TW202130404A - Organic solvent recovery system - Google Patents
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本發明係關於一種有機溶劑回收系統。The invention relates to an organic solvent recovery system.
過去,作為從含有有機溶劑之排放氣體回收有機溶劑的處理系統,已知一種組合有冷卻冷凝裝置及使用吸附元件之濃縮裝置的系統。冷卻冷凝裝置,將有機溶劑冷凝回收,降低排放氣體中的有機溶劑濃度。使用吸附元件之濃縮裝置,使從冷卻冷凝裝置排出的有機溶劑濃度已降低之排放氣體接觸吸附元件,吸附有機溶劑,進一步降低排放氣體中的有機溶劑濃度,且對吸附有有機溶劑之吸附材噴吹高溫氣體而使有機溶劑脫附,作為含有高濃度有機溶劑之脫附氣體排出。將脫附氣體送回至冷卻冷凝裝置,予以再處理(參考專利文獻1、2)。 [習知技術文獻] [專利文獻]In the past, as a processing system for recovering organic solvent from exhaust gas containing organic solvent, a system combining a cooling and condensing device and a concentration device using an adsorption element is known. Cool the condensing device to condense and recover the organic solvent to reduce the concentration of the organic solvent in the exhaust gas. Use the concentration device of the adsorption element to make the exhaust gas whose concentration of the organic solvent discharged from the cooling and condensing device contact the adsorption element, adsorb the organic solvent, further reduce the concentration of the organic solvent in the exhaust gas, and spray the adsorbent with the organic solvent Blow high-temperature gas to desorb the organic solvent, and discharge it as a desorption gas containing a high concentration of organic solvent. The desorbed gas is sent back to the cooling and condensing device for reprocessing (refer to Patent Documents 1 and 2). [Literature Technical Literature] [Patent Literature]
專利文獻1:日本特開第2016-101553號公報 專利文獻2:日本特開第2017-991號公報Patent Document 1: Japanese Patent Laid-Open No. 2016-101553 Patent Document 2: Japanese Patent Laid-Open No. 2017-991
[本發明所欲解決的問題][Problems to be solved by the present invention]
於生產設備中,補給一定量之乾淨氣體。因而,將補給氣體分之排放氣體往外部環境排出。近年,伴隨世界性之排放氣體管制,要求將有機溶劑去除至極低濃度,要求高度的處理效率。In the production equipment, a certain amount of clean gas is supplied. Therefore, the exhaust gas, which is the supply gas, is discharged to the external environment. In recent years, with the worldwide emission gas control, it is required to remove organic solvents to extremely low concentrations, and high processing efficiency is required.
本發明之目的在於提供一種有機溶劑回收系統,可從排放氣體將有機溶劑更高效率地回收。 [解決問題之技術手段]The purpose of the present invention is to provide an organic solvent recovery system that can recover organic solvents from exhaust gas more efficiently. [Technical means to solve the problem]
依本發明揭露的有機溶劑回收系統之一態樣,則為一種有機溶劑回收系統,具備:冷卻冷凝裝置,藉由將含有有機溶劑之排放氣體冷卻,而將該有機溶劑液化冷凝,作為該有機溶劑的濃度已降低之冷卻處理氣體排出;第一流通路徑,使該冷卻處理氣體的一部分流通;濃縮裝置,具備吸附元件,將從該第一流通路徑導入之該冷卻處理氣體所含有的該有機溶劑藉由該吸附元件吸附,作為該有機溶劑的濃度進一步降低之潔淨氣體排出,導入高溫氣體而從該吸附元件使該有機溶劑脫附,作為脫附氣體排出;以及第二流通路徑,將該脫附氣體導入至該冷卻冷凝裝置;於該有機溶劑回收系統中,該冷卻冷凝裝置,具備:網眼狀構造體,藉由接觸冷卻後之該排放氣體,而使冷凝的該有機溶劑與該冷卻處理氣體分離;以及腔室,將通過該網眼狀構造體後之該冷卻處理氣體貯存一定時間;該第一流通路徑,設置為從該腔室之頂棚部將該冷卻處理氣體的一部分導入至該濃縮裝置。According to one aspect of the organic solvent recovery system disclosed in the present invention, it is an organic solvent recovery system including: a cooling and condensing device, which cools the exhaust gas containing the organic solvent to liquefy and condense the organic solvent as the organic solvent. The cooling process gas whose solvent concentration has been reduced is discharged; the first circulation path allows a part of the cooling process gas to circulate; the concentration device is equipped with an adsorption element, and the organic contained in the cooling process gas introduced from the first circulation path The solvent is adsorbed by the adsorption element and discharged as a clean gas whose concentration of the organic solvent is further reduced. A high-temperature gas is introduced to desorb the organic solvent from the adsorption element and is discharged as a desorption gas; and the second flow path is The desorption gas is introduced into the cooling and condensing device; in the organic solvent recovery system, the cooling and condensing device is provided with: a mesh-like structure that contacts the cooled exhaust gas to condense the organic solvent and the Separation of the cooling processing gas; and a chamber for storing the cooling processing gas after passing through the mesh structure for a certain period of time; the first circulation path is set to introduce a part of the cooling processing gas from the ceiling portion of the chamber To the concentration device.
於該有機溶劑回收系統中,該腔室具備分隔部,該分隔部可與從該網眼狀構造體排出之該冷卻處理氣體的排氣方向對向而進行該第一流通路徑的吸入。In the organic solvent recovery system, the chamber is provided with a partition that can be opposed to the exhaust direction of the cooling process gas discharged from the mesh structure to perform the suction of the first flow path.
於該有機溶劑回收系統中,該冷卻冷凝裝置,具備藉由與冷媒之熱交換而施行該冷卻的熱交換器。In the organic solvent recovery system, the cooling and condensing device includes a heat exchanger that performs the cooling by heat exchange with a refrigerant.
於該有機溶劑回收系統中,該第二流通路徑,將脫附部設置於較該脫附氣體與該排放氣體的合流位置更為上部。In the organic solvent recovery system, the second circulation path has the desorption part located above the confluence position of the desorption gas and the exhaust gas.
於該有機溶劑回收系統中,該排放氣體為從生產設備排出之氣體;具備返回路徑,其使從該第一流通路徑排出之該冷卻處理氣體的一部分以外亦即該冷卻處理氣體的其餘部分,返回至該生產設備。In the organic solvent recovery system, the exhaust gas is the gas discharged from the production equipment; a return path is provided, which allows a part of the cooling process gas discharged from the first circulation path, that is, the remaining part of the cooling process gas, Return to the production facility.
於該有機溶劑回收系統中,該熱交換器,包含第一熱交換器、及設置於該第一熱交換器之前段的第二熱交換器;該第二熱交換器,將導入至該冷卻冷凝裝置之該排放氣體,藉由與該冷卻處理氣體的其餘部分之熱交換而冷卻。In the organic solvent recovery system, the heat exchanger includes a first heat exchanger and a second heat exchanger arranged in the front stage of the first heat exchanger; the second heat exchanger will be introduced to the cooling The exhaust gas of the condensing device is cooled by heat exchange with the rest of the cooling process gas.
依本發明揭露的有機溶劑回收系統之一態樣,則為一種有機溶劑回收系統,由從生產設備排出的含有有機溶劑之排放氣體,將該有機溶劑回收,包含:冷卻冷凝裝置,藉由將含有該有機溶劑之該排放氣體冷卻,而將該有機溶劑液化冷凝,作為該有機溶劑的濃度已降低之冷卻處理氣體排出;第一流通路徑,使該冷卻處理氣體流通;第一濃縮裝置,將從該第一流通路徑導入之該冷卻處理氣體所含有的該有機溶劑藉由第一吸附元件吸附,作為該有機溶劑的濃度進一步降低之第一處理氣體排出,導入高溫氣體而從該第一吸附元件使該有機溶劑脫附,作為第一脫附氣體排出;第二流通路徑,使該第一處理氣體的一部分流通;第二濃縮裝置,將從該第二流通路徑導入之該第一處理氣體所含有的該有機溶劑藉由第二吸附元件吸附,作為該有機溶劑的濃度進一步降低之第二處理氣體排出,導入高溫氣體而從該第二吸附元件使該有機溶劑脫附,作為第二脫附氣體排出;以及第三流通路徑,使該第一脫附氣體及該第二脫附氣體,返回至該冷卻冷凝裝置。According to one aspect of the organic solvent recovery system disclosed in the present invention, it is an organic solvent recovery system. The organic solvent is recovered from the exhaust gas containing the organic solvent discharged from the production equipment, including: a cooling and condensing device, The exhaust gas containing the organic solvent is cooled, and the organic solvent is liquefied and condensed to be discharged as a cooling processing gas whose concentration of the organic solvent has been reduced; the first circulation path allows the cooling processing gas to circulate; the first concentrating device The organic solvent contained in the cooled processing gas introduced from the first flow path is adsorbed by the first adsorption element, and discharged as a first processing gas whose concentration of the organic solvent is further reduced, and a high-temperature gas is introduced to adsorb from the first adsorption element. The element desorbs the organic solvent and discharges it as the first desorption gas; the second circulation path allows a part of the first processing gas to circulate; the second concentrating device, the first processing gas introduced from the second circulation path The organic solvent contained is adsorbed by the second adsorption element and discharged as a second processing gas whose concentration of the organic solvent is further reduced. A high-temperature gas is introduced to desorb the organic solvent from the second adsorption element as a second desorption. The attached gas is discharged; and a third circulation path is used to return the first desorbed gas and the second desorbed gas to the cooling and condensing device.
於該有機溶劑回收系統中,該冷卻冷凝裝置,更包含:網眼狀構造體,藉由接觸該冷卻後之該排放氣體,而使冷凝的該有機溶劑與該冷卻處理氣體分離;以及腔室,將通過該網眼狀構造體後之該冷卻處理氣體貯存一定時間;該第一流通路徑,設置為從該腔室之頂棚部將該冷卻處理氣體導入至該第一濃縮裝置。In the organic solvent recovery system, the cooling and condensing device further includes: a mesh-like structure for separating the condensed organic solvent from the cooling process gas by contacting the cooled exhaust gas; and a chamber , Storing the cooling processing gas after passing through the mesh structure for a certain period of time; the first circulation path is arranged to introduce the cooling processing gas from the ceiling portion of the chamber to the first concentrating device.
於該有機溶劑回收系統中,該腔室具備分隔部,該分隔部可與從該網眼狀構造體排出之該冷卻處理氣體的排氣方向對向而進行該第一流通路徑的吸入。In the organic solvent recovery system, the chamber is provided with a partition that can be opposed to the exhaust direction of the cooling process gas discharged from the mesh structure to perform the suction of the first flow path.
於該有機溶劑回收系統中,該冷卻冷凝裝置,更包含藉由與冷媒之熱交換而施行該冷卻的熱交換器。In the organic solvent recovery system, the cooling and condensing device further includes a heat exchanger that performs the cooling by heat exchange with a refrigerant.
於該有機溶劑回收系統中,更包含返回路徑,其使從該第二流通路徑排出之該第一處理氣體的一部分以外亦即該第一處理氣體的其餘部分,返回至該生產設備。The organic solvent recovery system further includes a return path for returning part of the first processing gas discharged from the second circulation path, that is, the remaining part of the first processing gas, to the production equipment.
於該有機溶劑回收系統中,該熱交換器,包含第一熱交換器、及設置於該第一熱交換器之前段的第二熱交換器;該第二熱交換器,將導入至該冷卻冷凝裝置之該排放氣體,藉由與該第一處理氣體的其餘部分之熱交換而冷卻。In the organic solvent recovery system, the heat exchanger includes a first heat exchanger and a second heat exchanger arranged in the front stage of the first heat exchanger; the second heat exchanger will be introduced to the cooling The exhaust gas of the condensing device is cooled by heat exchange with the rest of the first processing gas.
依本發明揭露的有機溶劑回收系統之一態樣,則為一種有機溶劑回收系統,由從生產設備排出的含有有機溶劑之排放氣體,將該有機溶劑回收,包含:冷卻冷凝裝置,藉由將含有該有機溶劑之該排放氣體冷卻,而將該有機溶劑液化冷凝,作為該排放氣體之該有機溶劑的濃度已降低之冷卻處理氣體排出;冷卻氣體流通路徑,使該冷卻處理氣體流通;濃縮裝置,將從該冷卻氣體流通路徑導入之該冷卻處理氣體所含有的該有機溶劑藉由吸附元件吸附,作為該有機溶劑的濃度進一步降低之處理氣體排出,導入高溫氣體而從該吸附元件使該有機溶劑脫附,作為脫附氣體排出;以及脫附氣體流通路徑,將該脫附氣體導入至該冷卻冷凝裝置。According to one aspect of the organic solvent recovery system disclosed in the present invention, it is an organic solvent recovery system. The organic solvent is recovered from the exhaust gas containing the organic solvent discharged from the production equipment, including: a cooling and condensing device, The exhaust gas containing the organic solvent is cooled, and the organic solvent is liquefied and condensed, and the cooling process gas whose concentration of the organic solvent has been reduced as the exhaust gas is discharged; the cooling gas circulation path allows the cooling process gas to circulate; concentrating device , The organic solvent contained in the cooling processing gas introduced from the cooling gas flow path is adsorbed by the adsorption element, and discharged as processing gas whose concentration of the organic solvent is further reduced, and high temperature gas is introduced to make the organic solvent from the adsorption element The solvent is desorbed and discharged as a desorbed gas; and a desorbed gas flow path is used to introduce the desorbed gas to the cooling and condensing device.
該冷卻冷凝裝置,包含:冷卻部,使該排放氣體流通;以及分離部,在沿著該排放氣體的流動方向觀察之情況,位於該冷卻部的下游側;該分離部,具備:承接部,承接以該冷卻部冷卻的含有該有機溶劑之冷卻冷凝液;網眼狀構造體,藉由接觸冷卻後之該排放氣體,而使該冷卻冷凝液與該冷卻處理氣體分離;以及腔室,將通過該網眼狀構造體後之該冷卻處理氣體貯存一定時間;沿著該排放氣體的流動方向觀察之情況,相對於從該冷卻部往該分離部流動的方向,使該分離部內從該網眼狀構造體往該腔室流動的方向交叉,藉以使該排放氣體沿L字形方向流動。The cooling and condensing device includes: a cooling part that allows the exhaust gas to circulate; and a separation part located on the downstream side of the cooling part when viewed along the flow direction of the exhaust gas; the separation part includes: a receiving part, Receiving the cooling condensate containing the organic solvent cooled by the cooling part; a mesh-like structure that separates the cooling condensate from the cooling processing gas by contacting the exhaust gas after cooling; and a chamber, After passing through the mesh-like structure, the cooling processing gas is stored for a certain period of time; when viewed along the flow direction of the exhaust gas, relative to the direction from the cooling part to the separation part, the separation part flows from the net The eye-shaped structure crosses the flow direction of the chamber, so that the exhaust gas flows in the L-shaped direction.
