JP7435367B2 - Organic solvent recovery system - Google Patents
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- JP7435367B2 JP7435367B2 JP2020144541A JP2020144541A JP7435367B2 JP 7435367 B2 JP7435367 B2 JP 7435367B2 JP 2020144541 A JP2020144541 A JP 2020144541A JP 2020144541 A JP2020144541 A JP 2020144541A JP 7435367 B2 JP7435367 B2 JP 7435367B2
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- 239000003960 organic solvent Substances 0.000 title claims description 98
- 238000011084 recovery Methods 0.000 title claims description 34
- 238000001816 cooling Methods 0.000 claims description 72
- 238000003795 desorption Methods 0.000 claims description 47
- 238000001179 sorption measurement Methods 0.000 claims description 41
- 238000000034 method Methods 0.000 claims description 21
- 238000004519 manufacturing process Methods 0.000 claims description 10
- 238000009833 condensation Methods 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims description 6
- 239000003507 refrigerant Substances 0.000 claims description 5
- 238000005192 partition Methods 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 150
- 239000003463 adsorbent Substances 0.000 description 12
- 230000008929 regeneration Effects 0.000 description 9
- 238000011069 regeneration method Methods 0.000 description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 238000010926 purge Methods 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 3
- 229910021536 Zeolite Inorganic materials 0.000 description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 239000010457 zeolite Substances 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 2
- DIOQZVSQGTUSAI-UHFFFAOYSA-N decane Chemical compound CCCCCCCCCC DIOQZVSQGTUSAI-UHFFFAOYSA-N 0.000 description 2
- 230000006866 deterioration Effects 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000002209 hydrophobic effect Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- ZFPGARUNNKGOBB-UHFFFAOYSA-N 1-Ethyl-2-pyrrolidinone Chemical compound CCN1CCCC1=O ZFPGARUNNKGOBB-UHFFFAOYSA-N 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- FXHOOIRPVKKKFG-UHFFFAOYSA-N N,N-Dimethylacetamide Chemical compound CN(C)C(C)=O FXHOOIRPVKKKFG-UHFFFAOYSA-N 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
- 238000009736 wetting Methods 0.000 description 1
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Description
本発明は、有機溶剤を含有する排ガスから有機溶剤を濃縮および回収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 for concentrating and recovering organic solvents from exhaust gas containing organic solvents.
従来、有機溶剤を含有する排ガスから有機溶剤を回収する処理システムとして、冷却凝縮装置および吸着素子を使用した濃縮装置を組み合わせたものが知られている。冷却凝縮装置は、有機溶剤を凝縮回収し、排ガス中の有機溶剤濃度を低減させる。吸着素子を使用した濃縮装置は、冷却凝縮装置から排出された有機溶剤濃度が低減された排ガスを吸着素子に接触させて有機溶剤を吸着させて更に排ガス中の有機溶剤濃度を低減させるとともに、有機溶剤を吸着した吸着材に高温のガスを吹き付けて有機溶剤を脱着させて高濃度の有機溶剤を含有する脱着ガスとして排出する。脱着ガスは冷却凝縮装置に返送され、再処理される（特許文献１、２参照）。 BACKGROUND ART Conventionally, as a treatment system for recovering organic solvents from exhaust gas containing organic solvents, a combination of a cooling condensing device and a concentrating device using an adsorption element is known. The cooling condensing device condenses and recovers the organic solvent to reduce the concentration of the organic solvent in the exhaust gas. A concentrator using an adsorption element brings the flue gas discharged from the cooling condensation equipment, which has a reduced concentration of organic solvent, into contact with the adsorption element to adsorb the organic solvent, further reducing the concentration of organic solvent in the flue gas, and High-temperature gas is blown onto the adsorbent that has adsorbed the solvent to desorb the organic solvent and discharge it as a desorption gas containing a high concentration of organic solvent. The desorbed gas is returned to the cooling condensation device and reprocessed (see Patent Documents 1 and 2).
生産設備においては、一定量のクリーンガスが補給される。従って、補給ガス分の排ガスが外部環境へ排出される。近年、世界的な排ガス規制に伴い、極低濃度までの有機溶剤の除去が求められており、高度な処理効率が求められる。 Production facilities are supplied with a certain amount of clean gas. Therefore, exhaust gas equivalent to the makeup gas is discharged to the outside environment. In recent years, with global exhaust gas regulations, there has been a need to remove organic solvents down to extremely low concentrations, and a high level of processing efficiency is required.
本発明は上記課題を背景になされたもので、排ガスから有機溶剤をより高効率に回収することが可能な有機溶剤回収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 was made in view of the above problems, and an object of the present invention is to provide an organic solvent recovery system that can recover organic solvents from exhaust gas with higher efficiency.
