減少させ、
吸着後は前記吸着塔内の気体を真空ポンプにより吸引して減圧させることで前記活性炭から前記揮発性有機化合物を脱離させる揮発性有機化合物処理装置を運用するにあたり、
前記吸着塔と前記真空ポンプとの間に、通過風量が異なる二本以上のルートを有する並列区間を設け、
それぞれのルートには独立して動作可能な弁を有し、
前記脱離を開始する際に、比較的通過風量が小さな前記ルートの弁を開放させた後に、比較的通過風量が大きな前記ルートの弁を開放させる運用方法により、上記の課題を解決したのである。 This invention
The concentration of volatile organic compounds in the volatile organic compound-containing gas is reduced by adsorbing the volatile organic compounds on the activated carbon by means of an adsorption tower having an adsorbent accommodating portion filled with activated carbon that adsorbs volatile organic compounds.
In operating a volatile organic compound processing apparatus that desorbs the volatile organic compound from the activated carbon by sucking the gas in the adsorption tower with a vacuum pump and reducing the pressure after adsorption.
A parallel section having two or more routes having different passing air volumes is provided between the suction tower and the vacuum pump.
Each route has a valve that can operate independently
At the start of the desorption, the above problem was solved by an operation method in which the valve of the route having a relatively small passing air volume was opened and then the valve of the route having a relatively large passing air volume was opened. ..

これは次のような新たな知見に基づくものである。吸着を終えた吸着塔について脱離を開始するにあたって、まず比較的通過風量が小さな前記ルートの弁を開放させると、吸着塔内が緩やかに減圧され始める。比較的通過風量が小さなとは、後から開放させる比較的通過風量が大きなルートに比べて小さいことをいい、バルブなどで調整する。概ね、比率にして１／３以下に小さいことが望ましい。 This is based on the following new findings. When the adsorption tower that has finished adsorption is started to be desorbed, first, when the valve of the route having a relatively small passing air volume is opened, the inside of the adsorption tower begins to be gradually depressurized. A relatively small passing air volume means that the passing air volume to be opened later is smaller than that of a route having a relatively large passing air volume, and is adjusted with a valve or the like. Generally, it is desirable that the ratio is as small as 1/3 or less.

通過風量が小さなルートのみ開放された場合、通過風量が大きなルートが開放された場合と比べて、脱離開始直後に真空ポンプに導入されるガスの体積は同じでも、吸着塔から供給されるガスの質量は減るので、真空ポンプの出口で大気圧に戻した段階での体積は減少することになる。すると、コンデンサが処理しなければならないガス量を抑制することができる。その上で、吸着塔内の圧力がある程度低下した段階で比較的通過風量が大きな前記ルートの弁を開放させると、真空ポンプに導入されるガスの体積は増大するが、既に圧力が低下しているため、真空ポンプの出口で大気圧に戻すと体積は大幅に縮小することになる。このため、真空ポンプの出口から排出されたコンデンサが処理しなければならないガス量の増加が抑制できる。このタイミングは、コンデンサに入る風量を１／ｎに抑えようとする場合、圧力が大気圧の１／ｎまで下がった段階で切り替えるとよい。 When only the route with a small passing air volume is opened, the gas supplied from the adsorption tower is the same as the case where the route with a large passing air volume is opened, even if the volume of gas introduced into the vacuum pump immediately after the start of desorption is the same. Since the mass of the gas is reduced, the volume at the stage of returning to atmospheric pressure at the outlet of the vacuum pump is reduced. Then, the amount of gas that the capacitor must process can be suppressed. Then, when the valve of the route having a relatively large passing air volume is opened when the pressure in the suction tower drops to some extent, the volume of the gas introduced into the vacuum pump increases, but the pressure has already dropped. Therefore, if the pressure is returned to atmospheric pressure at the outlet of the vacuum pump, the volume will be significantly reduced. Therefore, it is possible to suppress an increase in the amount of gas that must be processed by the condenser discharged from the outlet of the vacuum pump. This timing may be switched when the pressure drops to 1 / n of the atmospheric pressure when the air volume entering the condenser is to be suppressed to 1 / n.