於該有機溶劑回收系統中,於該網眼狀構造體的下游側,配置用於將該冷卻處理氣體加熱之加熱器。In the organic solvent recovery system, a heater for heating the cooling process gas is arranged on the downstream side of the mesh structure.
於該有機溶劑回收系統中,於該腔室內,設置防止該冷卻冷凝液往該冷卻氣體流通路徑流動的堰部。In the organic solvent recovery system, a weir is provided in the chamber to prevent the cooling condensate from flowing to the cooling gas flow path.
於該有機溶劑回收系統中,該濃縮裝置,包含第一濃縮裝置、及位於該第一濃縮裝置的下游側之第二濃縮裝置;該第一濃縮裝置,將從該冷卻氣體流通路徑導入之該冷卻處理氣體所含有的該有機溶劑藉由第一吸附元件吸附,作為該有機溶劑的濃度進一步降低之第一處理氣體排出,導入高溫氣體而從該第一吸附元件使該有機溶劑脫附,作為第一脫附氣體排出;該有機溶劑回收系統,更包含使該第一處理氣體的一部分流通之第一處理氣體流通路徑;該第二濃縮裝置,將從該第一處理氣體流通路徑導入之該第一處理氣體所含有的該有機溶劑藉由第二吸附元件吸附,作為該有機溶劑的濃度進一步降低之第二處理氣體排出,導入高溫氣體而從該第二吸附元件使該有機溶劑脫附,作為第二脫附氣體排出。In the organic solvent recovery system, the concentration device includes a first concentration device and a second concentration device located on the downstream side of the first concentration device; the first concentration device introduces the cooling gas flow path into the The organic solvent contained in the cooling process gas is adsorbed by the first adsorption element, and discharged as the first process gas whose concentration of the organic solvent is further reduced, and high-temperature gas is introduced to desorb the organic solvent from the first adsorption element. The first desorption gas is discharged; the organic solvent recovery system further includes a first processing gas flow path through which a part of the first processing gas circulates; the second concentrating device introduces the first processing gas through the flow path The organic solvent contained in the first processing gas is adsorbed by the second adsorption element, and discharged as a second processing gas whose concentration of the organic solvent is further reduced, and a high-temperature gas is introduced to desorb the organic solvent from the second adsorption element, It is discharged as the second desorption gas.
於該有機溶劑回收系統中,該第一濃縮裝置,將該第一吸附元件於繞筒軸旋轉之中空圓柱狀的轉筒之繞筒軸的圓周方向配置複數個。In the organic solvent recovery system, the first concentrating device arranges a plurality of the first adsorption elements in the circumferential direction around the cylindrical axis of the hollow cylindrical rotating drum rotating around the cylindrical axis.
於該有機溶劑回收系統中,該第二濃縮裝置,將該第二吸附元件配置於繞筒軸旋轉之圓盤狀的吸附轉筒。In the organic solvent recovery system, the second concentrating device arranges the second adsorption element on a disc-shaped adsorption drum rotating around a drum axis.
依本發明揭露的有機溶劑回收系統之一態樣,則為一種有機溶劑回收系統,由從生產設備排出的含有有機溶劑之排放氣體,將該有機溶劑回收,具備:冷卻冷凝裝置,藉由將含有該有機溶劑之該排放氣體冷卻,而將該有機溶劑液化冷凝,作為該有機溶劑的濃度已降低之冷卻處理氣體排出;冷卻氣體流通路徑,使該冷卻處理氣體流通;第一濃縮裝置,將從該冷卻氣體流通路徑導入之該冷卻處理氣體所含有的該有機溶劑藉由第一吸附元件吸附,作為該有機溶劑的濃度進一步降低之第一處理氣體排出,導入高溫氣體而從該第一吸附元件使該有機溶劑脫附,作為第一脫附氣體排出;第一處理氣體流通路徑,使該第一處理氣體的一部分流通;以及第二濃縮裝置,將從該第一處理氣體流通路徑導入之該第一處理氣體所含有的該有機溶劑藉由第二吸附元件吸附,作為該有機溶劑的濃度進一步降低之第二處理氣體排出,導入高溫氣體而從該第二吸附元件使該有機溶劑脫附,作為第二脫附氣體排出;使該第一脫附氣體,返回至該冷卻冷凝裝置,且使該第二脫附氣體,返回至該冷卻氣體流通路徑。According to one aspect of the organic solvent recovery system disclosed in the present invention, it is an organic solvent recovery system. The organic solvent is recovered from the exhaust gas containing organic solvent discharged from the production equipment. The organic solvent is equipped with a cooling and condensing device. The exhaust gas containing the organic solvent is cooled, and the organic solvent is liquefied and condensed, and discharged as a cooling processing gas whose concentration of the organic solvent has been reduced; a cooling gas circulation path allows the cooling processing gas to circulate; a first concentrating device The organic solvent contained in the cooling process gas introduced from the cooling gas flow path is adsorbed by the first adsorption element, and discharged as the first process gas whose concentration of the organic solvent is further reduced, and high temperature gas is introduced to adsorb from the first adsorption element. The element desorbs the organic solvent and discharges it as the first desorption gas; the first processing gas flow path allows a part of the first processing gas to circulate; and the second concentrating device introduces the first processing gas through the flow path The organic solvent contained in the first processing gas is adsorbed by the second adsorption element, and discharged as a second processing gas whose concentration of the organic solvent is further reduced, and a high-temperature gas is introduced to desorb the organic solvent from the second adsorption element , It is discharged as the second desorption gas; the first desorption gas is returned to the cooling and condensing device, and the second desorption gas is returned to the cooling gas flow path.
依本發明揭露的有機溶劑回收系統之一態樣,則為一種有機溶劑回收系統,由從生產設備排出的含有有機溶劑之排放氣體,將該有機溶劑回收,具備:冷卻冷凝裝置,藉由將含有該有機溶劑之該排放氣體冷卻,而將該有機溶劑液化冷凝,作為該有機溶劑的濃度已降低之冷卻處理氣體排出;冷卻氣體流通路徑,使該冷卻處理氣體流通;第一濃縮裝置,將從該冷卻氣體流通路徑導入之該冷卻處理氣體所含有的該有機溶劑藉由第一吸附元件吸附,作為該有機溶劑的濃度進一步降低之第一處理氣體排出,藉由第一加熱器導入高溫氣體而從該第一吸附元件使該有機溶劑脫附,作為第一脫附氣體排出;第一處理氣體流通路徑,使該第一處理氣體的一部分流通;以及第二濃縮裝置,將從該第一處理氣體流通路徑導入之該第一處理氣體所含有的該有機溶劑藉由第二吸附元件吸附,作為該有機溶劑的濃度進一步降低之第二處理氣體排出,藉由第二加熱器導入高溫氣體而從該第二吸附元件使該有機溶劑脫附,作為第二脫附氣體排出;使該第一脫附氣體,返回至該冷卻冷凝裝置,且使該第二脫附氣體,返回至該第一加熱器。According to one aspect of the organic solvent recovery system disclosed in the present invention, it is an organic solvent recovery system. The organic solvent is recovered from the exhaust gas containing organic solvent discharged from the production equipment. The organic solvent is equipped with a cooling and condensing device. The exhaust gas containing the organic solvent is cooled, and the organic solvent is liquefied and condensed, and discharged as a cooling processing gas whose concentration of the organic solvent has been reduced; a cooling gas circulation path allows the cooling processing gas to circulate; a first concentrating device The organic solvent contained in the cooling processing gas introduced from the cooling gas flow path is adsorbed by the first adsorption element, and discharged as the first processing gas whose concentration of the organic solvent is further reduced, and high temperature gas is introduced by the first heater The organic solvent is desorbed from the first adsorption element and discharged as the first desorption gas; the first processing gas flow path allows a part of the first processing gas to circulate; and the second concentrating device removes the first processing gas from the The organic solvent contained in the first processing gas introduced into the processing gas flow path is adsorbed by the second adsorption element and discharged as the second processing gas whose concentration of the organic solvent is further reduced, and the high temperature gas is introduced by the second heater. The organic solvent is desorbed from the second adsorption element and discharged as the second desorption gas; the first desorption gas is returned to the cooling and condensing device, and the second desorption gas is returned to the first Heater.
依本發明揭露的有機溶劑回收系統之一態樣,則為一種有機溶劑回收系統,由從生產設備排出的含有有機溶劑之排放氣體,將該有機溶劑回收,具備:冷卻冷凝裝置,藉由將含有該有機溶劑之該排放氣體冷卻,而將該有機溶劑液化冷凝,作為該有機溶劑的濃度已降低之冷卻處理氣體排出;冷卻氣體流通路徑,使該冷卻處理氣體流通;第一濃縮裝置,將從該冷卻氣體流通路徑導入之該冷卻處理氣體所含有的該有機溶劑藉由第一吸附元件吸附,作為該有機溶劑的濃度進一步降低之第一處理氣體排出,導入高溫氣體而從該第一吸附元件使該有機溶劑脫附,作為第一脫附氣體排出;第一處理氣體流通路徑,使該第一處理氣體的一部分流通;冷卻冷凝裝置返回路徑,使從該第一處理氣體流通路徑排出之該第一處理氣體的一部分以外亦即該第一處理氣體的其餘部分,返回至該冷卻冷凝裝置;以及第二濃縮裝置,將從該第一處理氣體流通路徑導入之該第一處理氣體所含有的該有機溶劑藉由第二吸附元件吸附,作為該有機溶劑的濃度進一步降低之第二處理氣體排出,導入高溫氣體而從該第二吸附元件使該有機溶劑脫附,作為第二脫附氣體排出;使該第一脫附氣體,返回至該冷卻冷凝裝置,且使該第二脫附氣體,返回至該冷卻冷凝裝置返回路徑。According to one aspect of the organic solvent recovery system disclosed in the present invention, it is an organic solvent recovery system. The organic solvent is recovered from the exhaust gas containing organic solvent discharged from the production equipment. The organic solvent is equipped with a cooling and condensing device. The exhaust gas containing the organic solvent is cooled, and the organic solvent is liquefied and condensed, and discharged as a cooling processing gas whose concentration of the organic solvent has been reduced; a cooling gas circulation path allows the cooling processing gas to circulate; a first concentrating device The organic solvent contained in the cooling process gas introduced from the cooling gas flow path is adsorbed by the first adsorption element, and discharged as the first process gas whose concentration of the organic solvent is further reduced, and high temperature gas is introduced to adsorb from the first adsorption element. The element desorbs the organic solvent and discharges it as the first desorption gas; the first processing gas flow path allows a part of the first processing gas to circulate; the cooling condensing device return path is used to discharge the gas from the first processing gas flow path A part of the first processing gas, that is, the rest of the first processing gas, is returned to the cooling and condensing device; and a second concentrating device is contained in the first processing gas introduced from the first processing gas flow path The organic solvent is adsorbed by the second adsorption element, and discharged as a second processing gas whose concentration of the organic solvent is further reduced, and a high-temperature gas is introduced to desorb the organic solvent from the second adsorption element as a second desorption gas Discharge; the first desorption gas is returned to the cooling and condensing device, and the second desorption gas is returned to the cooling and condensing device return path.
依本發明揭露的有機溶劑回收系統之一態樣,則為一種有機溶劑回收系統,由從生產設備排出的含有有機溶劑之排放氣體,將該有機溶劑回收,具備:冷卻冷凝裝置,藉由將含有該有機溶劑之該排放氣體冷卻,而將該有機溶劑液化冷凝,作為該有機溶劑的濃度已降低之冷卻處理氣體排出;冷卻氣體流通路徑,使該冷卻處理氣體流通;第一濃縮裝置,將從該冷卻氣體流通路徑導入之該冷卻處理氣體所含有的該有機溶劑藉由第一吸附元件吸附,作為該有機溶劑的濃度進一步降低之第一處理氣體排出,導入高溫氣體而從該第一吸附元件使該有機溶劑脫附,作為第一脫附氣體排出;第一處理氣體流通路徑,使該第一處理氣體的一部分流通;第二濃縮裝置,將從該第一處理氣體流通路徑導入之該第一處理氣體所含有的該有機溶劑藉由第二吸附元件吸附,作為該有機溶劑的濃度進一步降低之第二處理氣體排出,導入高溫氣體而從該第二吸附元件使該有機溶劑脫附,作為第二脫附氣體排出;該冷卻冷凝裝置,包含藉由與冷媒之熱交換而施行冷卻的熱交換器;該有機溶劑回收系統更包含生產設備返回路徑,該生產設備返回路徑使從該生產設備排出之該排放氣體的一部分,於通過該熱交換器後返回至該生產設備;使該第一脫附氣體,返回至該冷卻冷凝裝置,且使該第二脫附氣體,返回至該生產設備返回路徑。According to one aspect of the organic solvent recovery system disclosed in the present invention, it is an organic solvent recovery system. The organic solvent is recovered from the exhaust gas containing organic solvent discharged from the production equipment. The organic solvent is equipped with a cooling and condensing device. The exhaust gas containing the organic solvent is cooled, and the organic solvent is liquefied and condensed, and discharged as a cooling processing gas whose concentration of the organic solvent has been reduced; a cooling gas circulation path allows the cooling processing gas to circulate; a first concentrating device The organic solvent contained in the cooling process gas introduced from the cooling gas flow path is adsorbed by the first adsorption element, and discharged as the first process gas whose concentration of the organic solvent is further reduced, and high temperature gas is introduced to adsorb from the first adsorption element. The element desorbs the organic solvent and discharges it as the first desorption gas; the first processing gas flow path allows a part of the first processing gas to circulate; the second concentrating device introduces the first processing gas through the first processing gas flow path. The organic solvent contained in the first processing gas is adsorbed by the second adsorption element, and discharged as the second processing gas whose concentration of the organic solvent is further reduced, high temperature gas is introduced to desorb the organic solvent from the second adsorption element, It is discharged as the second desorption gas; the cooling and condensing device includes a heat exchanger that performs cooling by heat exchange with the refrigerant; the organic solvent recovery system further includes a production equipment return path, which makes the production equipment return path from the production equipment Part of the exhaust gas discharged from the equipment is returned to the production equipment after passing through the heat exchanger; the first desorbed gas is returned to the cooling and condensing device, and the second desorbed gas is returned to the production The return path of the device.