本発明者らは、上記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到った。即ち本発明は、以下の通りである。
１．生産設備から排出される有機溶剤を含有する排ガスから前記有機溶剤を回収する有機溶剤回収システムであって、前記有機溶剤を含有する前記排ガスを冷却することで、前記有機溶剤を液化凝縮し、前記有機溶剤の濃度が低減された冷却処理ガスとして排出する冷却凝縮装置と、前記冷却処理ガスを通流させる第一通流経路と、前記第一通流経路から導入された前記冷却処理ガスに含まれる前記有機溶剤を第一吸着素子にて吸着して前記有機溶剤の濃度が更に低減された第一処理ガスとして排出し、高温ガスを導入して前記第一吸着素子から前記有機溶剤を脱着して第一脱着ガスとして排出する第一濃縮装置と、前記第一処理ガスの一部を通流させる第二通流経路と、前記第二通流経路から導入された前記第一処理ガスに含まれる前記有機溶剤を第二吸着素子にて吸着して前記有機溶剤の濃度が更に低減された第二処理ガスとして排出し、高温ガスを導入して前記第二吸着素子から前記有機溶剤を脱着して第二脱着ガスとして排出する第二濃縮装置と、前記第一脱着ガスおよび前記第二脱着ガスを前記冷却凝縮装置に戻す第三通流経路と、を備えた、有機溶剤回収システム。
２．前記冷却凝縮装置は、前記冷却後の前記排ガスを接触させることで凝縮した前記有機溶剤と前記冷却処理ガスとを分離させる網目状構造体と、前記網目状構造体を通過後の前記冷却処理ガスを一定時間貯留させるチャンバーと、をさらに備え、前記第一通流経路は、前記チャンバーの天井部から前記冷却処理ガスを前記第一濃縮装置に導入するように設置されている、上記１に記載の有機溶剤回収システム。
３．前記チャンバーは、前記網目状構造体から排出される前記冷却処理ガスの排気方向と対向するように前記第一通流経路の吸込みを可能にする仕切部を有する、上記２に記載の有機溶剤回収システム。
４．前記冷却凝縮装置は、冷媒との熱交換により前記冷却を行う熱交換器をさらに備える、上記１から上記３のいずれか１つに記載の有機溶剤回収システム。
５．前記第二通流経路から排出される前記第一処理ガスの一部以外である前記第一処理ガスの残部を、前記生産設備に戻す返却経路をさらに備える、上記１から上記４のいずれか１つに記載の有機溶剤回収システム。
６．前記熱交換器は、第一熱交換器と、前記第一熱交換器の前段に設けた第二熱交換器とを含み、前記第二熱交換器は、前記冷却凝縮装置に導入される前記排ガスを、前記第一処理ガスの残部との熱交換により冷却する、上記４または上記５に記載の有機溶剤回収システム。
また、以下の構成を備えてもよい。
１．有機溶剤を含有する排ガスを冷却することで、前記有機溶剤を液化凝縮し、前記有機溶剤の濃度が低減された冷却処理ガスとして排出する冷却凝縮装置と、前記冷却処理ガスの一部を通流させる第一通流経路と、吸着素子を有し、前記第一通流経路から導入された前記冷却処理ガスに含まれる前記有機溶剤を前記吸着素子にて吸着して前記有機溶剤の濃度が更に低減された清浄ガスとして排出し、高温ガスを導入して前記吸着素子から前記有機溶剤を脱着して脱着ガスとして排出する濃縮装置と、前記脱着ガスを前記冷却凝縮装置に導入する第二通流経路と、を備えた有機溶剤回収システムにおいて、前記冷却凝縮装置は、冷却後の前記排ガスを接触させることで凝縮した前記有機溶剤と前記冷却処理ガスとを分離させる網目状構造体と、当該網目状構造体を通過後の前記冷却処理ガスを一定時間貯留させるチャンバーとを備え、前記第一通流経路は、前記チャンバーの天井部から前記冷却処理ガスの一部を前記濃縮装置に導入するように設置されていることを特徴とする有機溶剤回収システム。
２．前記チャンバーは、前記網目状構造体から排出される冷却処理ガスの排気方向と対向するように前記第一通流経路の吸込みを可能にする仕切部を有することを特徴とする上記１に記載の有機溶剤回収システム。
３．前記冷却凝縮装置は、冷媒との熱交換により前記冷却を行う熱交換器を備えることを特徴とする上記１または２に記載の有機溶剤回収システム。
４．前記第二通流経路は、前記脱着部が前記脱着ガスと前記排気ガスとの合流位置より上部に設置されていることを特徴とする上記１から３のいずれか１つに記載の有機溶剤回収システム。
５．前記排ガスは生産設備から排出されるガスであり、前記第一通流経路から排出される前記冷却処理ガスの一部以外である前記冷却処理ガスの残部を、前記生産設備に戻す返却経路を備えていることを特徴とする上記１から４のいずれか１つに記載の有機溶剤回収システム。
６．前記冷却凝縮装置に導入される排ガスを、前記冷却処理ガスの残部との熱交換により冷却する第二熱交換器を、前記第一熱交換器の前段に備えていることを特徴とする上記５に記載の有機溶剤回収システム。
In order to solve the above-mentioned problems, the inventors of the present invention have made extensive studies and have finally completed the present invention. That is, the present invention is as follows.