単に、従来よりも通過風量が小さなルートのみで吸引すると、コンデンサへの負荷を抑えることができる代わりに、吸着塔内を十分に減圧させるために必要な時間がかかりすぎてしまう。この発明にかかる運用方法では、まず比較的通過風量が小さなルートで吸引して最初にコンデンサが処理する気体のピーク量を抑制する。その後所定の時間が経過した後に、比較的通過風量が大きなルートで吸引することで十分に減圧できるまでにかかる時間を抑制する。また、あらかじめ比較的通過風量が小さなルートで減圧させておくと、比較的通過風量が大きなルートを開放しても、コンデンサに到達するガス量の増大は十分に抑えることができる。 If suction is performed only by a route having a smaller passing air volume than before, the load on the condenser can be suppressed, but it takes too much time to sufficiently reduce the pressure inside the adsorption tower. In the operation method according to the present invention, first, the peak amount of the gas processed by the condenser is suppressed by sucking the gas through a route having a relatively small passing air volume. After a predetermined time has elapsed, the time required for sufficient decompression can be suppressed by sucking the air through a route having a relatively large air flow. Further, if the pressure is reduced in advance by a route having a relatively small passing air volume, an increase in the amount of gas reaching the condenser can be sufficiently suppressed even if the route having a relatively large passing air volume is opened.

コンデンサの入口に供給されるガス量と、コンデンサが有する必要がある伝熱面積とは比例関係にあり、ピーク時の風量を１／ｎにすれば、コンデンサが必要とする伝熱面積も１／ｎに抑制することができる。 The amount of gas supplied to the inlet of the condenser is proportional to the heat transfer area that the condenser needs to have, and if the peak air volume is set to 1 / n, the heat transfer area required by the condenser is also 1 / n. It can be suppressed to n.

この発明により、揮発性有機化合物の脱離に必要とするコンデンサの処理能力を抑制でき、運用上の負荷及びコストを下げ、揮発性有機化合物の処理を従来よりも省エネルギーで行うことができる。 According to the present invention, the processing capacity of the capacitor required for desorption of the volatile organic compound can be suppressed, the operational load and cost can be reduced, and the processing of the volatile organic compound can be performed with less energy than before.

この発明にかかる運用方法を実行する揮発性有機化合物処理装置の構成例図Configuration example diagram of a volatile organic compound processing apparatus that executes the operation method according to the present invention. ２基の吸着塔でこの発明にかかる運用方法を実行する吸着と脱着の状態遷移図State transition diagram of adsorption and desorption in which the operation method according to the present invention is executed by two adsorption towers. （ａ）脱離開始時点の吸引口付近の構成図、（ｂ）メイン側吸引口を開いた時点の構成図(A) Configuration diagram near the suction port at the start of desorption, (b) Configuration diagram at the time when the main suction port is opened 従来の真空吸引による脱離を実行する揮発性有機化合物処理装置の構成例図Configuration example diagram of a volatile organic compound processing device that performs desorption by conventional vacuum suction

以下、この発明の実施形態を説明する。この発明は、揮発性有機化合物含有ガスの濃度を低減させて大気中へ排出可能とし、その分の揮発性有機化合物を吸着剤に吸着させる揮発性有機化合物の処理装置１０の運用方法である。この処理装置１０で吸着を行う吸着塔１１は吸着剤として活性炭を有し、吸着された揮発性有機化合物は真空ポンプ１７で減圧されることで吸着剤から脱離させて、吸着剤を繰り返し利用できる。脱離させた揮発性有機化合物は凝縮して回収する。図１はこれらの一連のサイクルを行う処理装置１０の全体像の例を示す。 Hereinafter, embodiments of the present invention will be described. The present invention is an operation method of a volatile organic compound processing apparatus 10 that reduces the concentration of a volatile organic compound-containing gas so that it can be discharged into the atmosphere and adsorbs the volatile organic compound to the adsorbent. The adsorption tower 11 that adsorbs with this processing device 10 has activated carbon as an adsorbent, and the adsorbed volatile organic compounds are desorbed from the adsorbent by being depressurized by the vacuum pump 17, and the adsorbent is repeatedly used. it can. The desorbed volatile organic compounds are condensed and recovered. FIG. 1 shows an example of an overall image of the processing apparatus 10 that performs these series of cycles.