於該有機溶劑回收系統中,該第一濃縮裝置,將該第一吸附元件於繞筒軸旋轉之中空圓柱狀的轉筒之繞筒軸的圓周方向配置複數個。In the organic solvent recovery system, the first concentrating device arranges a plurality of the first adsorption elements in the circumferential direction around the cylindrical axis of the hollow cylindrical rotating drum rotating around the cylindrical axis.
於該有機溶劑回收系統中,該第二濃縮裝置,將該第二吸附元件配置於繞筒軸旋轉之圓盤狀的吸附轉筒。In the organic solvent recovery system, the second concentrating device arranges the second adsorption element on a disc-shaped adsorption drum rotating around a drum axis.
依本發明揭露的有機溶劑回收系統之一態樣,則為一種有機溶劑回收系統,由從生產設備排出的含有有機溶劑之排放氣體,將該有機溶劑回收,具備:冷卻冷凝裝置,藉由將含有該有機溶劑之該排放氣體冷卻,而將該有機溶劑液化冷凝,作為該有機溶劑的濃度已降低之冷卻處理氣體排出;冷卻氣體流通路徑,使該冷卻處理氣體的一部分流通;第一濃縮裝置,將從該冷卻氣體流通路徑導入之該冷卻處理氣體所含有的該有機溶劑藉由第一吸附元件吸附,作為該有機溶劑的濃度進一步降低之第一處理氣體排出,導入高溫氣體而從該第一吸附元件使該有機溶劑脫附,作為第一脫附氣體排出;第一處理氣體流通路徑,使該第一處理氣體流通;第二濃縮裝置,將從該第一處理氣體流通路徑導入之該第一處理氣體所含有的該有機溶劑藉由第二吸附元件吸附,作為該有機溶劑的濃度進一步降低之第二處理氣體排出,導入高溫氣體而從該第二吸附元件使該有機溶劑脫附,作為第二脫附氣體排出;該冷卻冷凝裝置,包含藉由與冷媒之熱交換而施行該排放氣體的冷卻之熱交換器;該有機溶劑回收系統更包含熱交換器返回路徑,該熱交換器返回路徑使該冷卻處理氣體的一部分以外亦即該冷卻處理氣體的其餘部分,返回至該熱交換器;使該第一脫附氣體,返回至該冷卻冷凝裝置,且使該第二脫附氣體,返回至該冷卻氣體流通路徑。According to one aspect of the organic solvent recovery system disclosed in the present invention, it is an organic solvent recovery system. The organic solvent is recovered from the exhaust gas containing organic solvent discharged from the production equipment. The organic solvent is equipped with a cooling and condensing device. The exhaust gas containing the organic solvent is cooled, and the organic solvent is liquefied and condensed, and discharged as a cooling processing gas whose concentration of the organic solvent has been reduced; a cooling gas circulation path, allowing a part of the cooling processing gas to circulate; a first concentrating device , The organic solvent contained in the cooling processing gas introduced from the cooling gas flow path is adsorbed by the first adsorption element, and discharged as the first processing gas whose concentration of the organic solvent is further reduced, and the high temperature gas is introduced from the first adsorption element An adsorption element desorbs the organic solvent and discharges it as the first desorption gas; the first processing gas circulation path allows the first processing gas to circulate; and the second concentrating device introduces the first processing gas through the first processing gas circulation path. The organic solvent contained in the first processing gas is adsorbed by the second adsorption element, and discharged as the second processing gas whose concentration of the organic solvent is further reduced, high temperature gas is introduced to desorb the organic solvent from the second adsorption element, It is discharged as the second desorption gas; the cooling and condensing device includes a heat exchanger that performs cooling of the exhaust gas by heat exchange with a refrigerant; the organic solvent recovery system further includes a heat exchanger return path, the heat exchanger The return path allows part of the cooling process gas, that is, the rest of the cooling process gas, to return to the heat exchanger; to return the first desorption gas to the cooling and condensing device, and to make the second desorption gas , Return to the cooling gas flow path.
依本發明揭露的有機溶劑回收系統之一態樣,則為一種有機溶劑回收系統,由從生產設備排出的含有有機溶劑之排放氣體,將該有機溶劑回收,具備:冷卻冷凝裝置,藉由將含有該有機溶劑之該排放氣體冷卻,而將該有機溶劑液化冷凝,作為該有機溶劑的濃度已降低之冷卻處理氣體排出;冷卻氣體流通路徑,使該冷卻處理氣體的一部分流通;第一濃縮裝置,將從該冷卻氣體流通路徑導入之該冷卻處理氣體所含有的該有機溶劑藉由第一吸附元件吸附,作為該有機溶劑的濃度進一步降低之第一處理氣體排出,藉由加熱器導入高溫氣體而從該第一吸附元件使該有機溶劑脫附,作為第一脫附氣體排出;第一處理氣體流通路徑,使該第一處理氣體流通;以及第二濃縮裝置,將從該第一處理氣體流通路徑導入之該第一處理氣體所含有的該有機溶劑藉由第二吸附元件吸附,作為該有機溶劑的濃度進一步降低之第二處理氣體排出,導入高溫氣體而從該第二吸附元件使該有機溶劑脫附,作為第二脫附氣體排出;該冷卻冷凝裝置,包含藉由與冷媒之熱交換而施行該排放氣體的冷卻之熱交換器;該有機溶劑回收系統更包含熱交換器返回路徑,該熱交換器返回路徑使該冷卻處理氣體的一部分以外亦即該冷卻處理氣體的其餘部分,返回至該熱交換器;使該第一脫附氣體,返回至該冷卻冷凝裝置,且使該第二脫附氣體,返回至該加熱器。According to one aspect of the organic solvent recovery system disclosed in the present invention, it is an organic solvent recovery system. The organic solvent is recovered from the exhaust gas containing organic solvent discharged from the production equipment. The organic solvent is equipped with a cooling and condensing device. The exhaust gas containing the organic solvent is cooled, and the organic solvent is liquefied and condensed, and discharged as a cooling processing gas whose concentration of the organic solvent has been reduced; a cooling gas circulation path, allowing a part of the cooling processing gas to circulate; a first concentrating device , The organic solvent contained in the cooling processing gas introduced from the cooling gas flow path is adsorbed by the first adsorption element, and discharged as the first processing gas whose concentration of the organic solvent is further reduced, and high temperature gas is introduced by a heater The organic solvent is desorbed from the first adsorption element and discharged as the first desorption gas; the first processing gas flow path allows the first processing gas to circulate; and the second concentrating device removes the first processing gas from The organic solvent contained in the first processing gas introduced in the flow path is adsorbed by the second adsorption element, and discharged as the second processing gas whose concentration of the organic solvent is further reduced, and the high temperature gas is introduced to make the second adsorption element The organic solvent is desorbed and discharged as the second desorption gas; the cooling and condensing device includes a heat exchanger that performs cooling of the exhaust gas by heat exchange with a refrigerant; the organic solvent recovery system further includes a heat exchanger return path , The heat exchanger return path makes part of the cooling process gas, that is, the rest of the cooling process gas, return to the heat exchanger; returns the first desorbed gas to the cooling and condensing device, and makes the The second desorption gas returns to the heater.
依本發明揭露的有機溶劑回收系統之一態樣,則為一種有機溶劑回收系統,由從生產設備排出的含有有機溶劑之排放氣體,將該有機溶劑回收,具備:冷卻冷凝裝置,藉由將含有該有機溶劑之該排放氣體冷卻,而將該有機溶劑液化冷凝,作為該有機溶劑的濃度已降低之冷卻處理氣體排出;冷卻氣體流通路徑,使該冷卻處理氣體的一部分流通;第一濃縮裝置,將從該冷卻氣體流通路徑導入之該冷卻處理氣體所含有的該有機溶劑藉由第一吸附元件吸附,作為該有機溶劑的濃度進一步降低之第一處理氣體排出,導入高溫氣體而從該第一吸附元件使該有機溶劑脫附,作為第一脫附氣體排出;第一處理氣體流通路徑,使該第一處理氣體流通;第二濃縮裝置,將從該第一處理氣體流通路徑導入之該第一處理氣體所含有的該有機溶劑藉由第二吸附元件吸附,作為該有機溶劑的濃度進一步降低之第二處理氣體排出,導入高溫氣體而從該第二吸附元件使該有機溶劑脫附,作為第二脫附氣體排出;該冷卻冷凝裝置,包含藉由與冷媒之熱交換而施行冷卻的熱交換器;該有機溶劑回收系統更包含熱交換器返回路徑,該熱交換器返回路徑使該冷卻處理氣體的一部分以外亦即該冷卻處理氣體的其餘部分,返回至該熱交換器;使該第一脫附氣體,返回至該冷卻冷凝裝置,且使該第二脫附氣體,返回至該熱交換器返回路徑。According to one aspect of the organic solvent recovery system disclosed in the present invention, it is an organic solvent recovery system. The organic solvent is recovered from the exhaust gas containing organic solvent discharged from the production equipment. The organic solvent is equipped with a cooling and condensing device. The exhaust gas containing the organic solvent is cooled, and the organic solvent is liquefied and condensed, and discharged as a cooling processing gas whose concentration of the organic solvent has been reduced; a cooling gas circulation path, allowing a part of the cooling processing gas to circulate; a first concentrating device , The organic solvent contained in the cooling processing gas introduced from the cooling gas flow path is adsorbed by the first adsorption element, and discharged as the first processing gas whose concentration of the organic solvent is further reduced, and the high temperature gas is introduced from the first adsorption element An adsorption element desorbs the organic solvent and discharges it as the first desorption gas; the first processing gas circulation path allows the first processing gas to circulate; and the second concentrating device introduces the first processing gas through the first processing gas circulation path. The organic solvent contained in the first processing gas is adsorbed by the second adsorption element, and discharged as the second processing gas whose concentration of the organic solvent is further reduced, high temperature gas is introduced to desorb the organic solvent from the second adsorption element, Is discharged as the second desorbed gas; the cooling and condensing device includes a heat exchanger that performs cooling by heat exchange with the refrigerant; the organic solvent recovery system further includes a heat exchanger return path, and the heat exchanger return path causes the Part of the cooling process gas, that is, the rest of the cooling process gas, is returned to the heat exchanger; the first desorbed gas is returned to the cooling and condensing device, and the second desorbed gas is returned to the Heat exchanger return path.
依本發明揭露的有機溶劑回收系統之一態樣,則為一種有機溶劑回收系統,由從生產設備排出的含有有機溶劑之排放氣體,將該有機溶劑回收,具備:冷卻冷凝裝置,藉由將含有該有機溶劑之該排放氣體冷卻,而將該有機溶劑液化冷凝,作為該有機溶劑的濃度已降低之冷卻處理氣體排出;冷卻氣體流通路徑,使該冷卻處理氣體的一部分流通;第一濃縮裝置,將從該冷卻氣體流通路徑導入之該冷卻處理氣體所含有的該有機溶劑藉由第一吸附元件吸附,作為該有機溶劑的濃度進一步降低之第一處理氣體排出,導入高溫氣體而從該第一吸附元件使該有機溶劑脫附,作為第一脫附氣體排出;第一處理氣體流通路徑,使該第一處理氣體流通;第二濃縮裝置,將從該第一處理氣體流通路徑導入之該第一處理氣體所含有的該有機溶劑藉由第二吸附元件吸附,作為該有機溶劑的濃度進一步降低之第二處理氣體排出,導入高溫氣體而從該第二吸附元件使該有機溶劑脫附,作為第二脫附氣體排出;該冷卻冷凝裝置,包含藉由與冷媒之熱交換而施行冷卻的熱交換器;該有機溶劑回收系統,更包含:熱交換器返回路徑,使該冷卻處理氣體的一部分以外亦即該冷卻處理氣體的其餘部分,返回至該熱交換器;以及生產設備返回路徑,使從該生產設備排出之該排放氣體的一部分,於通過該熱交換器後返回至該生產設備;使該第一脫附氣體,返回至該冷卻冷凝裝置,且使該第二脫附氣體,返回至該生產設備返回路徑。According to one aspect of the organic solvent recovery system disclosed in the present invention, it is an organic solvent recovery system. The organic solvent is recovered from the exhaust gas containing organic solvent discharged from the production equipment. The organic solvent is equipped with a cooling and condensing device. The exhaust gas containing the organic solvent is cooled, and the organic solvent is liquefied and condensed, and discharged as a cooling processing gas whose concentration of the organic solvent has been reduced; a cooling gas circulation path, allowing a part of the cooling processing gas to circulate; a first concentrating device , The organic solvent contained in the cooling processing gas introduced from the cooling gas flow path is adsorbed by the first adsorption element, and discharged as the first processing gas whose concentration of the organic solvent is further reduced, and the high temperature gas is introduced from the first adsorption element An adsorption element desorbs the organic solvent and discharges it as the first desorption gas; the first processing gas circulation path allows the first processing gas to circulate; and the second concentrating device introduces the first processing gas through the first processing gas circulation path. The organic solvent contained in the first processing gas is adsorbed by the second adsorption element, and discharged as the second processing gas whose concentration of the organic solvent is further reduced, high temperature gas is introduced to desorb the organic solvent from the second adsorption element, Is discharged as the second desorption gas; the cooling and condensing device includes a heat exchanger that performs cooling by heat exchange with the refrigerant; the organic solvent recovery system further includes: a heat exchanger return path to cool the treated gas Part of the gas, that is, the remaining part of the cooling process gas, is returned to the heat exchanger; and the production equipment return path, so that a part of the exhaust gas discharged from the production equipment returns to the production equipment after passing through the heat exchanger ; Make the first desorption gas return to the cooling and condensing device, and make the second desorption gas return to the return path of the production equipment.
於該有機溶劑回收系統中,該第一濃縮裝置,將該第一吸附元件於繞筒軸旋轉之中空圓柱狀的轉筒之繞筒軸的圓周方向配置複數個。In the organic solvent recovery system, the first concentrating device arranges a plurality of the first adsorption elements in the circumferential direction around the cylindrical axis of the hollow cylindrical rotating drum rotating around the cylindrical axis.
於該有機溶劑回收系統中,該第二濃縮裝置,將該第二吸附元件配置於繞筒軸旋轉之圓盤狀的吸附轉筒。 [本發明之效果]In the organic solvent recovery system, the second concentrating device arranges the second adsorption element on a disc-shaped adsorption drum rotating around a drum axis. [Effects of the invention]
依本發明揭露之內容,可提供一種有機溶劑回收系統,可從排放氣體將有機溶劑更高效率地回收。According to the disclosure of the present invention, an organic solvent recovery system can be provided, which can recover organic solvents from exhaust gas more efficiently.