1. An organic solvent recovery system that recovers the organic solvent from exhaust gas containing the organic solvent discharged from production equipment, the organic solvent is liquefied and condensed by cooling the exhaust gas containing the organic solvent, and the organic solvent is liquefied and condensed. a cooling condensing device that discharges a cooled processing gas with a reduced concentration of an organic solvent; a first flow path through which the cooled processing gas flows; The organic solvent is adsorbed by a first adsorption element and discharged as a first treatment gas in which the concentration of the organic solvent is further reduced, and high-temperature gas is introduced to desorb the organic solvent from the first adsorption element. a first concentrator that discharges the gas as a first desorption gas; a second flow path through which a portion of the first processing gas flows; The organic solvent is adsorbed by a second adsorption element and discharged as a second treated gas in which the concentration of the organic solvent is further reduced, and high-temperature gas is introduced to desorb the organic solvent from the second adsorption element. An organic solvent recovery system comprising: a second concentrating device for discharging the first desorbing gas and the second desorbing gas as a second desorbing gas; and a third flow path for returning the first desorbing gas and the second desorbing gas to the cooling condensing device.
2. The cooling condensing device includes a network structure that separates the condensed organic solvent and the cooling process gas by bringing the cooled exhaust gas into contact with each other, and a network structure that separates the cooling process gas after passing through the network structure. The method according to 1 above, further comprising a chamber for storing the gas for a certain period of time, and the first flow path is installed so as to introduce the cooled processing gas into the first concentrator from the ceiling of the chamber. organic solvent recovery system.
3. The organic solvent recovery according to 2 above, wherein the chamber has a partition portion that allows suction into the first flow path so as to face the exhaust direction of the cooling processing gas discharged from the network structure. system.
4. The organic solvent recovery system according to any one of 1 to 3 above, wherein the cooling condensing device further includes a heat exchanger that performs the cooling by heat exchange with a refrigerant.
5. Any one of 1 to 4 above, further comprising a return path for returning the remainder of the first processing gas other than a part of the first processing gas discharged from the second flow path to the production equipment. Organic solvent recovery system described in .
6. The heat exchanger includes a first heat exchanger and a second heat exchanger provided upstream of the first heat exchanger, and the second heat exchanger includes the 6. The organic solvent recovery system according to 4 or 5 above, wherein the exhaust gas is cooled by heat exchange with the remainder of the first treated gas.
Further, the following configuration may be provided.
1. A part of the cooled gas is passed through a cooling condensing device that cools the exhaust gas containing the organic solvent, liquefies and condenses the organic solvent, and discharges it as a cooled gas with a reduced concentration of the organic solvent. the organic solvent contained in the cooled gas introduced from the first flow path is adsorbed by the adsorption element to further increase the concentration of the organic solvent; a concentrator for discharging the organic solvent as a reduced clean gas and introducing a high-temperature gas to desorb the organic solvent from the adsorption element and discharging it as a desorption gas; and a second flow for introducing the desorption gas into the cooling condensation device. In the organic solvent recovery system, the cooling condensing device includes a network structure that separates the organic solvent condensed by contacting the cooled exhaust gas from the cooled processing gas; a chamber for storing the cooled processing gas for a certain period of time after passing through the shaped structure, and the first flow path is configured to introduce a part of the cooled processing gas into the concentrator from the ceiling of the chamber. An organic solvent recovery system that is installed in
2. 1 above, wherein the chamber has a partition portion that allows suction into the first flow path so as to face the exhaust direction of the cooling process gas discharged from the mesh structure. Organic solvent recovery system.
3. 3. The organic solvent recovery system as described in 1 or 2 above, wherein the cooling condensing device includes a heat exchanger that performs the cooling by heat exchange with a refrigerant.
4. The organic solvent recovery according to any one of 1 to 3 above, wherein the second flow path is such that the desorption section is installed above a position where the desorption gas and the exhaust gas meet. system.
5. The exhaust gas is gas discharged from the production equipment, and includes a return route for returning the remainder of the cooling processing gas other than a part of the cooling processing gas discharged from the first flow path to the production equipment. 5. The organic solvent recovery system according to any one of 1 to 4 above.
6. 5 above, characterized in that a second heat exchanger that cools the exhaust gas introduced into the cooling condensing device by heat exchange with the remainder of the cooling process gas is provided at a stage upstream of the first heat exchanger. The organic solvent recovery system described in .
本発明による有機溶剤回収システムは、上記構成により、高効率に有機溶剤の回収および外部環境への有機溶剤の排出量を削減できる。 With the above configuration, the organic solvent recovery system according to the present invention can highly efficiently recover organic solvents and reduce the amount of organic solvents discharged into the external environment.
以下、本発明の実施の形態について、図を参照して詳細に説明する。なお、以下に示す図の実施の形態においては、同一または対応する部分については、適宜省略し、その説明についても繰り返さないことにする。 Hereinafter, embodiments of the present invention will be described in detail with reference to the drawings. In the embodiments shown in the figures below, the same or corresponding parts will be omitted as appropriate, and the description thereof will not be repeated.
図１は、本発明の実施の形態における有機溶剤回収システム１の構成図である。有機溶剤回収システム１は、冷却凝縮装置１００、濃縮装置２００、第一通流経路３００、第二通流経路４００とで構成されている。 FIG. 1 is a configuration diagram of an organic solvent recovery system 1 in an embodiment of the present invention. The organic solvent recovery system 1 includes a cooling condensing device 100, a concentrating device 200, a first flow path 300, and a second flow path 400.