この発明にかかる運用方法で運用する処理装置で処理する揮発性有機化合物とは、常圧で加熱することで気体になり得る有機化合物であり、特に常温で液体であるものが吸着処理しやすい。例えば、メタノール、エタノール、イソプロピルアルコール等の炭素数が１〜８程度のアルコール、トルエン、ベンゼンなどの芳香族有機化合物などの、炭化水素系の溶剤が挙げられる。 The volatile organic compound processed by the processing apparatus operated by the operation method according to the present invention is an organic compound that can be turned into a gas by heating at normal pressure, and a compound that is liquid at room temperature is particularly easy to be adsorbed. Examples thereof include hydrocarbon solvents such as alcohols having about 1 to 8 carbon atoms such as methanol, ethanol and isopropyl alcohol, and aromatic organic compounds such as toluene and benzene.

個々の吸着塔１１（１１ａ，１１ｂ）は角形又は円筒形であり、装置内部には、揮発性有機化合物を吸着し、真空吸引にて脱着できる吸着剤を充填させた吸着剤収容部１２を設けてある。この吸着剤としては、粒状活性炭を用いることができる。吸着塔１１の内部を上下方向に通過するためには、必ず吸着剤収容部１２を通過しなければならない。吸着剤収容部１２の底面と上面はどちらも吸着塔１１内に格納されている。このような吸着塔１１が並列に複数基設けられている。図１の例では２基の吸着塔１１ａ，１１ｂを記載しているが、２基に限定されるものではなく、３基以上でもよい。 The individual adsorption towers 11 (11a, 11b) are square or cylindrical, and an adsorbent accommodating portion 12 filled with an adsorbent that adsorbs volatile organic compounds and can be desorbed by vacuum suction is provided inside the apparatus. There is. Granular activated carbon can be used as the adsorbent. In order to pass through the inside of the adsorption tower 11 in the vertical direction, it must pass through the adsorbent accommodating portion 12. Both the bottom surface and the top surface of the adsorbent accommodating portion 12 are stored in the adsorbent tower 11. A plurality of such adsorption towers 11 are provided in parallel. In the example of FIG. 1, two adsorption towers 11a and 11b are described, but the number is not limited to two, and may be three or more.

吸着塔１１の吸着剤収容部１２より上端側には、揮発性有機化合物含有ガスＡの導入口１３が設けてあり、原ガスブロワ１６によって生じた圧力によって揮発性有機化合物含有ガスＡが導入される。吸着剤収容部１２より下端側には、揮発性有機化合物が吸着剤に吸着されることでその濃度が低下した処理後ガスＢの排出口１４が設けてある。排出口１４は大気中へ放出するものである。 An introduction port 13 for the volatile organic compound-containing gas A is provided on the upper end side of the adsorbent accommodating portion 12 of the adsorption tower 11, and the volatile organic compound-containing gas A is introduced by the pressure generated by the raw gas blower 16. .. On the lower end side of the adsorbent accommodating portion 12, a discharge port 14 for the treated gas B whose concentration is reduced by adsorbing the volatile organic compound by the adsorbent is provided. The discharge port 14 discharges into the atmosphere.

また、揮発性有機化合物を脱着した有機化合物同伴ガスＤを減圧吸引するための吸引口１５が、吸着剤収容部１２の上端よりも上端側に設けてある。この吸引口１５から有機化合物同伴ガスＤが搬送される。 Further, a suction port 15 for sucking the organic compound-accompanied gas D to which the volatile organic compound has been desorbed under reduced pressure is provided on the upper end side of the adsorbent accommodating portion 12. The gas D accompanying the organic compound is conveyed from the suction port 15.

有機化合物同伴ガスＤは、真空ポンプ１７によって吸引されることで、減圧した状態で真空ポンプ１７に到達する。真空ポンプ１７の出口からは大気圧に戻って容積が小さくなった高濃度ガスＥが排出される。この高濃度ガスＥはコンデンサ１８ａに供給されて冷却水Ｇにより冷却される。冷却により有機化合物同伴ガスＤに含まれていた揮発性有機化合物を分離回収する（回収有機化合物Ｆ）。 The gas D accompanied by the organic compound reaches the vacuum pump 17 in a reduced pressure state by being sucked by the vacuum pump 17. High-concentration gas E, which has returned to atmospheric pressure and has a reduced volume, is discharged from the outlet of the vacuum pump 17. This high-concentration gas E is supplied to the condenser 18a and cooled by the cooling water G. The volatile organic compound contained in the gas D accompanying the organic compound is separated and recovered by cooling (recovered organic compound F).