針對依據本發明之各實施形態的有機溶劑回收系統,以下,參考圖式並予以說明。以下說明之實施形態中,在提及個數、數量等的情況,除了特別記載的情況以外,本發明之範圍並未限定於該個數、數量等。有對相同之零件、相當之零件,給予相同參考符號而不重複進行說明的情況。從一開始,即預定將實施形態之構成適當地組合使用。The organic solvent recovery system according to each embodiment of the present invention is described below with reference to the drawings. In the embodiments described below, when the number, number, etc. are mentioned, the scope of the present invention is not limited to the number, number, etc., except in the case of special description. There are cases where the same reference symbols are given to the same or equivalent parts without repeating the description. From the beginning, it is planned to appropriately combine and use the constitution of the embodiment.
[實施形態1A]
圖1係概略顯示實施形態1A之有機溶劑回收系統1A之構成的圖。有機溶劑回收系統1A,係以冷卻冷凝裝置100、濃縮裝置300、第一流通路徑F1、及第二流通路徑F2構成。[
冷卻冷凝裝置100,具備冷卻部110、分離部120及腔室123。含有有機溶劑之排放氣體G1,藉由通過冷卻部110而冷卻,該有機溶劑伴隨於此而液化冷凝。接著,該排放氣體G2,藉由通過分離部120,而分離為經液化冷凝之冷卻冷凝液L1與有機溶劑濃度降低之冷卻處理氣體G3。最後,以通過腔室123,將冷卻處理氣體的一部分(吸附入口氣體)G4往濃縮裝置300供給之方式分配,從冷卻冷凝裝置100排出。The cooling and condensing
冷卻部110之冷卻手段/構成並無特別限定,有藉由冷卻水、冷水、鹹水等冷媒與排放氣體之間接熱交換而進行冷卻的第一熱交換器111等。冷卻溫度等之條件,亦依作為回收對象的有機溶劑適當決定即可。The cooling means/configuration of the
此外,冷卻部110,亦可於第一熱交換器111之前,設置藉由冷卻處理氣體的其餘部分(返回氣體)G6與排放氣體G1之熱交換而使排放氣體G1冷卻的第二熱交換器112。此係由於可減少第一熱交換器111所需之傳熱面積與冷媒量的緣故。In addition, the
分離部120之分離手段/構成並無特別限定,具有除霧器、濾網、篩孔等接觸液滴而加以捕捉的網眼狀構造體121等。網眼狀構造體121捕捉到之冷卻冷凝液L1,因重力而往配置於網眼狀構造體121的下部之貯存槽125集液,作為回收液L3回收。The separation means/configuration of the
腔室123,係具有一定容量之空間的構造體。分配給往濃縮裝置300供給之冷卻處理氣體的一部分(吸附入口氣體)G4、及冷卻處理氣體的其餘部分(返回氣體)G6。腔室123具備分隔部128,分隔部128可與從網眼狀構造體121排出之冷卻處理氣體G3的排氣方向對向而進行第一流通路徑F1的吸入。The
濃縮裝置300具備包含吸附材之吸附元件310,藉由與氣體接觸而吸附其含有的有機溶劑,藉由與加熱氣體接觸而使吸附的有機溶劑脫附。此外,吸附元件310,包含脫附部(脫附區)311與吸附部(吸附區)312。吸附部312,藉由將冷卻處理氣體的一部分(吸附入口氣體)G4導入,而使冷卻處理氣體的一部分(吸附入口氣體)G4與吸附材接觸,藉以將冷卻處理氣體的一部分(吸附入口氣體)G4所含有之有機溶劑吸附於吸附材,藉此使冷卻處理氣體的一部分(吸附入口氣體)G4潔淨化,作為潔淨氣體G9排出。The concentrating
脫附部311,藉由將較冷卻處理氣體的一部分(吸附入口氣體)G4更高溫之氣體G10導入至吸附材,而使有機溶劑從吸附材脫附,藉此作為含有有機溶劑之脫附氣體G11排出。The
作為吸附元件310所包含之吸附材,廣泛利用活性氧化鋁、矽膠、活性碳材料或沸石,其中特別適合利用活性碳與疏水性沸石。活性碳與疏水性沸石,將低濃度的有機化合物吸附、脫附之功能良好,一直以來作為吸附材利用在各種裝置。As the adsorption material contained in the
此外,實施形態之濃縮裝置的具體構成並無特別限定,但如圖1所示,已知下述構成:具備旋轉軸、及繞旋轉軸而設置之吸附元件310,藉由使吸附元件310繞旋轉軸旋轉,而於吸附部312中,使吸附有冷卻處理氣體的一部分(吸附入口氣體)G4中的有機溶劑之吸附材連續地往脫附部311移動。In addition, the specific configuration of the concentrating device of the embodiment is not particularly limited. However, as shown in FIG. 1, the following configuration is known: a rotating shaft and an
實施形態之濃縮裝置300,如圖1所示,脫附部311宜配置於較吸附部312更為下部。此係因即便在脫附氣體G11中所含有的有機溶劑之一部分液化冷凝而產生脫附冷凝液L2的情況中,仍使脫附冷凝液L2不易附著於吸附部312之緣故。使脫附冷凝液L2,往較脫附部311更下部滴落,沿著脫附部之外部的內面等而回收。更佳態樣中,如圖1所示,宜使脫附部311往下方傾斜。此係為了使脫附冷凝液L2更容易往下方滴落。In the
濃縮裝置300,亦可具備脫附部311之脫附處理結束的部分在往吸附部312移動之前往其移動的吹掃部(未圖示)。亦可為將潔淨氣體G9的一部分導入至吹掃部,將從吹掃部排出之吹掃部出口氣體導入至吸附部312之構成。此係因藉由以潔淨氣體G9吹掃結束脫附的吸附材,而防止殘留於吸附材之脫附氣體G11往潔淨氣體G9的混入,可將吸附材冷卻之緣故。The concentrating
濃縮裝置300,使用於脫附之高溫氣體G10,宜為利用再生加熱器350等加熱手段使潔淨氣體G9的一部分成為高溫狀態者。此係因不在吸附部312增加有機溶劑含有氣體的處理風量之緣故。排放氣體G1的溫度為50~200℃的溫度之情況中,更宜以再生加熱器350等使排放氣體G1的一部分升溫而使用。此係因藉由將高溫之排放氣體G1使用於脫附,而可降低再生加熱器350的使用效用,藉由排放氣體G1的溫度而使脫附不需要再生加熱器350之緣故。此外,將排放氣體G1及脫附氣體G11通過冷卻冷凝裝置100的比例,假設為排放氣體G1為0%~50%,脫附氣體G11為50%~100%。The concentrating
第一流通路徑F1,係將冷卻處理氣體的一部分(吸附入口氣體)G4從腔室123往濃縮裝置300導入之部位。第一流通路徑F1的往腔室123之連接口,宜為腔室123之頂棚部127。此係為了抑制分離部120未捕捉到的微少液滴之往濃縮裝置300的侵入,防止後述因濃縮裝置300之吸附元件310的潤濕所造成之性能降低/強度降低等。更佳態樣中,宜設置分隔部128,以與冷卻處理氣體G3的流通方向對向之方式,將冷卻處理氣體的一部分(吸附入口氣體)G4取出。可進一步防止液滴的侵入。除此之外,亦可於冷卻處理氣體的一部分(吸附入口氣體)G4之取出口,設置與上述網眼狀構造體121類似的防液滴侵入構件,亦可設置用於使液滴氣化的加熱器。The first flow path F1 is a part where a part of the cooling process gas (adsorption inlet gas) G4 is introduced from the
第二流通路徑F2,係將脫附氣體G11送回至冷卻冷凝裝置100之排放氣體G1的導入部之部位。第二流通路徑F2,宜以將脫附部311配置於較脫附氣體G11與往冷卻冷凝裝置100供給之排放氣體G1的合流位置更為上部之方式連接。此係因由濃縮裝置300之脫附氣體G11產生的脫附冷凝液L2,容易往冷卻冷凝裝置100移動之緣故。更佳態樣中,宜構成為使冷卻冷凝裝置100之排放氣體G1的導入部及貯存槽125此兩處流通。此係使由脫附氣體G11產生的脫附冷凝液L2變得容易直接往貯存槽125回收之緣故。The second flow path F2 is to return the desorbed gas G11 to the inlet of the exhaust gas G1 of the cooling and condensing
實施形態的有機溶劑回收系統1A之濃縮裝置300的使用於脫附之高溫氣體G10,如同前述宜為利用再生加熱器350等加熱手段使潔淨氣體G9的一部分成為高溫狀態者,但在排放氣體G1的溫度為50~200℃的溫度之情況中,更宜以再生加熱器350等使排放氣體G1的一部分升溫而使用。此係因藉由將高溫之排放氣體使用於脫附,而可降低再生加熱器350的使用效用,藉由排放氣體G1的溫度而使脫附不需要再生加熱器350之緣故。此外,將排放氣體G1及脫附氣體G11往冷卻冷凝裝置100通過的比例,假設為排放氣體G1為0%~50%,脫附氣體G11為50%~100%。The
排放氣體G1,係從生產設備130排出之氣體的情況,亦可成為使冷卻處理氣體的其餘部分(返回氣體)G6,返回至生產設備130之構成。When the exhaust gas G1 is the gas discharged from the
欲進一步降低冷卻處理氣體的其餘部分(返回氣體)G6所包含之有機溶劑濃度的情況,亦可如圖2所示,追加導入將冷卻處理氣體的其餘部分(返回氣體)G6予以處理之濃縮裝置500。此外,欲進一步降低潔淨氣體G9所包含之有機溶劑濃度的情況,亦可如圖3所示,追加導入將潔淨氣體G9予以處理之濃縮裝置600。濃縮裝置500、濃縮裝置600,可與濃縮裝置300為相同構成,亦可為其他構成。此外,追加導入之濃縮裝置數量並無限制。將從任一濃縮裝置排出之脫附氣體,經由第二流通路徑F2,送回至冷卻冷凝裝置100之排放氣體G1的導入部。To further reduce the concentration of the organic solvent contained in the remaining part of the cooling process gas (return gas) G6, as shown in Figure 2, an additional concentrating device for processing the remaining part of the cooling process gas (return gas) G6 can be introduced. 500. In addition, if it is desired to further reduce the concentration of the organic solvent contained in the clean gas G9, as shown in FIG. 3, a concentrating
在實施形態,作為排放氣體G1所含有的有機溶劑,列舉可藉由1℃~50℃之冷卻而液化回收的有機溶劑。作為有機溶劑,例如為N-甲基吡咯烷酮、N-乙基吡咯烷酮、N,N-二甲基甲醯胺、N,N-二甲基乙醯胺、或正癸烷。其等僅為例示,並未限定於其等。所含有的有機溶劑,可為1種亦可為複數種。In the embodiment, examples of the organic solvent contained in the exhaust gas G1 include organic solvents that can be liquefied and recovered by cooling at 1°C to 50°C. The organic solvent is, for example, N-methylpyrrolidone, N-ethylpyrrolidone, N,N-dimethylformamide, N,N-dimethylacetamide, or n-decane. These etc. are only examples, and are not limited to them. The organic solvent contained may be one type or plural types.