冷却凝縮装置１００は、冷却部１１０と分離部１２０およびチャンバー１２３を有している。有機溶剤を含有する排ガス（Ｇ１）は冷却部１１０を通過することによって冷却し、それに伴って該有機溶剤を液化凝縮させる。次に該排ガス（Ｇ２）は、分離部１２０を通過することによって、液化凝縮された冷却凝縮液（Ｌ１）と有機溶剤濃度の低減された冷却処理ガス（Ｇ３）とに分離される。最後にチャンバー１２３を通じて、冷却処理ガスの一部（吸着入口ガス）（Ｇ４）が濃縮装置２００へ供給するように分配されて、冷却凝縮装置１００から排出される。 The cooling condensing device 100 includes a cooling section 110, a separation section 120, and a chamber 123. The exhaust gas (G1) containing an organic solvent is cooled by passing through the cooling section 110, and the organic solvent is liquefied and condensed accordingly. Next, the exhaust gas (G2) passes through the separation section 120 and is separated into a liquefied and condensed cooled condensate (L1) and a cooled treated gas (G3) with a reduced organic solvent concentration. Finally, through the chamber 123, a portion of the cooling process gas (adsorption inlet gas) (G4) is distributed to be supplied to the concentrator 200 and discharged from the cooling condenser 100.
冷却部１１０の冷却手段・構成は特に限定しないが、冷却水、冷水、ブラインなどの冷媒と排ガスとの間接的な熱交換によって冷却する第一熱交換器１１１などがある。冷却温度などの条件も回収対象となる有機溶剤によって適宜決めればよい。 The cooling means and structure of the cooling unit 110 are not particularly limited, but include a first heat exchanger 111 that performs cooling by indirect heat exchange between a refrigerant such as cooling water, cold water, or brine, and exhaust gas. Conditions such as cooling temperature may be determined as appropriate depending on the organic solvent to be recovered.
また、冷却部１１０は、第一熱交換器１１１の前に、冷却処理ガスの残部（リターンガス）（Ｇ５）と排ガス（Ｇ１）との熱交換によって排ガス（Ｇ１）を冷却させる第二熱交換器１１２を設けてもよい。第一熱交換器１１１に必要な伝面や冷媒量が削減されるからである。 In addition, the cooling unit 110 is provided with a second heat exchanger that cools the exhaust gas (G1) by heat exchange between the remainder of the cooling process gas (return gas) (G5) and the exhaust gas (G1) before the first heat exchanger 111. A container 112 may also be provided. This is because the transmission surface and the amount of refrigerant required for the first heat exchanger 111 are reduced.
分離部１２０の分離手段・構成は特に限定しないが、デミスター、フィルター、メッシュなどの液滴を接触して捕捉する網目状構造体１２１などがある。網目状構造体１２１に捕捉された冷却凝縮液（Ｌ１）は、重力によって綿状構造体１２１下部に配置されたタンク１２２へ集液され、回収液（Ｌ３）として回収される。 The separation means and structure of the separation section 120 are not particularly limited, but include a demister, a filter, a mesh structure 121 that contacts and captures droplets, and the like. The cooled condensate (L1) captured by the network structure 121 is collected by gravity into a tank 122 disposed below the cotton structure 121, and is recovered as a recovery liquid (L3).
チャンバー１２３は、一定容量の空間を有する構造体である。濃縮装置２００へ供給する冷却処理ガスの一部（吸着入口ガス）（Ｇ４）と、冷却処理ガスの残部（リターンガス）（Ｇ５）に分配される。 Chamber 123 is a structure having a certain volume of space. It is distributed into a part of the cooled process gas (adsorption inlet gas) (G4) to be supplied to the concentrator 200 and the remainder of the cooled process gas (return gas) (G5).
濃縮装置２００は、ガスが接触することによって、含有する有機溶剤を吸着し、加熱ガスを接触することによって、吸着した有機溶剤を脱着させる吸着材を含む吸着素子２１０を有している。また、吸着素子２１０は、脱着部（脱着ゾーン）２１１と吸着部（吸着ゾーン）２１２とを含んでいる。吸着部２１２では、冷却処理ガスの一部（吸着入口ガス）（Ｇ４）が導入されることで、吸着材に冷却処理ガスの一部（吸着入口ガス）（Ｇ４）が接触することで、冷却処理ガスの一部（吸着入口ガス）（Ｇ４）に含有される有機溶剤が吸着材に吸着され、これにより冷却処理ガスの一部（吸着入口ガス）（Ｇ４）が清浄化されて清浄ガス（Ｇ６）として排出される。 The concentrator 200 includes an adsorption element 210 that includes an adsorbent that adsorbs the contained organic solvent when it comes into contact with gas, and desorbs the adsorbed organic solvent when it comes into contact with heated gas. Further, the adsorption element 210 includes a desorption section (desorption zone) 211 and an adsorption section (adsorption zone) 212. In the adsorption section 212, a part of the cooling process gas (adsorption inlet gas) (G4) is introduced, and a part of the cooling process gas (adsorption inlet gas) (G4) comes into contact with the adsorbent. The organic solvent contained in a part of the processing gas (adsorption inlet gas) (G4) is adsorbed by the adsorbent, thereby cleaning a part of the cooling processing gas (adsorption inlet gas) (G4) and converting it into a clean gas ( G6).