それぞれの吸着塔１１への入口及び出口にはバルブを設けてある。すなわち、導入口１３ａ，１３ｂには導入口バルブ２１ａ，２１ｂを、排出口１４ａ，１４ｂには排出口バルブ２２ａ，２２ｂを、それぞれ設けてある。 Valves are provided at the inlet and outlet to each suction tower 11. That is, the introduction ports 13a and 13b are provided with the introduction port valves 21a and 21b, and the discharge ports 14a and 14b are provided with the discharge port valves 22a and 22b, respectively.

一方、吸引口１５から先は複数本に分岐し、並列区間が設けられ、真空ポンプ１７より手前で合流している。並列区間を構成する分岐したそれぞれのルートは、通過する風量が異なるように調整されている。図では吸着塔１１ａ，１１ｂごとに、２本に分岐している。分岐したうち、時間あたりの通過風量が比較的大きな方の経路をメインルート、比較的小さな方の経路をサブルートと呼ぶ。メインルートにはメインルートバルブ２３ａ，２３ｂを設け、サブルートにはサブルートバルブ２４ａ，２４ｂを設けてある。 On the other hand, the suction port 15 is branched into a plurality of lines, a parallel section is provided, and the suction port 15 merges before the vacuum pump 17. Each of the branched routes that make up the parallel section is adjusted so that the amount of air passing through it is different. In the figure, each of the adsorption towers 11a and 11b is branched into two. Of the branches, the route with a relatively large air flow per hour is called the main route, and the route with a relatively small air volume is called the sub route. The main route is provided with main route valves 23a and 23b, and the sub route is provided with sub route valves 24a and 24b.

前記メインルートと前記サブルートの時間あたりの通過風量の比率は２０：１〜３：１であることが好ましく、１０：１〜５：１であるとより好ましい。３：１よりも比が小さいと、脱離開始直後にピークとなるコンデンサ１８ａが処理すべき処理量を低減させる効果が十分に発揮されず、コンデンサ１８ａに要求される処理能力が十分に抑制できない。一方、２０：１よりも比が大きいと、前記サブルートを先行して開放させることで吸着塔１１内をある程度減圧させるために必要な時間が掛かりすぎてしまい、他方の吸着塔の吸着が終わるまでに脱離が完了しなかったり、減圧が不十分なまま前記メインルートを開放しなければならなくなってコンデンサ１８ａが処理すべき処理量のピークが十分に低減させられないおそれがある。 The ratio of the passing air volume of the main route to the sub route per hour is preferably 20: 1-3: 1, and more preferably 10: 1 to 5: 1. If the ratio is smaller than 3: 1, the effect of reducing the processing amount to be processed by the capacitor 18a, which peaks immediately after the start of desorption, is not sufficiently exhibited, and the processing capacity required for the capacitor 18a cannot be sufficiently suppressed. .. On the other hand, if the ratio is larger than 20: 1, it takes too much time to reduce the pressure inside the adsorption tower 11 to some extent by opening the subroute in advance, and until the adsorption of the other adsorption tower is completed. There is a possibility that the desorption is not completed or the main route must be opened with insufficient depressurization, so that the peak of the processing amount to be processed by the capacitor 18a cannot be sufficiently reduced.

なお、前記ルートが３本以上に分岐している場合には、後述する開放順に２番目になるルートと１番目になるルートとの通過風量の比率が前記の範囲であると好ましい。 When the route is branched into three or more, it is preferable that the ratio of the passing air volume between the second route and the first route in the opening order described later is in the above range.

上記の通過風量の比率を調整する手法としては、例えば前記サブルートに通過風量を調整できる通過風量調整バルブ２５ａ，２５ｂを設け、これを調整することで上記の範囲に調整することができる。 As a method for adjusting the ratio of the passing air volume, for example, the passing air volume adjusting valves 25a and 25b that can adjust the passing air volume are provided in the sub-route, and the passing air volume can be adjusted within the above range by adjusting the valves.