[實施形態1B]
圖4係概略顯示實施形態1B的有機溶劑回收系統1B之構成的圖。有機溶劑回收系統1B,係由冷卻冷凝裝置100、第一濃縮裝置200、第二濃縮裝置300、及各種流通路徑構成。[
冷卻冷凝裝置100,具備冷卻部110及分離部120。含有有機溶劑之排放氣體G1,從生產設備130排出。排放氣體G1,藉由通過冷卻部110而冷卻。排放氣體G1,伴隨通過冷卻部110而使有機溶劑液化冷凝。The cooling and condensing
通過冷卻部110之排放氣體G2,藉由通過分離部120,而分離為經液化冷凝之冷卻冷凝液L1與有機溶劑濃度降低之冷卻處理氣體G3。冷卻處理氣體G3,通過腔室123,作為冷卻處理氣體G4從冷卻冷凝裝置100往第一濃縮裝置200排出。The exhaust gas G2 passing through the cooling
冷卻部110之冷卻手段及構成,並無特別限定。在實施形態1B,使用藉由冷卻水、冷水、鹹水等冷媒與排放氣體之間接熱交換而進行冷卻的第一熱交換器111。第一熱交換器111,位於使排放氣體G1往上下方向流通之位置。The cooling means and structure of the
冷卻部110,於第一熱交換器111之前,設置藉由後述冷卻處理氣體G6與排放氣體G1之熱交換而使排放氣體G1冷卻的第二熱交換器112。第二熱交換器112,可減少第一熱交換器111所需之傳熱面積與冷媒量。排放氣體G1及冷卻處理氣體G6的一部分,通過第五流通路徑F5往生產設備130返回。第一熱交換器111及第二熱交換器112中的冷卻溫度等之條件,依作為回收對象的有機溶劑適當決定即可。The
分離部120之分離手段及構成並無特別限定。在實施形態1B,使用除霧器、濾網、及篩孔等接觸液滴而加以捕捉的網眼狀構造體121。分離部120具備漏斗狀之承接部122,承接部122承接以冷卻部110冷卻的包含有機溶劑之冷卻冷凝液L1。以冷卻部110冷卻之冷卻冷凝液L1、及網眼狀構造體121捕捉到之冷卻冷凝液L1,因重力而流至承接部122後,往配置於承接部122的下部之貯存槽125集液,作為回收液L3回收。The separation means and structure of the
腔室123,係具有一定容量之空間的構造體。於腔室123內,設置堰部124。堰部124,防止冷卻冷凝液L1的一部分往腔室123之前端方向移動而往作為冷卻氣體流通路徑的第一流通路徑F1流通之情形。堰部124,達到將冷卻冷凝液L1確實地回收之作用。使於腔室123內貯存一定時間之冷卻處理氣體G3,作為冷卻處理氣體G4在第一流通路徑F1流通,往第一濃縮裝置200供給。The
在有機溶劑回收系統1B,沿著排放氣體G1的流動方向觀察之情況,相對於從冷卻部110往分離部120流動的方向,使分離部120內從網眼狀構造體121往腔室123流動的方向交叉,藉以成為使排放氣體G1(排放氣體G2、冷卻處理氣體G3)沿L字形方向流動的構造。In the organic
有機溶劑回收系統1B,以冷卻部110與分離部120構成處為L字形構造,故可抑制因液滴、飛沫而使第一濃縮裝置200及第二濃縮裝置300暴露的情形。第一濃縮裝置200及第二濃縮裝置300,若暴露而吸附劑潤濕,則有強度降低或破損的可能。有機溶劑回收系統1B,藉由具有L字形構造,而可防止第一濃縮裝置200及第二濃縮裝置300之強度降低或破損。The organic
第一濃縮裝置200具備包含吸附材之吸附轉筒212,藉由與氣體接觸而吸附其含有的有機溶劑,藉由與加熱氣體接觸而使吸附的有機溶劑脫附。吸附轉筒212,係由以複數個分隔部分隔出之複數個吸附單元210構成。吸附轉筒212,藉由複數個吸附單元210而使全體成為中空圓柱狀的形狀。吸附轉筒212,設置於處理室內,設置為流體可沿徑方向流動。吸附轉筒212,設置為受到馬達之旋轉驅動力而可繞筒軸旋轉。The first concentrating
在第一濃縮裝置200,使吸附單元210的一部分構成吸附部,吸附從吸附單元210的外側向內側供給之冷卻處理氣體G4所含有的有機溶劑;且使吸附單元210的其餘部分構成脫附部,藉由從吸附單元210的內側向外側供給加熱空氣而使吸附於吸附單元210的有機溶劑從吸附單元210脫附。In the first concentrating
潔淨化時,將供給至處理室內之冷卻處理氣體G4,從吸附轉筒212的外周面往吸附部導入。導入至吸附部之冷卻處理氣體G4,在沿著徑方向從外周面向內周面通過吸附轉筒212時,將有機溶劑吸附至位於吸附部之複數個吸附單元210,藉以潔淨化。At the time of cleaning, the cooled processing gas G4 supplied into the processing chamber is introduced from the outer peripheral surface of the
將經潔淨化的作為被處理流體之冷卻處理氣體G5、G6,作為潔淨氣體,從吸附單元210之上部排出。使排出之潔淨氣體的一部分,作為冷卻處理氣體G5在第二流通路徑F2流通,往第二濃縮裝置300供給。使排出之潔淨氣體的一部分,作為冷卻處理氣體G6在第四流通路徑F4流通,往第二熱交換器112返回。The cleaned cooling processing gases G5 and G6 serving as the fluid to be processed are discharged from the upper portion of the
內周側流路形成構件211及外周側流路形成構件213,以將圓周方向中之吸附轉筒212的一部分夾入之方式,於吸附轉筒212的內周側及外周側中彼此相對向地配置。由內周側流路形成構件211及外周側流路形成構件213所包夾之吸附轉筒212的區域為脫附部。The inner circumference side flow
為了施行有機溶劑之脫附,而從內周側流路形成構件211,對脫附部導入藉由再生加熱器250加熱之冷卻處理氣體G5的一部分即高溫氣體G7。導入至脫附部之高溫氣體G7,在通過吸附轉筒212時,從位於脫附部之複數個吸附單元210,藉由熱使吸附於其等的有機溶劑脫附。含有有機溶劑之脫附氣體G8,作為濃縮氣體,從脫附部通過外周側流路形成構件213,往處理室外排出,返回至第三流通路徑F3。將脫附氣體G8中所含有的有機溶劑之一部分液化冷凝,作為脫附冷凝液L2往貯存槽125集液。In order to perform the desorption of the organic solvent, the high-temperature gas G7, which is a part of the cooling process gas G5 heated by the
第三流通路徑F3,係將脫附氣體G8及後述脫附氣體G11送回至冷卻冷凝裝置100之排放氣體G1的導入部之部位。第三流通路徑F3,宜以將脫附部配置於較脫附氣體與往冷卻冷凝裝置100供給之排放氣體G1的合流位置更為上部之方式連接。此係因由第一濃縮裝置200之脫附氣體G8及第二濃縮裝置300之脫附氣體G11產生的脫附冷凝液L2,容易往冷卻冷凝裝置100移動之緣故。第三流通路徑F3,宜構成為使冷卻冷凝裝置100之排放氣體G1的導入部及貯存槽125此兩處流通。此係使由脫附氣體G8及脫附氣體G11產生的脫附冷凝液L2變得容易直接往貯存槽125回收之緣故。The third flow path F3 is a part where the desorbed gas G8 and the desorbed gas G11 described later are returned to the inlet of the exhaust gas G1 of the cooling and condensing
於第一濃縮裝置200中,對位於吸附部之吸附單元210施行被處理物質的吸附處理,對在吸附處理後位於脫附部之吸附單元210施行被處理物質的脫附處理。藉由使吸附轉筒212繞筒軸旋轉,而使吸附單元210將脫附部與吸附部交互地移動,連續地實施被處理物質的吸附處理與脫附處理。In the first concentrating
作為構成吸附單元210之吸附元件的材料,可利用活性氧化鋁、矽膠、活性碳材料、沸石等。吸附單元210中之吸附元件的形狀並無特別限定,例如,可為將含有活性碳材料或沸石之薄片形成為蜂巢狀者,亦可為將活性碳纖維不織布疊層者。As the material constituting the adsorption element of the
第二濃縮裝置300具備包含吸附材之吸附元件310,藉由與氣體接觸而吸附其含有的有機溶劑,藉由與加熱氣體接觸而使吸附的有機溶劑脫附。吸附元件310,包含脫附部(脫附區)311與吸附部(吸附區)312。吸附部312,藉由將冷卻處理氣體G5導入,而使冷卻處理氣體G5與吸附材接觸,藉以將冷卻處理氣體G5所含有的有機溶劑吸附於吸附材,使冷卻處理氣體G5潔淨化,作為潔淨氣體G9排出。The second concentrating
脫附部311,藉由將較冷卻處理氣體G5更高溫之氣體G10導入至吸附材,而使有機溶劑從吸附材脫附,藉此作為含有有機溶劑之脫附氣體G11排出。The
作為吸附元件310所包含之吸附材,廣泛利用活性氧化鋁、矽膠、活性碳材料或沸石,其中特別適合利用活性碳與疏水性沸石。As the adsorption material contained in the
如圖4所示,第二濃縮裝置300,具備旋轉軸、及繞旋轉軸而設置之吸附元件310。第二濃縮裝置300,為下述構成:藉由使吸附元件310繞旋轉軸旋轉,而於吸附部312中,使吸附有從第二流通路徑F2導入之冷卻處理氣體G5中的有機溶劑之吸附材連續地往脫附部311移動。As shown in FIG. 4, the second concentrating
如圖4所示,第二濃縮裝置300,宜將脫附部311配置於較吸附部312更為下部。此係因即便在脫附氣體G11中所含有的有機溶劑之一部分液化冷凝而產生脫附冷凝液L2的情況中,仍使脫附冷凝液L2不易附著於吸附部312之緣故。使脫附冷凝液L2,往較脫附部311更下部滴落,沿著脫附部之外部的內面等而回收。更佳態樣中,宜為了使脫附冷凝液L2更容易往下方滴落,而使脫附部311往下方傾斜。As shown in FIG. 4, in the second concentrating
第二濃縮裝置300,亦可具備脫附部311之脫附處理結束的部分在往吸附部312移動之前往其移動的清潔部(吹掃部)。亦可為將潔淨氣體G9的一部分導入至吹掃部,將從吹掃部排出之吹掃部出口氣體導入至吸附部312之構成。此係因藉由以潔淨氣體G9清潔結束脫附的吸附材,而防止殘留於吸附材之脫附氣體G11往潔淨氣體G9的混入,可將吸附材冷卻之緣故。The second concentrating
使用於脫附之高溫氣體G10,宜為利用再生加熱器350等加熱手段使潔淨氣體G9的一部分成為高溫狀態者。此係因吸附部312中,不增加有機溶劑含有氣體的處理風量之緣故。The high-temperature gas G10 used for desorption is preferably one that uses heating means such as the
[實施形態2B]
圖5係概略顯示實施形態2B的有機溶劑回收系統2B之構成的圖。有機溶劑回收系統2B,係由冷卻冷凝裝置100、第一濃縮裝置200、第二濃縮裝置300、及各種流通路徑構成。有機溶劑回收系統2B,除了下述點以外之構成,與實施形態1B的有機溶劑回收系統1B相同:於腔室123內設置加熱器126。[
加熱器126,將冷卻後之冷卻處理氣體G3略為加熱。藉由將冷卻處理氣體G3略微加熱,而可防止有機溶劑或水分之冷凝。The
[作用/效果]
本實施形態之冷卻冷凝裝置100,包含:冷卻部110,使排放氣體G1流通;以及分離部120,在沿著排放氣體G1的流動方向觀察之情況,位於冷卻部110的下游側。分離部120,具備:承接部122,承接以冷卻部110冷卻的含有有機溶劑之冷卻冷凝液L1;網眼狀構造體121,藉由接觸冷卻後之排放氣體G2,而使冷卻冷凝液L1與冷卻處理氣體G3分離;以及腔室123,將通過網眼狀構造體121後之冷卻處理氣體G3貯存一定時間。[Effect]
The cooling and condensing
沿著排放氣體G1的流動方向觀察之情況,相對於從冷卻部110往分離部120流動的方向,使分離部120內從網眼狀構造體121往腔室123流動的方向交叉,藉以使該排放氣體沿L字形方向流動。藉此,可從排放氣體G1將含有有機溶劑之冷卻冷凝液L1更高效率地回收。本實施形態之有機溶劑回收系統,由於以冷卻部110與分離部120構成處為L字形構造,故可抑制因液滴、飛沫而使設置於後段之第一濃縮裝置200及第二濃縮裝置300暴露的情形。When viewed along the flow direction of the exhaust gas G1, with respect to the direction from the
於本實施形態之網眼狀構造體121的下游側,配置用於將冷卻處理氣體G3加熱之加熱器126。藉此,藉由將冷卻處理氣體G3略微加熱,而可防止有機溶劑或水分之冷凝。On the downstream side of the
於本實施形態之腔室123內,設置堰部124。藉此,可防止冷卻冷凝液L1往作為冷卻氣體流通路徑之第一流通路徑F1流動。In the
本實施形態之濃縮裝置,包含第一濃縮裝置200、及位於第一濃縮裝置的下游側之第二濃縮裝置300。第一濃縮裝置200,將從第一流通路徑F1導入之冷卻處理氣體G4所含有的有機溶劑藉由吸附單元210吸附,作為有機溶劑的濃度進一步降低之冷卻處理氣體G5排出,導入高溫氣體G7而從吸附單元210使有機溶劑脫附,作為脫附氣體G8排出。The concentration device of this embodiment includes a
本實施形態之有機溶劑回收系統,更包含使冷卻處理氣體G5的一部分流通之第二流通路徑F2;第二濃縮裝置300,將從第二流通路徑F2導入之冷卻處理氣體G5所含有的有機溶劑藉由吸附元件310吸附,作為有機溶劑的濃度進一步降低之潔淨氣體G9排出,導入高溫氣體G10而從吸附元件310使有機溶劑脫附,作為脫附氣體G11排出。The organic solvent recovery system of this embodiment further includes a second flow path F2 for circulating a part of the cooling process gas G5; the second concentrating
將本實施形態之第一濃縮裝置200,於使吸附單元210繞筒軸旋轉之中空圓柱狀的轉筒之繞筒軸的圓周方向配置複數個。藉此,可高效率地回收有機溶劑。The first concentrating
本實施形態之第二濃縮裝置300,將吸附元件310配置於繞筒軸旋轉之圓盤狀的吸附轉筒。藉此,可高效率地回收有機溶劑。In the second concentrating
[其他實施形態]
上述實施形態中,濃縮裝置,利用第一濃縮裝置200與第二濃縮裝置300此兩台。濃縮裝置,亦可因應風量,應用兩台第一濃縮裝置200或兩台第二濃縮裝置300。此外,亦可因應去除效率,應用三台以上之濃縮裝置。[Other embodiments]
In the above embodiment, two concentrating devices, the first concentrating
作為排放氣體G1所含有的有機溶劑,列舉可藉由1℃~50℃之冷卻而液化回收的有機溶劑。作為有機溶劑,例如為N-甲基吡咯烷酮、N-乙基吡咯烷酮、N,N-二甲基甲醯胺、N,N-二甲基乙醯胺、或正癸烷。其等僅為例示,並未限定於其等。所含有的有機溶劑,可為1種亦可為複數種。Examples of the organic solvent contained in the exhaust gas G1 include organic solvents that can be liquefied and recovered by cooling at 1°C to 50°C. The organic solvent is, for example, N-methylpyrrolidone, N-ethylpyrrolidone, N,N-dimethylformamide, N,N-dimethylacetamide, or n-decane. These etc. are only examples, and are not limited to them. The organic solvent contained may be one type or plural types.