脱着部２１１では、吸着材に冷却処理ガスの一部（吸着入口ガス）（Ｇ４）よりも高温のガス（Ｇ７）が導入されることで、有機溶剤が吸着材から脱着され、これにより有機溶剤を含有する脱着ガス（Ｇ８）として排出される。 In the desorption section 211, the organic solvent is desorbed from the adsorbent by introducing a gas (G7) with a higher temperature than a part of the cooling process gas (adsorption inlet gas) (G4) into the adsorbent. is discharged as a desorption gas (G8) containing
吸着素子２１０に含まれる吸着材としては、活性アルミナ、シリカゲル、活性炭素材やゼオライトが広く利用されており、中でも活性炭と疎水性ゼオライトが特に好適に利用されている。活性炭と疎水性ゼオライトは、低濃度の有機化合物を吸着、脱着する機能に優れており、古くから吸着材として各種の装置に利用されている。 As the adsorbent contained in the adsorption element 210, activated alumina, silica gel, activated carbon material, and zeolite are widely used, and activated carbon and hydrophobic zeolite are particularly preferably used. Activated carbon and hydrophobic zeolite have excellent ability to adsorb and desorb organic compounds at low concentrations, and have been used as adsorbents in various devices for a long time.
また、本発明の実施形態における濃縮装置の具体的な構成は特に限定しないが、図１に示す通り、回転軸２３０と、回転軸２３０の周りに設けられた吸着素子２１０とを備え、回転軸２３１周りに吸着素子２１０を回転させることにより、吸着部２１２において、冷却処理ガスの一部（吸着入口ガス）（Ｇ４）中の有機溶剤を吸着した吸着材が連続的に脱着部２１１に移動する構成が知られている。 Further, although the specific configuration of the concentrator in the embodiment of the present invention is not particularly limited, as shown in FIG. By rotating the adsorption element 210 around 231, the adsorbent that has adsorbed the organic solvent in a part of the cooling process gas (adsorption inlet gas) (G4) in the adsorption section 212 continuously moves to the desorption section 211. The configuration is known.
本発明の実施形態における濃縮装置２００は、図１に示す通り、脱着部２１１は吸着部２１２よりも下部に配置された方が好ましい。脱着ガス（Ｇ８）中に含まれる有機溶剤の一部が液化凝縮して脱着凝縮液（Ｌ２）が発生した場合においても、吸着部２１２に脱着凝縮液（Ｌ２）が付着しにくくなるからである。脱着凝縮液（Ｌ２）は脱着部２１１より下部へ落ち、脱着部の外装の内面などを伝って回収される。より好ましくは、図１に示す通り、脱着部２１１は下に傾斜をつけた方が良い。脱着凝縮液（Ｌ２）がより下へ落ち易くなるためである。 As shown in FIG. 1, in the concentrator 200 according to the embodiment of the present invention, the desorption section 211 is preferably disposed below the adsorption section 212. This is because even if a part of the organic solvent contained in the desorption gas (G8) is liquefied and condensed to generate a desorption condensate (L2), it becomes difficult for the desorption condensate (L2) to adhere to the adsorption section 212. . The desorption condensate (L2) falls below the desorption section 211 and is collected along the inner surface of the exterior of the desorption section. More preferably, as shown in FIG. 1, the attachment/detachment part 211 is sloped downward. This is because the desorption condensate (L2) falls more easily to the bottom.
濃縮装置２００は、脱着部２１１の脱着処理が完了した部分が吸着部２１２への移行の前に移行するパージ部（図示せず）を有していてもよい。清浄ガス（Ｇ６）の一部がパージ部に導入され、パージ部から排出されたパージ部出口ガスが、吸着部２１２に導入されるような構成であってもよい。清浄ガス（Ｇ６）により脱着完了した吸着材をパージすることで、吸着材に残る脱着ガス（Ｇ８）が清浄ガス（Ｇ６）へ混入することを防ぎ、吸着材を冷却することができるからである。 The concentrator 200 may include a purge section (not shown) to which a portion of the desorption section 211 that has completed the desorption process is transferred to the adsorption section 212 before being transferred to the adsorption section 212 . A configuration may be adopted in which a part of the clean gas (G6) is introduced into the purge section, and the purge section outlet gas discharged from the purge section is introduced into the adsorption section 212. This is because by purging the adsorbent that has completed desorption with the clean gas (G6), it is possible to prevent the desorption gas (G8) remaining in the adsorbent from mixing with the clean gas (G6) and to cool the adsorbent. .