この発明にかかる揮発性有機化合物処理装置の運用方法について、図２に示すシーケンス図と、図３に示す状態図を用いて説明する。まず、吸着塔１１ａで吸着を開始する際には（Ｓ１０１）、導入口バルブ２１ａと、排出口バルブ２２ａを開放し、吸引口１５ａのサブルートバルブ２４ａ、メインルートバルブ２３ａは閉鎖する。吸着が終わったら導入口バルブ２１ａと、排出口バルブ２２ａを一旦閉鎖すると同時に、吸着塔１１ｂで吸着を開始する（Ｓ１０２）。次に、吸着塔１１ａでは脱離を開始する（Ｓ１０３〜）。このとき、まずサブルートバルブ２４ａを開放し、メインルートバルブ２３ａは閉鎖したままとする（Ｓ１０３）。このときの状態を図３（ａ）に示す。サブルートのみ開放されているため、通過風量が制限されており、吸着塔１１ａの中の減圧は緩やかに進行する。これにより、コンデンサ１８ａが処理しなければならないガス量も抑制されている。 The operation method of the volatile organic compound processing apparatus according to the present invention will be described with reference to the sequence diagram shown in FIG. 2 and the state diagram shown in FIG. First, when the suction tower 11a starts suction (S101), the introduction port valve 21a and the discharge port valve 22a are opened, and the sub-root valve 24a and the main route valve 23a of the suction port 15a are closed. When the suction is completed, the inlet valve 21a and the discharge valve 22a are temporarily closed, and at the same time, the suction tower 11b starts suction (S102). Next, the adsorption tower 11a starts desorption (S103 to). At this time, first, the sub-route valve 24a is opened, and the main route valve 23a is kept closed (S103). The state at this time is shown in FIG. 3 (a). Since only the sub-route is open, the amount of air passing through is limited, and the decompression in the adsorption tower 11a proceeds slowly. As a result, the amount of gas that the condenser 18a must process is also suppressed.

次に、サブルートの開放から、吸着塔１１ａ内の気圧が十分に低下したら、メインルートのメインルートバルブ２３ａを開放し、メインルートとサブルートの両方から吸引を行う（Ｓ１０４）。この状態を図３（ｂ）に示す。メインルートを通過する風量が増えるが、このときまでに既に吸着塔１１ａの内のガスはある程度抜けているので、コンデンサ１８ａが処理しなければならないガス量が過度に上がることを抑制している。ここで、Ｓ１０３からＳ１０４に切り替えるタイミングは、予め吸着塔１１ａ内の気圧の変動を測定しておき、最適と思われるタイミングになるようにタイマー制御しておいてもよいし、吸着塔１１ａ内に設けた圧力計の値を測定しながら、適切な気圧になった時点で切り替えてもよい。その後、吸着塔１１ａ内の圧力が十分に低下したら脱離を終了する（Ｓ１０５）。 Next, when the air pressure in the suction tower 11a drops sufficiently from the opening of the sub-route, the main route valve 23a of the main route is opened, and suction is performed from both the main route and the sub-route (S104). This state is shown in FIG. 3 (b). Although the amount of air passing through the main route increases, the gas in the adsorption tower 11a has already been released to some extent by this time, so that the amount of gas that the condenser 18a must process is suppressed from increasing excessively. Here, the timing of switching from S103 to S104 may be determined by measuring the fluctuation of the atmospheric pressure in the adsorption tower 11a in advance and controlling the timer so as to be the optimum timing, or in the adsorption tower 11a. While measuring the value of the provided pressure gauge, it may be switched when the appropriate atmospheric pressure is reached. After that, when the pressure in the adsorption tower 11a is sufficiently lowered, the desorption is completed (S105).