[實施形態1C]
圖6係概略顯示實施形態1C的有機溶劑回收系統1C之構成的圖。有機溶劑回收系統1C,係由冷卻冷凝裝置100、第一濃縮裝置200、第二濃縮裝置300、及各種流通路徑構成。[Embodiment 1C]
Fig. 6 is a diagram schematically showing the configuration of the organic solvent recovery system 1C of the embodiment 1C. The organic solvent recovery system 1C is composed of a cooling and condensing
冷卻冷凝裝置100,具備冷卻部110及分離部120。含有有機溶劑之排放氣體G1,從生產設備130排出。排放氣體G1,藉由通過冷卻部110而冷卻。排放氣體G1,伴隨通過冷卻部110而使有機溶劑液化冷凝。The cooling and condensing
通過冷卻部110之排放氣體G2,藉由通過分離部120,而分離為經液化冷凝之冷卻冷凝液L1與有機溶劑濃度降低之冷卻處理氣體G3。冷卻處理氣體G3,通過腔室123,作為冷卻處理氣體G4從冷卻冷凝裝置100往第一濃縮裝置200排出。The exhaust gas G2 passing through the cooling
冷卻部110之冷卻手段及構成,並無特別限定。在實施形態1,使用藉由冷卻水、冷水、鹹水等冷媒與排放氣體之間接熱交換而進行冷卻的第一熱交換器111。第一熱交換器111,位於使排放氣體G1往水平方向流通之位置。The cooling means and structure of the
冷卻部110,於第一熱交換器111之前,設置藉由後述冷卻處理氣體G6與排放氣體G1之熱交換而使排放氣體G1冷卻的第二熱交換器112。第二熱交換器112,可減少第一熱交換器111所需之傳熱面積與冷媒量。排放氣體G1及冷卻處理氣體G6的一部分,通過第五流通路徑F5往生產設備130返回。第一熱交換器111及第二熱交換器112中的冷卻溫度等之條件,依作為回收對象的有機溶劑適當決定即可。The
分離部120之分離手段及構成並無特別限定。在實施形態1C,使用除霧器、濾網、及篩孔等接觸液滴而加以捕捉的網眼狀構造體121。網眼狀構造體121捕捉到之冷卻冷凝液L1,因重力而往配置於網眼狀構造體121的下部之貯存槽125集液,作為回收液L3回收。The separation means and structure of the
腔室123,係具有一定容量之空間的構造體。使於腔室123內貯存一定時間之冷卻處理氣體G3,作為冷卻處理氣體G4在第一流通路徑F1流通,往第一濃縮裝置200供給。腔室123具備分隔部128,分隔部128可與從網眼狀構造體121排出之冷卻處理氣體G3的排氣方向對向而進行第一流通路徑F1的吸入。The
第一流通路徑F1,係將冷卻處理氣體G4從腔室123往第一濃縮裝置200導入之部位。第一流通路徑F1的往腔室123之連接口,宜為腔室123之頂棚部127。藉此,抑制分離部120未捕捉到的微少液滴之往第一濃縮裝置200的侵入,可防止後述因第一濃縮裝置200之吸附單元210的潤濕所造成之性能降低/強度降低等。更佳態樣中,宜以與冷卻處理氣體G3的流通方向對向之方式,將冷卻處理氣體G4取出。藉此,可進一步防止液滴的侵入。除此之外,亦可於冷卻處理氣體G4之取出口,設置與上述網眼狀構造體121類似的防液滴侵入構件,亦可設置用於使液滴氣化的加熱器。The first flow path F1 is a part where the cooling processing gas G4 is introduced from the
第一濃縮裝置200具備包含吸附材之吸附轉筒212,藉由與氣體接觸而吸附其含有的有機溶劑,藉由與加熱氣體接觸而使吸附的有機溶劑脫附。吸附轉筒212,係由以複數個分隔部分隔出之複數個吸附單元210構成。吸附轉筒212,藉由複數個吸附單元210而使全體成為中空圓柱狀的形狀。吸附轉筒212,設置於處理室內,設置為流體可沿徑方向流動。吸附轉筒212,設置為受到馬達之旋轉驅動力而可繞筒軸旋轉。The first concentrating
在第一濃縮裝置200,使吸附單元210的一部分構成吸附部,吸附從吸附單元210的外側向內側供給之冷卻處理氣體G4所含有的有機溶劑;且使吸附單元210的其餘部分構成脫附部,藉由從吸附單元210的內側向外側供給加熱空氣而使吸附於吸附單元210的有機溶劑從吸附單元210脫附。In the first concentrating
潔淨化時,將供給至處理室內之冷卻處理氣體G4,從吸附轉筒212的外周面往吸附部導入。導入至吸附部之冷卻處理氣體G4,在沿著徑方向從外周面向內周面通過吸附轉筒212時,將有機溶劑吸附至位於吸附部之複數個吸附單元210,藉以潔淨化。At the time of cleaning, the cooled processing gas G4 supplied into the processing chamber is introduced from the outer peripheral surface of the
將經潔淨化的作為被處理流體之冷卻處理氣體G5、G6,作為潔淨氣體,從吸附單元210之上部排出。使排出之潔淨氣體的一部分,作為冷卻處理氣體G5在第二流通路徑F2流通,往第二濃縮裝置300供給。使排出之潔淨氣體的一部分,作為冷卻處理氣體G6在第四流通路徑F4流通,往第二熱交換器112返回。The cleaned cooling processing gases G5 and G6 serving as the fluid to be processed are discharged from the upper portion of the
內周側流路形成構件211及外周側流路形成構件213,以將圓周方向中之吸附轉筒212的一部分夾入之方式,於吸附轉筒212的內周側及外周側中彼此相對向地配置。由內周側流路形成構件211及外周側流路形成構件213所包夾之吸附轉筒212的區域,為脫附部。The inner circumference side flow
為了施行有機溶劑之脫附,而從內周側流路形成構件211,對脫附部導入藉由再生加熱器250加熱之冷卻處理氣體G5的一部分即高溫氣體G7。導入至脫附部之高溫氣體G7,在通過吸附轉筒212時,從位於脫附部之複數個吸附單元210,藉由熱使吸附於其等的有機溶劑脫附。含有有機溶劑之脫附氣體G8,作為濃縮氣體,從脫附部通過外周側流路形成構件213,往處理室外排出,返回至第三流通路徑F3。將脫附氣體G8中所含有的有機溶劑之一部分液化冷凝,作為脫附冷凝液L2往貯存槽125集液。In order to perform the desorption of the organic solvent, the high-temperature gas G7, which is a part of the cooling process gas G5 heated by the
第三流通路徑F3,係將脫附氣體G8送回至冷卻冷凝裝置100之排放氣體G1的導入部之部位。第三流通路徑F3,宜以將脫附部配置於較脫附氣體G8與往冷卻冷凝裝置100供給之排放氣體G1的合流位置更為上部之方式連接。藉由此一配置,由第一濃縮裝置200之脫附氣體G8產生的脫附冷凝液L2,變得容易往冷卻冷凝裝置100移動。第三流通路徑F3,宜構成為使冷卻冷凝裝置100之排放氣體G1的導入部及貯存槽125此兩處流通。藉由此一構成,由脫附氣體G8產生的脫附冷凝液L2變得容易直接往貯存槽125回收。The third flow path F3 is to return the desorbed gas G8 to the inlet of the exhaust gas G1 of the cooling and condensing
於第一濃縮裝置200中,對位於吸附部之吸附單元210施行被處理物質的吸附處理,對在吸附處理後位於脫附部之吸附單元210施行被處理物質的脫附處理。藉由使吸附轉筒212繞筒軸旋轉,而使吸附單元210將脫附部與吸附部交互地移動,連續地實施被處理物質的吸附處理與脫附處理。In the first concentrating
作為構成吸附單元210之吸附元件的材料,可利用活性氧化鋁、矽膠、活性碳材料、沸石等。吸附單元210中之吸附元件的形狀並無特別限定,例如,可為將含有活性碳材料或沸石之薄片形成為蜂巢狀者,亦可為將活性碳纖維不織布疊層者。As the material constituting the adsorption element of the
第二濃縮裝置300具備包含吸附材之吸附元件310,藉由與氣體接觸而吸附其含有的有機溶劑,藉由與加熱氣體接觸而使吸附的有機溶劑脫附。吸附元件310,包含脫附部(脫附區)311與吸附部(吸附區)312。吸附部312,藉由將冷卻處理氣體G5導入,而使冷卻處理氣體G5與吸附材接觸,藉以將冷卻處理氣體G5所含有的有機溶劑吸附於吸附材,使冷卻處理氣體G5潔淨化,作為潔淨氣體G9排出。The second concentrating
脫附部311,藉由將較冷卻處理氣體G5更高溫之氣體G10導入至吸附材,而使有機溶劑從吸附材脫附,藉此作為含有有機溶劑之脫附氣體G11排出。脫附氣體G11,通過第六流通路徑F6,返回至第一流通路徑F1。The
有機溶劑回收系統1C,由於使脫附氣體G11返回至第一流通路徑F1,故於冷卻冷凝裝置100中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統1C,可對於冷卻冷凝裝置100的小型化、節能化有所助益。有機溶劑回收系統1C,由於脫附氣體G11為高溫,故可抑制冷卻處理氣體G4中所包含的NMP(N-甲基吡咯烷酮)、水分等之冷凝。Since the organic solvent recovery system 1C returns the desorbed gas G11 to the first flow path F1, the cooling and condensing
作為吸附元件310所包含之吸附材,廣泛利用活性氧化鋁、矽膠、活性碳材料或沸石,其中特別適合利用活性碳與疏水性沸石。As the adsorption material contained in the
如圖6所示,第二濃縮裝置300,具備旋轉軸、及繞旋轉軸而設置之吸附元件310。第二濃縮裝置300,為下述構成:藉由使吸附元件310繞旋轉軸旋轉,而於吸附部312中,使吸附有從第二流通路徑F2導入之冷卻處理氣體G5中的有機溶劑之吸附材連續地往脫附部311移動。As shown in FIG. 6, the second concentrating
第二濃縮裝置300,亦可具備脫附部311之脫附處理結束的部分在往吸附部312移動之前往其移動的清潔部(吹掃部)。亦可為將潔淨氣體G9的一部分導入至吹掃部,將從吹掃部排出之吹掃部出口氣體導入至吸附部312之構成。此係因藉由以潔淨氣體G9清潔結束脫附的吸附材,而防止殘留於吸附材之脫附氣體G11往潔淨氣體G9的混入,可將吸附材冷卻之緣故。The second concentrating
使用於脫附之高溫氣體G10,宜為利用再生加熱器350等加熱手段使潔淨氣體G9的一部分成為高溫狀態者。藉由使其成為高溫狀態,於吸附部312中,可抑制有機溶劑含有氣體的處理風量之增加。The high-temperature gas G10 used for desorption is preferably one that uses heating means such as the
[實施形態2C]
圖7係概略顯示實施形態2C的有機溶劑回收系統2C之構成的圖。有機溶劑回收系統2C,係由冷卻冷凝裝置100、第一濃縮裝置200、第二濃縮裝置300、及各種流通路徑構成。有機溶劑回收系統2C,除了下述點以外之構成,與實施形態1C的有機溶劑回收系統1C相同:使第二濃縮裝置300之脫附氣體G11通過第六流通路徑F6,返回至再生加熱器250。[Embodiment 2C]
Fig. 7 is a diagram schematically showing the configuration of an organic solvent recovery system 2C of Embodiment 2C. The organic solvent recovery system 2C is composed of a cooling and condensing
有機溶劑回收系統2C,由於使脫附氣體G11返回至再生加熱器250,故於冷卻冷凝裝置100及第一濃縮裝置200中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統2C,可對於冷卻冷凝裝置100及第一濃縮裝置200的小型化、節能化有所助益。有機溶劑回收系統2C,由於脫附氣體G11為高溫,故可對於再生加熱器250的節能化有所助益。Since the organic solvent recovery system 2C returns the desorbed gas G11 to the
[實施形態3C]
圖8係概略顯示實施形態3C的有機溶劑回收系統3C之構成的圖。有機溶劑回收系統3C,係由冷卻冷凝裝置100、第一濃縮裝置200、第二濃縮裝置300、及各種流通路徑構成。有機溶劑回收系統3C,使第二濃縮裝置300之脫附氣體G11通過第六流通路徑F6,返回至第四流通路徑F4。有機溶劑回收系統3C,除了下述點以外之構成,與實施形態1C的有機溶劑回收系統1C相同:使第二濃縮裝置300之脫附氣體G11通過第六流通路徑F6,返回至第四流通路徑F4。[
使在第六流通路徑F6流通之脫附氣體G11,與從第二濃縮裝置300排出之冷卻處理氣體G6一同在第四流通路徑F4流通,往第二熱交換器112返回。有機溶劑回收系統3C,於冷卻冷凝裝置100及第一濃縮裝置200中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統3C,可對於冷卻冷凝裝置100及第一濃縮裝置200的小型化、節能化有所助益。有機溶劑回收系統3C,由於脫附氣體G11為高溫,故可使往第二熱交換器112流通之流體的溫度上升,可對於用於將排放氣體G1冷卻之第二熱交換器112的小型化、節能化有所助益。The desorbed gas G11 circulating in the sixth circulation path F6 is allowed to circulate in the fourth circulation path F4 together with the cooled processing gas G6 discharged from the second concentrating
[實施形態4C]
圖9係概略顯示實施形態4C的有機溶劑回收系統4C之構成的圖。有機溶劑回收系統4C,係由冷卻冷凝裝置100、第一濃縮裝置200、第二濃縮裝置300、及各種流通路徑構成。有機溶劑回收系統4C,使第二濃縮裝置300之脫附氣體G11通過第六流通路徑F6,返回至第五流通路徑F5。有機溶劑回收系統4C,除了下述點以外之構成,與實施形態1C的有機溶劑回收系統1C相同:使第二濃縮裝置300之脫附氣體G11通過第六流通路徑F6,返回至第五流通路徑F5。[
使在第六流通路徑F6流通之脫附氣體G11,與從第二熱交換器112排出之排放氣體G1及冷卻處理氣體G6的一部分一同在第五流通路徑F5流通,往生產設備130返回。有機溶劑回收系統4C,於冷卻冷凝裝置100及第一濃縮裝置200中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統4C,可對於冷卻冷凝裝置100及第一濃縮裝置200的小型化、節能化有所助益。有機溶劑回收系統4C,由於脫附氣體G11為高溫,故可提高從生產設備130再度排出之排放氣體G1的溫度。因此,有機溶劑回收系統4C,可使往第二熱交換器112流通之流體的溫度上升,可對於用於將排放氣體G1冷卻之第二熱交換器112的小型化、節能化有所助益。The desorbed gas G11 circulating in the sixth circulation path F6 is allowed to circulate in the fifth circulation path F5 together with part of the exhaust gas G1 discharged from the
[作用/效果]
本實施形態之有機溶劑回收系統1C,具備:冷卻冷凝裝置100,藉由將含有有機溶劑之排放氣體G1冷卻,而將有機溶劑液化冷凝,作為有機溶劑的濃度已降低之冷卻處理氣體G4排出;第一流通路徑F1,使冷卻處理氣體G4流通;第一濃縮裝置200,將從第一流通路徑F1導入之冷卻處理氣體G4所含有的有機溶劑藉由吸附單元210吸附,作為有機溶劑的濃度進一步降低之冷卻處理氣體G5排出,導入高溫氣體G7而從吸附單元210使有機溶劑脫附,作為脫附氣體G8排出;第二流通路徑F2,使冷卻處理氣體G5的一部分流通;以及第二濃縮裝置300,將從第二流通路徑F2導入之冷卻處理氣體G5所含有的有機溶劑藉由吸附元件310吸附,作為有機溶劑的濃度進一步降低之潔淨氣體G9排出,導入高溫氣體G10而從吸附元件310使有機溶劑脫附,作為脫附氣體G11排出。[Effect]
The organic solvent recovery system 1C of the present embodiment includes: a cooling and condensing
使脫附氣體G8,返回至冷卻冷凝裝置100,且使脫附氣體G11,返回至第一流通路徑F1。有機溶劑回收系統1C,由於使脫附氣體G11返回至第一流通路徑F1,故於冷卻冷凝裝置100中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統1C,可對於冷卻冷凝裝置100的小型化、節能化有所助益。有機溶劑回收系統1C,由於脫附氣體G11為高溫,故可抑制冷卻處理氣體G4中所包含的NMP(N-甲基吡咯烷酮)、水分等之冷凝。The desorbed gas G8 is returned to the cooling and condensing
使脫附氣體G8,返回至冷卻冷凝裝置100,且使脫附氣體G11,返回至再生加熱器250。有機溶劑回收系統2C,由於使脫附氣體G11返回至再生加熱器250,故於冷卻冷凝裝置100及第一濃縮裝置200中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統2C可對於冷卻冷凝裝置100及第一濃縮裝置200的小型化、節能化有所助益。有機溶劑回收系統2C,由於脫附氣體G11為高溫,故可對於再生加熱器250的節能化有所助益。The desorbed gas G8 is returned to the cooling and condensing
使脫附氣體G8,返回至冷卻冷凝裝置100,且使脫附氣體G11,返回至第四流通路徑F4。脫附氣體G11,與冷卻處理氣體G6一同在第四流通路徑F4流通,往第二熱交換器112返回。有機溶劑回收系統3C,於冷卻冷凝裝置100及第一濃縮裝置200中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統3C,可對於冷卻冷凝裝置100及第一濃縮裝置200的小型化、節能化有所助益。有機溶劑回收系統3C,由於脫附氣體G11為高溫,故可使往第二熱交換器112流通之流體的溫度上升,可對於用於將排放氣體G1冷卻之第二熱交換器112的小型化、節能化有所助益。The desorbed gas G8 is returned to the cooling and condensing
使脫附氣體G8,返回至冷卻冷凝裝置100,且使脫附氣體G11,返回至第五流通路徑F5。脫附氣體G11,與從第二熱交換器112排出之排放氣體G1及冷卻處理氣體G6的一部分一同在第五流通路徑F5流通,往生產設備130返回。有機溶劑回收系統4C,於冷卻冷凝裝置100及第一濃縮裝置200中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統4C可對於冷卻冷凝裝置100及第一濃縮裝置200的小型化、節能化有所助益。有機溶劑回收系統4C,由於脫附氣體G11為高溫,故可提高從生產設備130再度排出之排放氣體G1的溫度。因此,有機溶劑回收系統4C,可使往第二熱交換器112流通之流體的溫度上升,可對於用於將排放氣體G1冷卻之第二熱交換器112的小型化、節能化有所助益。The desorbed gas G8 is returned to the cooling and condensing
將本實施形態之第一濃縮裝置200,於使吸附單元210繞筒軸旋轉之中空圓柱狀的轉筒之繞筒軸的圓周方向配置複數個。藉此,可高效率地回收有機溶劑。The first concentrating
本實施形態之第二濃縮裝置300,將吸附元件310配置於繞筒軸旋轉之圓盤狀的吸附轉筒。藉此,可高效率地回收有機溶劑。In the second concentrating
[其他實施形態]
上述實施形態中,濃縮裝置,利用第一濃縮裝置200與第二濃縮裝置300此兩台。濃縮裝置,亦可因應風量,應用兩台第一濃縮裝置200或兩台第二濃縮裝置300。此外,亦可因應去除效率,應用三台以上之濃縮裝置。[Other embodiments]
In the above embodiment, two concentrating devices, the first concentrating
作為排放氣體G1所含有的有機溶劑,列舉可藉由1℃~50℃之冷卻而液化回收的有機溶劑。作為有機溶劑,例如為N-甲基吡咯烷酮、N-乙基吡咯烷酮、N,N-二甲基甲醯胺、N,N-二甲基乙醯胺、或正癸烷。其等僅為例示,並未限定於其等。所含有的有機溶劑,可為1種亦可為複數種。Examples of the organic solvent contained in the exhaust gas G1 include organic solvents that can be liquefied and recovered by cooling at 1°C to 50°C. The organic solvent is, for example, N-methylpyrrolidone, N-ethylpyrrolidone, N,N-dimethylformamide, N,N-dimethylacetamide, or n-decane. These etc. are only examples, and are not limited to them. The organic solvent contained may be one type or plural types.