濃縮装置２００は、脱着に使用する高温のガス（Ｇ７）は、清浄ガス（Ｇ６）の一部を再生ヒータ２５０などの加熱手段を用いて高温状態にしたものが好ましい。吸着部２１２で有機溶剤含有ガスの処理風量が増えないからである。排ガス（Ｇ１）の温度が５０～２００℃の温度の場合においては、排ガス（Ｇ１）の一部を再生ヒータ２５０などで昇温させて使用した方がより好ましい。高温の排ガス（Ｇ１）を脱着に用いることで、再生ヒータ２５０の使用ユーティリティを削減でき、排ガス（Ｇ１）の温度によっては脱着に再生ヒータ２５０が不要になるからである。また、冷却凝縮装置１００へ排ガス（Ｇ１）および脱着ガス（Ｇ８）を通過させる割合は、排ガス（Ｇ１）が０％～５０％であり、脱着ガス（Ｇ５）が５０％～１００％が想定される。 In the concentrator 200, the high temperature gas (G7) used for desorption is preferably a part of the clean gas (G6) heated to a high temperature using heating means such as the regeneration heater 250. This is because the processing air volume of the organic solvent-containing gas in the adsorption section 212 does not increase. When the temperature of the exhaust gas (G1) is between 50 and 200° C., it is more preferable to raise the temperature of a part of the exhaust gas (G1) using the regeneration heater 250 or the like. This is because by using the high temperature exhaust gas (G1) for desorption, the utility of the regeneration heater 250 can be reduced, and depending on the temperature of the exhaust gas (G1), the regeneration heater 250 becomes unnecessary for desorption. Furthermore, it is assumed that the proportion of the exhaust gas (G1) and desorption gas (G8) passing through the cooling condensing device 100 is 0% to 50% for the exhaust gas (G1) and 50% to 100% for the desorption gas (G5). Ru.
第一通流経路３００は、冷却処理ガスの一部（吸着入口ガス）（Ｇ４）をチャンバー１２３から濃縮装置２００へ導入する部位である。第一通流経路３００のチャンバー１２３への接続口は、チャンバー１２３の天井部が好ましい。分離部１２０で捕捉しきれなかった僅かな液滴の濃縮装置２００への侵入を抑制し、後述する濃縮装置２００の吸着素子２１０の濡れによる性能低下・強度低下などを防ぐためである。さらに好ましくは、冷却処理ガス（Ｇ３）の通気方向対して、対向するように冷却処理ガスの一部（吸着入口ガス）（Ｇ４）を取り出すようにした方が良い。より液滴の侵入を防ぐことができる。このほか、冷却処理ガスの一部（吸着入口ガス）（Ｇ４）の取り出し口に、上記綿状構造体１２１と類似の液滴侵入防止部材を設けても良いし、液滴を気化させるための加熱器を設けても良い。 The first flow path 300 is a part that introduces a part of the cooling process gas (adsorption inlet gas) (G4) from the chamber 123 to the concentrator 200. The connection port of the first flow path 300 to the chamber 123 is preferably the ceiling of the chamber 123. This is to suppress the intrusion of small droplets that could not be captured by the separation unit 120 into the concentrator 200, and to prevent performance deterioration and strength deterioration due to wetting of the adsorption element 210 of the concentrator 200, which will be described later. More preferably, a part of the cooling processing gas (adsorption inlet gas) (G4) is taken out so as to be opposite to the ventilation direction of the cooling processing gas (G3). Intrusion of droplets can be further prevented. In addition, a droplet intrusion prevention member similar to the above-mentioned cotton-like structure 121 may be provided at the outlet of a part of the cooling process gas (adsorption inlet gas) (G4), A heater may also be provided.
第二通流経路４００は、脱着ガス（Ｇ８）を冷却凝縮装置１００の排ガス（Ｇ１）導入部に返送する部位である。第二通流経路４００は、脱着部２１１は、冷却凝縮装置１００へ供給される排ガス（Ｇ１）の導入部よりもより上部に配置されるように接続されることが好ましい。前記濃縮装置２００の脱着ガス（Ｇ８）から発生した前記脱着凝縮液（Ｌ２）が、冷却凝縮装置１００へ移行しやすいからである。さらに好ましくは、冷却凝縮装置１００の排ガス（Ｇ１）導入部およびタンク１２２の二か所に通気されるように構成された方が良い。脱着ガス（Ｇ８）から発生した前記脱着凝縮液（Ｌ２）が直接タンク１２２へ回収されやすくなるからである。 The second flow path 400 is a part that returns the desorption gas (G8) to the exhaust gas (G1) introduction part of the cooling condensing device 100. It is preferable that the second flow path 400 is connected such that the desorption section 211 is disposed higher than the introduction section of the exhaust gas (G1) supplied to the cooling condensing device 100. This is because the desorption condensate (L2) generated from the desorption gas (G8) of the concentrator 200 easily moves to the cooling condensation device 100. More preferably, it is configured so that the exhaust gas (G1) inlet of the cooling condensing device 100 and the tank 122 are ventilated. This is because the desorption condensate (L2) generated from the desorption gas (G8) is easily collected directly into the tank 122.