メインルートバルブ２３ａ，２３ｂを開放する時点（Ｓ１０３→Ｓ１０４，Ｓ１０６→Ｓ１０７）における吸着塔１１ａ、１１ｂ内の圧力は、５ｋＰａ以上であると好ましく、１０ｋＰａ以上であるとより好ましい。なお、５ｋＰａは大気圧の１／２０であり、１０ｋＰａは大気圧の１／１０に相当する。一方、３３ｋＰａ以下であると好ましく、２０ｋＰａ以下であるとより好ましい。なお、３３ｋＰａは大気圧の１／３であり、２０ｋＰａは大気圧の１／５に相当する。５ｋＰａ未満までサブルートのみで減圧するには時間が掛かりすぎ、脱離が間に合わなくなるおそれがある。一方、３３ｋＰａを超えていると、まだ残存しているガスが多いため、メインルートバルブ２３ａ，２３ｂを開放したときにコンデンサ１８ａにかかる負荷が大きくなりすぎてしまう。 The pressure in the suction towers 11a and 11b at the time when the main route valves 23a and 23b are opened (S103 → S104, S106 → S107) is preferably 5 kPa or more, and more preferably 10 kPa or more. Note that 5 kPa is 1/20 of the atmospheric pressure, and 10 kPa corresponds to 1/10 of the atmospheric pressure. On the other hand, it is preferably 33 kPa or less, and more preferably 20 kPa or less. 33 kPa is 1/3 of the atmospheric pressure, and 20 kPa is 1/5 of the atmospheric pressure. It takes too much time to reduce the pressure to less than 5 kPa with only the subroute, and there is a risk that desorption will not be in time. On the other hand, if it exceeds 33 kPa, a large amount of gas still remains, so that the load applied to the condenser 18a becomes too large when the main route valves 23a and 23b are opened.

なお、メインルートバルブ２３ａ，２３ｂを開放した後、吸着塔１１ａ，１１ｂ内が所定の気圧以下になるまで減圧し、吸着剤から揮発性有機化合物を脱離させる。この減圧停止気圧は、溶剤の種類によって適宜変更してよい値である。なお、この終了タイミングは吸着塔１１ａ、１１ｂ内に設けた圧力計を基準にして終了してもよいし、過去の運用時における測定から、目標とする圧力にまで低下したと判断できる時点で終了してもよい。ただし、吸着を続けている吸着塔１１ｂの吸着能力の低下が限界に達する前に終了する必要がある。 After opening the main route valves 23a and 23b, the pressure inside the adsorption towers 11a and 11b is reduced to a predetermined pressure or less to desorb the volatile organic compounds from the adsorbent. This decompression stop pressure is a value that may be appropriately changed depending on the type of solvent. The end timing may be ended based on the pressure gauges provided in the suction towers 11a and 11b, or ends when it can be determined from the measurement in the past operation that the pressure has dropped to the target pressure. You may. However, it is necessary to finish before the decrease in the adsorption capacity of the adsorption tower 11b, which continues to adsorb, reaches the limit.

次に、脱離によって吸着能力を取り戻した吸着塔１１ａで再度吸着を行う（Ｓ１０６）。このとき、吸着塔１１ｂではまずサブルートバルブ２４ｂのみを開放して、吸引減圧させて脱離を開始させる。その後吸着塔１１ｂ内の圧力が上記の範囲となったら、メインルートバルブ２３ｂを開放する（Ｓ１０７）。その後、吸着塔１１ｂ内の圧力が十分に低下したら脱離を終了する（Ｓ１０８）。これらのタイミングの基準となる吸着塔１１ｂ内の圧力は、吸着塔１１ａでの脱離の際の基準と同じである。以後（Ｓ１０９〜）、交互に吸着と脱離を繰り返すたびに、脱離の際には先にサブルートを開放し、次いでメインルートを開放する。 Next, adsorption is performed again in the adsorption tower 11a, which has regained its adsorption capacity by desorption (S106). At this time, in the suction tower 11b, only the sub-root valve 24b is first opened, the suction pressure is reduced, and the desorption is started. After that, when the pressure in the suction tower 11b falls within the above range, the main route valve 23b is opened (S107). After that, when the pressure in the adsorption tower 11b is sufficiently lowered, the desorption is completed (S108). The pressure in the adsorption tower 11b, which is the reference for these timings, is the same as the reference for desorption in the adsorption tower 11a. After that (S109 ~), each time the adsorption and desorption are repeated alternately, the sub route is opened first and then the main route is released at the time of desorption.

以下、この発明の実施例を示す。（株）栗本鐵工所製吸着塔（活性炭層面積：０．１ｍ２、活性炭層厚：１．０ｍ）に、通過風速０．１６ｍ／ｓとなるように、トルエン濃度１％となる揮発性有機化合物含有ガスＡを導入し、吸着時間１０分となるように吸着を行った。 Hereinafter, examples of the present invention will be shown. Volatile with a toluene concentration of 1% so that the passing air velocity is 0.16 m / s in the adsorption tower (activated carbon layer area: 0.1 m 2 , activated carbon layer thickness: 1.0 m) manufactured by Kurimoto, Ltd. The organic compound-containing gas A was introduced, and adsorption was carried out so that the adsorption time was 10 minutes.