[實施形態1D]
圖10係概略顯示實施形態1D的有機溶劑回收系統1D之構成的圖。有機溶劑回收系統1D,係由冷卻冷凝裝置100、第一濃縮裝置200、第二濃縮裝置300、及各種流通路徑構成。[
冷卻冷凝裝置100,具備冷卻部110及分離部120。含有有機溶劑之排放氣體G1,從生產設備130排出。排放氣體G1,藉由通過冷卻部110而冷卻。排放氣體G1,伴隨通過冷卻部110而使有機溶劑液化冷凝。The cooling and condensing
通過冷卻部110之排放氣體G2,藉由通過分離部120,而分離為經液化冷凝之冷卻冷凝液L1與有機溶劑濃度降低之冷卻處理氣體G3。冷卻處理氣體G3,通過腔室123,使一部分作為冷卻處理氣體G4從冷卻冷凝裝置100往第一濃縮裝置200排出,其餘部分作為冷卻處理氣體G6從冷卻冷凝裝置100往後述第二熱交換器112返回。The exhaust gas G2 passing through the cooling
冷卻部110之冷卻手段及構成,並無特別限定。在實施形態1D,使用藉由冷卻水、冷水、鹹水等冷媒與排放氣體之間接熱交換而進行冷卻的第一熱交換器111。第一熱交換器111,位於使排放氣體G1往水平方向流通之位置。The cooling means and structure of the
冷卻部110,於第一熱交換器111之前,設置藉由冷卻處理氣體G6與排放氣體G1之熱交換而使排放氣體G1冷卻的第二熱交換器112。第二熱交換器112,可減少第一熱交換器111所需之傳熱面積與冷媒量。排放氣體G1及冷卻處理氣體G6的一部分,通過第五流通路徑F5往生產設備130返回。第一熱交換器111及第二熱交換器112中的冷卻溫度等之條件,依作為回收對象的有機溶劑適當決定即可。The cooling
分離部120之分離手段及構成並無特別限定。在實施形態1D,使用除霧器、濾網、及篩孔等接觸液滴而加以捕捉的網眼狀構造體121。網眼狀構造體121捕捉到之冷卻冷凝液L1,因重力而往配置於網眼狀構造體121的下部之貯存槽125集液,作為回收液L3回收。The separation means and structure of the
腔室123,係具有一定容量之空間的構造體。於腔室123內貯存一定時間之冷卻處理氣體G3,作為冷卻處理氣體G4使一部分在第一流通路徑F1流通,往第一濃縮裝置200供給。冷卻處理氣體G3,作為冷卻處理氣體G6使其餘部分在第四流通路徑F4流通,往第二熱交換器112返回。腔室123具備分隔部128,分隔部128可與從網眼狀構造體121排出之冷卻處理氣體G3的排氣方向對向而進行第一流通路徑F1的吸入。The
第一流通路徑F1,係將冷卻處理氣體G4從腔室123往第一濃縮裝置200導入之部位。第一流通路徑F1的往腔室123之連接口,宜為腔室123之頂棚部127。藉此,抑制分離部120未捕捉到的微少液滴之往第一濃縮裝置200的侵入,可防止後述第一濃縮裝置200之因吸附單元210的潤濕所造成之性能降低/強度降低等。更佳態樣中,宜以與冷卻處理氣體G3的流通方向對向之方式,將冷卻處理氣體G4取出。藉此,可進一步防止液滴的侵入。除此之外,亦可於冷卻處理氣體G4之取出口,設置與上述網眼狀構造體121類似的防液滴侵入構件,亦可設置用於使液滴氣化的加熱器。The first flow path F1 is a part where the cooling processing gas G4 is introduced from the
第一濃縮裝置200具備包含吸附材之吸附轉筒212,藉由與氣體接觸而吸附其含有的有機溶劑,藉由與加熱氣體接觸而使吸附的有機溶劑脫附。吸附轉筒212,係由以複數個分隔部分隔出之複數個吸附單元210構成。吸附轉筒212,藉由複數個吸附單元210而使全體成為中空圓柱狀的形狀。吸附轉筒212,設置於處理室內,設置為流體可沿徑方向流動。吸附轉筒212,設置為受到馬達之旋轉驅動力而可繞筒軸旋轉。The first concentrating
在第一濃縮裝置200,使吸附單元210的一部分構成吸附部,吸附從吸附單元210的外側向內側供給之冷卻處理氣體G4所含有的有機溶劑;且使吸附單元210的其餘部分構成脫附部,藉由從吸附單元210的內側向外側供給加熱空氣而使吸附於吸附單元210的有機溶劑從吸附單元210脫附。In the first concentrating
潔淨化時,將供給至處理室內之冷卻處理氣體G4,從吸附轉筒212的外周面往吸附部導入。導入至吸附部之冷卻處理氣體G4,在沿著徑方向從外周面向內周面通過吸附轉筒212時,將有機溶劑吸附至位於吸附部之複數個吸附單元210,藉以潔淨化。At the time of cleaning, the cooled processing gas G4 supplied into the processing chamber is introduced from the outer peripheral surface of the
將經潔淨化的作為被處理流體之冷卻處理氣體G5,作為潔淨氣體,從吸附單元210之上部排出。使排出之潔淨氣體,作為冷卻處理氣體G5在第二流通路徑F2流通,往第二濃縮裝置300供給。The cleaned cooling processing gas G5 as the fluid to be processed is discharged from the upper part of the
內周側流路形成構件211及外周側流路形成構件213,以將圓周方向中之吸附轉筒212的一部分夾入之方式,於吸附轉筒212的內周側及外周側中彼此相對向地配置。由內周側流路形成構件211及外周側流路形成構件213所包夾之吸附轉筒212的區域,為脫附部。The inner circumference side flow
為了施行有機溶劑之脫附,而從內周側流路形成構件211,對脫附部導入藉由再生加熱器250加熱之冷卻處理氣體G5的一部分即高溫氣體G7。導入至脫附部之高溫氣體G7,在通過吸附轉筒212時,從位於脫附部之複數個吸附單元210,藉由熱使吸附於其等的有機溶劑脫附。含有有機溶劑之脫附氣體G8,作為濃縮氣體,從脫附部通過外周側流路形成構件213,往處理室外排出,返回至第三流通路徑F3。將脫附氣體G8中所含有的有機溶劑之一部分液化冷凝,作為脫附冷凝液L2往貯存槽125集液。In order to perform the desorption of the organic solvent, the high-temperature gas G7, which is a part of the cooling process gas G5 heated by the
第三流通路徑F3,係將脫附氣體G8送回至冷卻冷凝裝置100之排放氣體G1的導入部之部位。第三流通路徑F3,宜以將脫附部配置於較脫附氣體G8與往冷卻冷凝裝置100供給之排放氣體G1的合流位置更為上部之方式連接。藉由此一配置,由第一濃縮裝置200之脫附氣體G8產生的脫附冷凝液L2,變得容易往冷卻冷凝裝置100移動。第三流通路徑F3,宜構成為使冷卻冷凝裝置100之排放氣體G1的導入部及貯存槽125此兩處流通。藉由此一構成,由脫附氣體G8產生的脫附冷凝液L2變得容易直接往貯存槽125回收。The third flow path F3 is to return the desorbed gas G8 to the inlet of the exhaust gas G1 of the cooling and condensing
於第一濃縮裝置200中,對位於吸附部之吸附單元210施行被處理物質的吸附處理,對在吸附處理後位於脫附部之吸附單元210施行被處理物質的脫附處理。藉由使吸附轉筒212繞筒軸旋轉,而使吸附單元210將脫附部與吸附部交互地移動,連續地實施被處理物質的吸附處理與脫附處理。In the first concentrating
作為構成吸附單元210之吸附元件的材料,可利用活性氧化鋁、矽膠、活性碳材料、沸石等。吸附單元210中之吸附元件的形狀並無特別限定,例如,可為將含有活性碳材料或沸石之薄片形成為蜂巢狀者,亦可為將活性碳纖維不織布疊層者。As the material constituting the adsorption element of the
第二濃縮裝置300具備包含吸附材之吸附元件310,藉由與氣體接觸而吸附其含有的有機溶劑,藉由與加熱氣體接觸而使吸附的有機溶劑脫附。吸附元件310,包含脫附部(脫附區)311與吸附部(吸附區)312。吸附部312,藉由將冷卻處理氣體G5導入,而使冷卻處理氣體G5與吸附材接觸,藉以將冷卻處理氣體G5所含有的有機溶劑吸附於吸附材,使冷卻處理氣體G5潔淨化,作為潔淨氣體G9排出。The second concentrating
脫附部311,藉由將較冷卻處理氣體G5更高溫之氣體G10導入至吸附材,而使有機溶劑從吸附材脫附,藉此作為含有有機溶劑之脫附氣體G11排出。脫附氣體G11,通過第六流通路徑F6,返回至第一流通路徑F1。The
有機溶劑回收系統1D,由於使脫附氣體G11返回至第一流通路徑F1,故於冷卻冷凝裝置100中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統1D,可對於冷卻冷凝裝置100的小型化、節能化有所助益。有機溶劑回收系統1D,由於脫附氣體G11為高溫,故可抑制冷卻處理氣體G4中所包含的NMP(N-甲基吡咯烷酮)、水分等之冷凝。Since the organic
作為吸附元件310所包含之吸附材,廣泛利用活性氧化鋁、矽膠、活性碳材料或沸石,其中特別適合利用活性碳與疏水性沸石。As the adsorption material contained in the
如圖10所示,第二濃縮裝置300,具備旋轉軸、及繞旋轉軸而設置之吸附元件310。第二濃縮裝置300,為下述構成:藉由使吸附元件310繞旋轉軸旋轉,而於吸附部312中,使吸附有從第二流通路徑F2導入之冷卻處理氣體G5中的有機溶劑之吸附材連續地往脫附部311移動。As shown in FIG. 10, the second concentrating
第二濃縮裝置300,亦可具備脫附部311之脫附處理結束的部分在往吸附部312移動之前往其移動的清潔部(吹掃部)。亦可為將潔淨氣體G9的一部分導入至吹掃部,將從吹掃部排出之吹掃部出口氣體導入至吸附部312之構成。此係因藉由以潔淨氣體G9清潔結束脫附的吸附材,而防止殘留於吸附材之脫附氣體G11往潔淨氣體G9的混入,可將吸附材冷卻之緣故。The second concentrating
使用於脫附之高溫氣體G10,宜為利用再生加熱器350等加熱手段使潔淨氣體G9的一部分成為高溫狀態者。藉由使其成為高溫狀態,於吸附部312中,可抑制有機溶劑含有氣體的處理風量之增加。The high-temperature gas G10 used for desorption is preferably one that uses heating means such as the
[實施形態2D]
圖11係概略顯示實施形態2D的有機溶劑回收系統2D之構成的圖。有機溶劑回收系統2D,係由冷卻冷凝裝置100、第一濃縮裝置200、第二濃縮裝置300、及各種流通路徑構成。有機溶劑回收系統2D,除了下述點以外之構成,與實施形態1D的有機溶劑回收系統1D相同:使第二濃縮裝置300之脫附氣體G11通過第六流通路徑F6,返回至再生加熱器250。[
有機溶劑回收系統2D,由於使脫附氣體G11返回至再生加熱器250,故於冷卻冷凝裝置100及第一濃縮裝置200中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統2D可對於冷卻冷凝裝置100及第一濃縮裝置200的小型化、節能化有所助益。有機溶劑回收系統2D,由於脫附氣體G11為高溫,故可對於再生加熱器250的節能化有所助益。Since the organic
[實施形態3D]
圖12係概略顯示實施形態3D的有機溶劑回收系統3D之構成的圖。有機溶劑回收系統3D,係由冷卻冷凝裝置100、第一濃縮裝置200、第二濃縮裝置300、及各種流通路徑構成。有機溶劑回收系統3D,使第二濃縮裝置300之脫附氣體G11通過第六流通路徑F6,返回至第四流通路徑F4。有機溶劑回收系統3D,除了下述點以外之構成,與實施形態1D的有機溶劑回收系統1D相同:使第二濃縮裝置300之脫附氣體G11通過第六流通路徑F6,返回至第四流通路徑F4。[
在第六流通路徑F6流通之脫附氣體G11,與從冷卻冷凝裝置100排出之冷卻處理氣體G6一同在第四流通路徑F4流通,往第二熱交換器112返回。有機溶劑回收系統3D,於冷卻冷凝裝置100及第一濃縮裝置200中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統3D,可對於冷卻冷凝裝置100及第一濃縮裝置200的小型化、節能化有所助益。有機溶劑回收系統3D,由於脫附氣體G11為高溫,故可使往第二熱交換器112流通之流體的溫度上升,可對於用於將排放氣體G1冷卻之第二熱交換器112的小型化、節能化有所助益。The desorbed gas G11 that flows through the sixth flow path F6 flows through the fourth flow path F4 together with the cooled processing gas G6 discharged from the cooling and condensing
[實施形態4D]
圖13係概略顯示實施形態4D的有機溶劑回收系統4D之構成的圖。有機溶劑回收系統4D,係由冷卻冷凝裝置100、第一濃縮裝置200、第二濃縮裝置300、及各種流通路徑構成。有機溶劑回收系統4D,使第二濃縮裝置300之脫附氣體G11通過第六流通路徑F6,返回至第五流通路徑F5。有機溶劑回收系統4D,除了下述點以外之構成,與實施形態1D的有機溶劑回收系統1D相同:使第二濃縮裝置300之脫附氣體G11通過第六流通路徑F6,返回至第五流通路徑F5。[
在第六流通路徑F6流通之脫附氣體G11,與從第二熱交換器112排出之排放氣體G1及冷卻處理氣體G6的一部分一同在第五流通路徑F5流通,往生產設備130返回。有機溶劑回收系統4D,於冷卻冷凝裝置100及第一濃縮裝置200中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統4D可對於冷卻冷凝裝置100及第一濃縮裝置200的小型化、節能化有所助益。有機溶劑回收系統4D,由於脫附氣體G11為高溫,故可提高從生產設備130再度排出之排放氣體G1的溫度。因此,有機溶劑回收系統4D,可使往第二熱交換器112流通之流體的溫度上升,可對於用於將排放氣體G1冷卻之第二熱交換器112的小型化、節能化有所助益。The desorbed gas G11 flowing through the sixth flow path F6 circulates through the fifth flow path F5 together with part of the exhaust gas G1 and the cooling process gas G6 discharged from the