本発明の実施形態における有機溶剤回収システム１の濃縮装置２００の脱着に使用する高温のガス（Ｇ７）は、前述の通り清浄ガス（Ｇ６）の一部を再生ヒータ２５０などの加熱手段を用いて高温状態にしたものが好ましいが、排ガス（Ｇ１）の温度が５０～２００℃の温度の場合においては、排ガス（Ｇ１）の一部を再生ヒータ２３などで昇温させて使用した方がより好ましい。高温の排ガスを脱着に用いることで、再生ヒータ２３の使用ユーティリティを削減でき、排ガス（Ｇ１）の温度によっては脱着に再生ヒータ２３が不要になるからである。また、冷却回収装置１０へ排ガス（Ｇ１）および脱着ガス（Ｇ５）を通過させる割合は、排ガス（Ｇ１）が０％～５０％であり、脱着ガス（Ｇ５）が５０％～１００％が想定される。 The high temperature gas (G7) used for desorption in the concentrator 200 of the organic solvent recovery system 1 in the embodiment of the present invention is obtained by converting a part of the clean gas (G6) using a heating means such as the regeneration heater 250 as described above. It is preferable to heat the exhaust gas (G1) to a high temperature, but if the temperature of the exhaust gas (G1) is between 50 and 200°C, it is more preferable to raise the temperature of a part of the exhaust gas (G1) using the regeneration heater 23 or the like. . This is because by using high-temperature exhaust gas for desorption, the utility of the regeneration heater 23 can be reduced, and depending on the temperature of the exhaust gas (G1), the regeneration heater 23 becomes unnecessary for desorption. Furthermore, it is assumed that the proportion of the exhaust gas (G1) and desorption gas (G5) passing through the cooling recovery device 10 is 0% to 50% for the exhaust gas (G1) and 50% to 100% for the desorption gas (G5). Ru.
排ガス（Ｇ１）は、生産設備から排出されるガスである場合、冷却処理ガスの残部（リターンガス）（Ｇ５）は、生産設備に戻される構成としてもよい。 When the exhaust gas (G1) is a gas discharged from the production equipment, the remainder of the cooling process gas (return gas) (G5) may be returned to the production equipment.
冷却処理ガスの残部（リターンガス）（Ｇ５）に含まれる有機溶剤濃度を更に低減したい場合、図２に示すように、冷却処理ガスの残部（リターンガス）（Ｇ５）を処理する濃縮装置５００を追加導入してもよい。また、清浄ガス（Ｇ６）に含まれる有機溶剤濃度を更に低減したい場合、図３に示すように、清浄空気（Ｇ６）を処理する濃縮装置６００を追加導入してもよい。濃縮装置５００や濃縮装置６００は、濃縮装置２００と同じ構成でも別の構成であってもよい。また、追加導入する濃縮装置数に制限はない。何れの濃縮装置から排出される脱着ガスは、第二通流経路４００を経由して、冷却凝縮装置１００の排ガス（Ｇ１）導入部に返送される。 If it is desired to further reduce the concentration of organic solvent contained in the remainder of the cooling process gas (return gas) (G5), as shown in FIG. It may be additionally introduced. Moreover, if it is desired to further reduce the organic solvent concentration contained in the clean gas (G6), as shown in FIG. 3, a concentrating device 600 for processing the clean air (G6) may be additionally introduced. The concentrator 500 and the concentrator 600 may have the same configuration as the concentrator 200 or a different configuration. Furthermore, there is no limit to the number of additional concentrators to be introduced. The desorption gas discharged from either of the concentrators is returned to the exhaust gas (G1) introduction section of the cooling condensing device 100 via the second flow path 400.
本発明の実施形態では、排ガス（Ｇ１）に含有される有機溶剤としては、１℃～５０℃の冷却にて液化して回収できる有機溶剤が挙げられる。有機溶剤としては、たとえば、Ｎ－メチル－２－ピロリドン、Ｎ－エチル－２－ピロリドン、Ｎ，Ｎ－ジメチルホルムアミド、Ｎ，Ｎ－ジメチルアセトアミド、またｎ－デカンである。これらは例示であり、これらに限定されることはない。含有される有機溶剤は、１種でも複数種でもよい。 In the embodiment of the present invention, the organic solvent contained in the exhaust gas (G1) includes an organic solvent that can be liquefied and recovered by cooling at 1° C. to 50° C. Examples of organic solvents include N -methyl-2-pyrrolidone, N -ethyl-2-pyrrolidone, N,N-dimethylformamide, N,N-dimethylacetamide, and n-decane. These are examples and are not limited to these. The number of organic solvents contained may be one or more.
上記開示した実施の形態はすべての点で例示であって、制限的なものではない。本発明の技術的範囲は特許請求の範囲によって画定され、また特許請求の範囲の記載と均等の意味および範囲内でのすべての変更を含むものである。 The embodiments disclosed above are illustrative in all respects and are not restrictive. The technical scope of the present invention is defined by the claims, and includes all changes within the meaning and scope equivalent to the claims.
本発明は、各種工場や研究施設等の生産設備から排出される有機溶剤を含有する排ガスを処理する装置に利用可能である。 INDUSTRIAL APPLICATION This invention can be utilized for the apparatus which processes the exhaust gas containing the organic solvent discharged|emitted from production equipment, such as various factories and a research facility.