メインルート及びサブルートの通過風量の比は５：１であり、真空ポンプの能力は２ｍ３／ｍｉｎのものを用いた。コンデンサとしては多管式のもの（伝熱面積：０．２ｍ２）を用いた。サブルートで２０ｋＰａとなるまで減圧した後に、メインルートを開放したところ、コンデンサは十分にガスを処理可能であった。 The ratio of the passing air volume of the main route and the sub route was 5: 1, and the capacity of the vacuum pump used was 2 m 3 / min. A multi-tube type capacitor (heat transfer area: 0.2 m 2 ) was used. When the main route was opened after the pressure was reduced to 20 kPa on the sub route, the capacitor was able to sufficiently process the gas.

比較例として、サブルートを持たずメインルートのみの装置を用いて、大気圧の時点でメインルートを開放して吸引を行ったところ、実施例のコンデンサでは能力が不足してしまい、伝熱面積が１．０ｍ２である多管式コンデンサが必要となった。 As a comparative example, when suction was performed by opening the main route at the time of atmospheric pressure using a device having only the main route without a sub route, the capacity of the capacitor of the embodiment was insufficient and the heat transfer area was increased. A multi-tube capacitor of 1.0 m 2 was required.

１０ 処理装置
１１，１１ａ，１１ｂ 吸着塔
１２，１２ａ，１２ｂ 活性炭（吸着剤収容部）
１３，１３ａ，１３ｂ 導入口
１４，１４ａ，１４ｂ 排出口
１５，１５ａ，１５ｂ 吸引口
１６ 原ガスブロワ
１７ 真空ポンプ
１８ａ，１８ｂ コンデンサ
２１，２１ａ，２１ｂ 導入口バルブ
２２，２２ａ，２２ｂ 排出口バルブ
２３，２３ａ，２３ｂ メインルートバルブ（吸引口バルブ）
２４ａ，２４ｂ サブルートバルブ
２５ａ，２５ｂ 通過風量調整バルブ
Ａ 揮発性有機化合物含有ガス
Ｂ 処理後ガス
Ｄ 有機化合物同伴ガス
Ｅ 高濃度ガス
Ｇ 冷却水
Ｆ 回収有機化合物 10 Processing equipment 11, 11a, 11b Adsorption tower 12, 12a, 12b Activated carbon (adsorbent storage unit)
13, 13a, 13b Introductory port 14, 14a, 14b Outlet port 15, 15a, 15b Suction port 16 Raw gas blower 17 Vacuum pump 18a, 18b Condenser 21, 21a, 21b Introductory port valve 22, 22a, 22b Outlet valve 23, 23a , 23b Main route valve (suction port valve)
24a, 24b Subroot valve 25a, 25b Passing air volume adjustment valve A Volatile organic compound-containing gas B Treated gas D Organic compound companion gas E High concentration gas G Cooling water F Recovered organic compound

Claims (4)