[作用/效果]
本實施形態之有機溶劑回收系統1D,具備:冷卻冷凝裝置100,藉由將含有有機溶劑之排放氣體G1冷卻,而將有機溶劑液化冷凝,作為有機溶劑的濃度已降低之冷卻處理氣體G4排出;第一流通路徑F1,使冷卻處理氣體G4的一部分流通;第一濃縮裝置200,將從第一流通路徑F1導入之冷卻處理氣體G4所包含的有機溶劑藉由吸附單元210吸附,作為有機溶劑的濃度進一步降低之冷卻處理氣體G5排出,導入高溫氣體G7而從吸附單元210使有機溶劑脫附,作為脫附氣體G8排出;第二流通路徑F2,使冷卻處理氣體G5流通;以及第二濃縮裝置300,將從第二流通路徑F2導入之冷卻處理氣體G5所含有的有機溶劑藉由吸附元件310吸附,作為有機溶劑的濃度進一步降低之潔淨氣體G9排出,導入高溫氣體G10而從吸附元件310使有機溶劑脫附,作為脫附氣體G11排出。[Effect]
The organic
冷卻冷凝裝置100,包含藉由與冷媒之熱交換而施行排放氣體G1的冷卻之第二熱交換器112。有機溶劑回收系統1D更包含第四流通路徑F4,第四流通路徑F4使作為冷卻處理氣體G4的一部分以外亦即冷卻處理氣體的其餘部分之冷卻處理氣體G6,返回至第二熱交換器112。使脫附氣體G8,返回至冷卻冷凝裝置100,且使脫附氣體G11,返回至第一流通路徑F1。有機溶劑回收系統1D,由於脫附氣體G11返回至第一流通路徑F1,故於冷卻冷凝裝置100中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統1D,可對於冷卻冷凝裝置100的小型化、節能化有所助益。有機溶劑回收系統1D,由於脫附氣體G11為高溫,故可抑制冷卻處理氣體G4中所包含的NMP(N-甲基吡咯烷酮)、水分等之冷凝。The cooling and condensing
使脫附氣體G8,返回至冷卻冷凝裝置100,且使脫附氣體G11,返回至再生加熱器250。有機溶劑回收系統2D,由於使脫附氣體G11返回至再生加熱器250,故於冷卻冷凝裝置100及第一濃縮裝置200中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統2D,可對於冷卻冷凝裝置100及第一濃縮裝置200的小型化、節能化有所助益。有機溶劑回收系統2D,由於脫附氣體G11為高溫,故可對於再生加熱器250的節能化有所助益。The desorbed gas G8 is returned to the cooling and condensing
使脫附氣體G8,返回至冷卻冷凝裝置100,且使脫附氣體G11,返回至第四流通路徑F4。脫附氣體G11,與冷卻處理氣體G6一同在第四流通路徑F4流通,往第二熱交換器112返回。有機溶劑回收系統3D,於冷卻冷凝裝置100及第一濃縮裝置200中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統3D,可對於冷卻冷凝裝置100及第一濃縮裝置200的小型化、節能化有所助益。有機溶劑回收系統3D,由於脫附氣體G11為高溫,故可使往第二熱交換器112流通之流體的溫度上升,可對於用於將排放氣體G1冷卻之第二熱交換器112的小型化、節能化有所助益。The desorbed gas G8 is returned to the cooling and condensing
使脫附氣體G8,返回至冷卻冷凝裝置100,且使脫附氣體G11,返回至第五流通路徑F5。脫附氣體G11,與從第二熱交換器112排出之排放氣體G1及冷卻處理氣體G6的一部分一同在第五流通路徑F5流通,往生產設備130返回。有機溶劑回收系統4D,於冷卻冷凝裝置100及第一濃縮裝置200中無須處理脫附氣體G11的風量分。因此,有機溶劑回收系統4D可對於冷卻冷凝裝置100及第一濃縮裝置200的小型化、節能化有所助益。有機溶劑回收系統4D,由於脫附氣體G11為高溫,故可提高從生產設備130再度排出之排放氣體G1的溫度。因此,有機溶劑回收系統4D,可使往第二熱交換器112流通之流體的溫度上升,可對於用於將排放氣體G1冷卻之第二熱交換器112的小型化、節能化有所助益。The desorbed gas G8 is returned to the cooling and condensing
將本實施形態之第一濃縮裝置200,於使吸附單元210繞筒軸旋轉之中空圓柱狀的轉筒之繞筒軸的圓周方向配置複數個。藉此,可高效率地回收有機溶劑。The first concentrating
本實施形態之第二濃縮裝置300,將吸附元件310配置於繞筒軸旋轉之圓盤狀的吸附轉筒。藉此,可高效率地回收有機溶劑。In the second concentrating
[其他實施形態]
上述實施形態中,濃縮裝置,利用第一濃縮裝置200與第二濃縮裝置300此兩台。濃縮裝置,亦可因應風量,應用兩台第一濃縮裝置200或兩台第二濃縮裝置300。此外,亦可因應去除效率,應用三台以上之濃縮裝置。[Other embodiments]
In the above embodiment, two concentrating devices, the first concentrating
作為排放氣體G1所含有的有機溶劑,列舉可藉由1℃~50℃之冷卻而液化回收的有機溶劑。作為有機溶劑,例如為N-甲基吡咯烷酮、N-乙基吡咯烷酮、N,N-二甲基甲醯胺、N,N-二甲基乙醯胺、或正癸烷。其等僅為例示,並未限定於其等。所含有的有機溶劑,可為1種亦可為複數種。Examples of the organic solvent contained in the exhaust gas G1 include organic solvents that can be liquefied and recovered by cooling at 1°C to 50°C. The organic solvent is, for example, N-methylpyrrolidone, N-ethylpyrrolidone, N,N-dimethylformamide, N,N-dimethylacetamide, or n-decane. These etc. are only examples, and are not limited to them. The organic solvent contained may be one type or plural types.
本次揭露之實施形態全部的點僅為例示,應考慮到其等並非用於限制本發明。本發明揭露之範圍,係由發明申請專利範圍而非上述說明顯示,本發明意在包含發明申請專利範圍、及其均等意涵與範圍內之全部變更。All the points of the embodiment disclosed this time are only examples, and it should be considered that they are not intended to limit the present invention. The scope of the disclosure of the present invention is shown by the scope of the invention patent application rather than the above description. The invention is intended to include the scope of the invention patent application and all changes within the equivalent meaning and scope thereof.
1A,1B,1C,1D,2B,2C,2D,3C,3D,4C,4D:有機溶劑回收系統
100:冷卻冷凝裝置
110:冷卻部
111:第一熱交換器
112:第二熱交換器
120:分離部
121:網眼狀構造體
122:承接部
123:腔室
124:堰部
126:加熱器
125:貯存槽
127:頂棚部
128:分隔部
130:生產設備
200:第一濃縮裝置
210:吸附單元
211:內周側流路形成構件
212:吸附轉筒
213:外周側流路形成構件
250,350:再生加熱器
300:第二濃縮裝置
310:吸附元件
311:脫附部(脫附區)
312:吸附部(吸附區)
500,600:濃縮裝置
F1:第一流通路徑
F2:第二流通路徑
F3:第三流通路徑
F4:第四流通路徑
F5:第五流通路徑
F6:第六流通路徑
G1,G2:排放氣體
G3,G4,G5,G6:冷卻處理氣體
G7,G10:高溫氣體
G8,G11:脫附氣體
G9:潔淨氣體
L1:冷卻冷凝液
L2:脫附冷凝液
L3:回收液1A, 1B, 1C, 1D, 2B, 2C, 2D, 3C, 3D, 4C, 4D: organic solvent recovery system
100: Cooling and condensing device
110: Cooling part
111: The first heat exchanger
112: second heat exchanger
120: Separation part
121: Mesh structure
122: Acceptance Department
123: Chamber
124: Weir
126: heater
125: storage tank
127: Ceiling Department
128: divider
130: production equipment
200: The first concentration device
210: Adsorption unit
211: Inner peripheral side flow path forming member
212: Adsorption drum
213: Peripheral flow
圖1係概略顯示實施形態1A的有機溶劑回收系統之構成的圖。
圖2係實施形態1A的有機溶劑回收系統之另一構成圖的一例。
圖3係實施形態1A的有機溶劑回收系統之更另一構成圖的一例。
圖4係實施形態1B的有機溶劑回收系統之構成概略顯示的圖。
圖5係概略顯示實施形態2B的有機溶劑回收系統之構成的圖。
圖6係概略顯示實施形態1C的有機溶劑回收系統之構成的圖。
圖7係概略顯示實施形態2C的有機溶劑回收系統之構成的圖。
圖8係概略顯示實施形態3C的有機溶劑回收系統之構成的圖。
圖9係概略顯示實施形態4C的有機溶劑回收系統之構成的圖。
圖10係概略顯示實施形態1D的有機溶劑回收系統之構成的圖。
圖11係概略顯示實施形態2D的有機溶劑回收系統之構成的圖。
圖12係概略顯示實施形態3D的有機溶劑回收系統之構成的圖。
圖13係概略顯示實施形態4D的有機溶劑回收系統之構成的圖。Fig. 1 is a diagram schematically showing the configuration of the organic solvent recovery system of
1A:有機溶劑回收系統 1A: Organic solvent recovery system
100:冷卻冷凝裝置 100: Cooling and condensing device
110:冷卻部 110: Cooling part
111:第一熱交換器 111: The first heat exchanger
112:第二熱交換器 112: second heat exchanger
120:分離部 120: Separation part
121:網眼狀構造體 121: Mesh structure
123:腔室 123: Chamber
125:貯存槽 125: storage tank
127:頂棚部 127: Ceiling Department
128:分隔部 128: divider
130:生產設備 130: production equipment
300:第二濃縮裝置 300: The second concentration device
310:吸附元件 310: Adsorption component
311:脫附部(脫附區) 311: Desorption part (desorption area)
312:吸附部(吸附區) 312: Adsorption part (adsorption zone)
350:再生加熱器 350: Regenerative heater
F1:第一流通路徑 F1: The first circulation path
F2:第二流通路徑 F2: Second circulation path
G1,G2:排放氣體 G1, G2: exhaust gas
G3,G4,G6:冷卻處理氣體 G3, G4, G6: Cooling process gas
G9:潔淨氣體 G9: Clean gas
G10:高溫氣體 G10: High temperature gas
G11:脫附氣體 G11: desorption gas
L1:冷卻冷凝液 L1: Cooling condensate
L2:脫附冷凝液 L2: Desorption condensate
L3:回收液 L3: Recovered liquid
Claims (30)
Applications Claiming Priority (10)
Application Number | Priority Date | Filing Date | Title |
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JP2019-236744 | 2019-12-26 | ||
JP2019236744A JP7434891B2 (en) | 2019-12-26 | 2019-12-26 | Organic solvent recovery system |
JP2020-144541 | 2020-08-28 | ||
JP2020-144544 | 2020-08-28 | ||
JP2020-144543 | 2020-08-28 | ||
JP2020144543 | 2020-08-28 | ||
JP2020144542 | 2020-08-28 | ||
JP2020144544 | 2020-08-28 | ||
JP2020144541A JP7435367B2 (en) | 2019-12-26 | 2020-08-28 | Organic solvent recovery system |
JP2020-144542 | 2020-08-28 |
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TW202130404A true TW202130404A (en) | 2021-08-16 |
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