１ 有機溶剤回収システム、５０ 排ガス導入経路、６０ 返還経路、１００ 冷却凝縮置、１１０ 冷却部、１１１ 第一熱交換器、１１２ 第二熱交換器、１２０ 分離部、１２１ 網目状構造体、１２２ タンク、１２３ チャンバー、２００ 濃縮装置、２１０ 吸着素子、２１１ 脱着部、２１２ 吸着部、２３０ 回転軸、２５０ 再生ヒータ、３００ 第一第二通流経路、４００ 第二通流経路、５００ 濃縮装置、６００ 濃縮装置、Ｇ１ 排ガス、Ｇ２ 冷却後の排ガス、Ｇ３ 冷却処理ガス、Ｇ４ 冷却処理ガスの一部、Ｇ５ 冷却処理ガスの残部、Ｇ６ 清浄ガス、Ｇ７ 高温のガス、Ｇ８ 脱着ガス、Ｌ１ 冷却凝縮液、Ｌ２ 脱着凝縮液、Ｌ３ 回収液。 1 organic solvent recovery system, 50 exhaust gas introduction route, 60 return route, 100 cooling condensation unit, 110 cooling unit, 111 first heat exchanger, 112 second heat exchanger, 120 separation unit, 121 mesh structure, 122 tank , 123 chamber, 200 concentrator, 210 adsorption element, 211 desorption section, 212 adsorption section, 230 rotating shaft, 250 regeneration heater, 300 first and second flow path, 400 second flow path, 500 concentrator, 600 concentration equipment, G1 exhaust gas, G2 exhaust gas after cooling, G3 cooling processing gas, G4 part of cooling processing gas, G5 remainder of cooling processing gas, G6 clean gas, G7 high temperature gas, G8 desorption gas, L1 cooling condensate, L2 Desorption condensate, L3 recovery liquid.
Claims (6)
前記有機溶剤を含有する前記排ガスを冷却することで、前記有機溶剤を液化凝縮し、前記有機溶剤の濃度が低減された冷却処理ガスとして排出する冷却凝縮装置と、
前記冷却処理ガスを通流させる第一通流経路と、
前記第一通流経路から導入された前記冷却処理ガスに含まれる前記有機溶剤を第一吸着素子にて吸着して前記有機溶剤の濃度が更に低減された第一処理ガスとして排出し、高温ガスを導入して前記第一吸着素子から前記有機溶剤を脱着して第一脱着ガスとして排出する第一濃縮装置と、
前記第一処理ガスの一部を通流させる第二通流経路と、
前記第二通流経路から導入された前記第一処理ガスに含まれる前記有機溶剤を第二吸着素子にて吸着して前記有機溶剤の濃度が更に低減された第二処理ガスとして排出し、高温ガスを導入して前記第二吸着素子から前記有機溶剤を脱着して第二脱着ガスとして排出する第二濃縮装置と、
前記第一脱着ガスおよび前記第二脱着ガスを前記冷却凝縮装置に戻す第三通流経路と、を備えた、有機溶剤回収システム。 An organic solvent recovery system that recovers organic solvents from exhaust gas containing organic solvents discharged from production equipment,
A cooling condensation device that liquefies and condenses the organic solvent by cooling the exhaust gas containing the organic solvent, and discharges the organic solvent as a cooled treated gas with a reduced concentration;
a first flow path through which the cooling processing gas flows;
The organic solvent contained in the cooled processing gas introduced from the first flow path is adsorbed by a first adsorption element and discharged as a first processing gas in which the concentration of the organic solvent is further reduced. a first concentration device that introduces a gas to desorb the organic solvent from the first adsorption element and discharge it as a first desorption gas;
a second flow path through which a portion of the first processing gas flows;
The organic solvent contained in the first processing gas introduced from the second flow path is adsorbed by a second adsorption element, and is discharged as a second processing gas in which the concentration of the organic solvent is further reduced. a second concentration device that introduces a gas to desorb the organic solvent from the second adsorption element and discharge it as a second desorption gas;
An organic solvent recovery system comprising: a third flow path for returning the first desorption gas and the second desorption gas to the cooling condensing device.
前記第一通流経路は、前記チャンバーの天井部から前記冷却処理ガスを前記第一濃縮装置に導入するように設置されている、請求項１に記載の有機溶剤回収システム。 The cooling condensing device includes a network structure that separates the condensed organic solvent and the cooling process gas by bringing the cooled exhaust gas into contact with each other, and a network structure that separates the cooling process gas after passing through the network structure. It further comprises a chamber for storing the water for a certain period of time,
The organic solvent recovery system according to claim 1, wherein the first flow path is installed so as to introduce the cooled processing gas into the first concentrator from the ceiling of the chamber.
前記第二熱交換器は、前記冷却凝縮装置に導入される前記排ガスを、前記第一処理ガスの残部との熱交換により冷却する、請求項４に記載の有機溶剤回収システム。 The heat exchanger includes a first heat exchanger and a second heat exchanger provided upstream of the first heat exchanger,
The organic solvent recovery system according to claim 4 , wherein the second heat exchanger cools the exhaust gas introduced into the cooling condensing device by heat exchange with the remainder of the first treated gas.
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| KR1020227025050A KR20220116284A (en) | 2019-12-26 | 2020-12-18 | Organic Solvent Recovery System |
| EP20904424.7A EP4082649A4 (en) | 2019-12-26 | 2020-12-18 | Organic solvent recovery system |
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