揮発性有機化合物を吸着する活性炭を充填する吸着剤収容部を有する吸着塔により、揮発性有機化合物含有ガスの揮発性有機化合物濃度を前記活性炭に吸着させることで減少させ、
吸着後は前記吸着塔内の気体を真空ポンプにより吸引して減圧させることで前記活性炭から前記揮発性有機化合物を脱離させる揮発性有機化合物処理装置を運用するにあたり、
前記吸着塔と前記真空ポンプとの間に、通過風量が異なる二本以上のルートを有する並列区間を設け、
それぞれのルートには独立して動作可能な弁を有し、
前記脱離を開始する際に、比較的通過風量が小さな前記ルートの弁を開放させた後に、比較的通過風量が大きな前記ルートの弁を開放させる、
揮発性有機化合物処理装置の運用方法。 The concentration of volatile organic compounds in the volatile organic compound-containing gas is reduced by adsorbing the volatile organic compounds on the activated carbon by means of an adsorption tower having an adsorbent accommodating portion filled with activated carbon that adsorbs volatile organic compounds.
In operating a volatile organic compound processing apparatus that desorbs the volatile organic compound from the activated carbon by sucking the gas in the adsorption tower with a vacuum pump and reducing the pressure after adsorption.
A parallel section having two or more routes having different passing air volumes is provided between the suction tower and the vacuum pump.
Each route has a valve that can operate independently
At the start of the desorption, the valve of the route having a relatively small passing air volume is opened, and then the valve of the route having a relatively large passing air volume is opened.
Operation method of volatile organic compound processing equipment. 比較的通過風量が大きな前記ルートと、比較的通過風量が小さな前記ルートとの、通過風量の比が、２０：１〜３：１である、請求項１に記載の揮発性有機化合物処理装置の運用方法。 The volatile organic compound processing apparatus according to claim 1, wherein the ratio of the passing air volume between the route having a relatively large passing air volume and the route having a relatively small passing air volume is 20: 1-3: 1. Operation method. 前記真空ポンプから排出された高濃度ガスを冷却するコンデンサを有し、
前記コンデンサにて前記高濃度ガスに含まれる前記揮発性有機化合物を凝縮させる、
請求項１又は２に記載の揮発性有機化合物処理装置の運用方法。 It has a condenser that cools the high-concentration gas discharged from the vacuum pump.
The condenser condenses the volatile organic compound contained in the high-concentration gas.
The method for operating the volatile organic compound processing apparatus according to claim 1 or 2. 揮発性有機化合物を吸着する活性炭を充填する吸着剤収容部を有し、揮発性有機化合物含有ガスの揮発性有機化合物濃度を前記活性炭に吸着させることで減少させることができる吸着塔と、
吸着がされた前記吸着塔内の気体を吸引して減圧させることで前記活性炭から前記揮発性有機化合物を脱離させるための真空ポンプと、を有し、
前記吸着塔と前記真空ポンプとの間に、通過風量が異なる二本以上のルートを有する並列区間を設け、
それぞれのルートには独立して動作可能な弁を有し、
前記脱離を開始する際に、比較的通過風量が小さな前記ルートの弁を開放させた後に、比較的通過風量が大きな前記ルートの弁を開放させる、
揮発性有機化合物処理装置。 An adsorption tower that has an adsorbent accommodating portion filled with activated carbon that adsorbs volatile organic compounds, and can reduce the concentration of volatile organic compounds in the volatile organic compound-containing gas by adsorbing it on the activated carbon.
It has a vacuum pump for desorbing the volatile organic compound from the activated carbon by sucking the adsorbed gas in the adsorption tower and reducing the pressure.
A parallel section having two or more routes having different passing air volumes is provided between the suction tower and the vacuum pump.
Each route has a valve that can operate independently
At the start of the desorption, the valve of the route having a relatively small passing air volume is opened, and then the valve of the route having a relatively large passing air volume is opened.
Volatile organic compound processing equipment.
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CN112275089A (en) * 2020-10-15 2021-01-29 河南中烟工业有限责任公司 Effluent disposal polluted gas purification system

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US5154735A (en) * 1990-03-29 1992-10-13 John Zink Company, A Division Of Koch Engineering Co., Inc. Process for recovering hydrocarbons from air-hydrocarbon vapor mixtures
JPH0663350A (en) * 1992-08-24 1994-03-08 Ebara Corp Method for recovering solvent
JP2012066250A (en) * 2012-01-06 2012-04-05 Jfe Engineering Corp Method for removing and recovering volatile organic compound
WO2014080984A1 (en) * 2012-11-22 2014-05-30 Uji Shigekazu Device for recovering volatile organic compound

Patent Citations (4)

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Publication number Priority date Publication date Assignee Title
US5154735A (en) * 1990-03-29 1992-10-13 John Zink Company, A Division Of Koch Engineering Co., Inc. Process for recovering hydrocarbons from air-hydrocarbon vapor mixtures
JPH0663350A (en) * 1992-08-24 1994-03-08 Ebara Corp Method for recovering solvent
JP2012066250A (en) * 2012-01-06 2012-04-05 Jfe Engineering Corp Method for removing and recovering volatile organic compound
WO2014080984A1 (en) * 2012-11-22 2014-05-30 Uji Shigekazu Device for recovering volatile organic compound

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112275089A (en) * 2020-10-15 2021-01-29 河南中烟工业有限责任公司 Effluent disposal polluted gas purification system

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