TW202103772A - Organic solvent recovery system - Google Patents

Organic solvent recovery system Download PDF

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TW202103772A
TW202103772A TW109110375A TW109110375A TW202103772A TW 202103772 A TW202103772 A TW 202103772A TW 109110375 A TW109110375 A TW 109110375A TW 109110375 A TW109110375 A TW 109110375A TW 202103772 A TW202103772 A TW 202103772A
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adsorption
organic solvent
carrier gas
desorption
recovery device
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岡田武将
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日商東洋紡股份有限公司
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0033—Other features
    • B01D5/0051—Regulation processes; Control systems, e.g. valves
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
    • B01D5/0084—Feeding or collecting the cooling medium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/38—Removing components of undefined structure
    • B01D53/44—Organic components

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  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Automation & Control Theory (AREA)
  • Treating Waste Gases (AREA)
  • Separation Of Gases By Adsorption (AREA)

Abstract

An organic solvent recovery system that separates and recovers an organic solvent from a gas to be treated containing the organic solvent, comprising: a circulation route to circulate a carrier gas; an adsorption and desorption device that has an adsorption and desorption element and that alternately performs adsorption of the organic solvent by way of introducing the gas to be treated and desorption of the organic solvent by way of introducing the carrier gas; a condensation and recovery device that is provided in the circulation route on the downstream side of the adsorption and desorption device and that condenses and recovers the organic solvent contained in the carrier gas by cooling the carrier gas discharged from the adsorption and desorption device; and a heating unit that is provided in the circulation route on the upstream side of the adsorption and desorption device and that heats the low-temperature carrier gas discharged from the condensation and recovery device. The condensation and recovery device adjusts the temperature of the carrier gas discharged from the condensation and recovery device so that the vapor pressure of the organic solvent contained in the carrier gas discharged from the condensation and recovery device is less than or equal to a prescribed value.

Description

有機溶劑回收系統Organic solvent recovery system

本發明係關於一種有機溶劑回收系統，從含有有機溶劑之被處理氣體分離出有機溶劑並將被處理氣體清潔化後排出，並且使用載體氣體來回收經分離之有機溶劑。The present invention relates to an organic solvent recovery system. The organic solvent is separated from the processed gas containing the organic solvent and the processed gas is cleaned and discharged, and the carrier gas is used to recover the separated organic solvent.

先前，如下含有有機溶劑之氣體處理系統已為人所知，即，使用吸附材料對含有有機溶劑之被處理氣體進行有機溶劑的吸附處理及脫附處理，使有機溶劑從被處理氣體移動至載體氣體，藉此可進行被處理氣體的清潔化及有機溶劑的回收。Previously, the following gas treatment systems containing organic solvents have been known, that is, the use of adsorbents to perform adsorption treatment and desorption treatment of organic solvents on the gas to be treated containing organic solvents, so that the organic solvent moves from the gas to be treated to the carrier The gas can be cleaned of the gas to be processed and the organic solvent can be recovered by this.

這種有機溶劑回收系統通常具備：吸附脫附處理裝置，係使含有有機溶劑之被處理氣體及處於高溫狀態之載體氣體在時間上交替地與吸附材料接觸；以及冷凝回收裝置，係藉由將從該吸附脫附處理裝置排出之載體氣體冷卻，而使有機溶劑冷凝並進行回收。This organic solvent recovery system usually has: an adsorption and desorption processing device, which makes the processed gas containing the organic solvent and the carrier gas in a high temperature state alternately contact the adsorption material in time; and a condensation recovery device, which is used to The carrier gas discharged from the adsorption-desorption treatment device is cooled, and the organic solvent is condensed and recovered.

作為這種有機溶劑回收系統之一，專利文獻1中揭示了一種使用水蒸氣作為載體氣體之含有有機溶劑之氣體處理系統。As one of such organic solvent recovery systems, Patent Document 1 discloses a gas processing system containing an organic solvent that uses water vapor as a carrier gas.

而且，近來，期望一種以回收之有機溶劑的高品質化或排水處理步驟的簡化為目的之低排水量的有機溶劑回收系統，且專利文獻2中揭示了一種對間接加熱至高溫之吸附材料供給載體氣體之有機溶劑回收系統。 [先前技術文獻] [專利文獻]In addition, recently, a low-water-volume organic solvent recovery system for the purpose of improving the quality of the recovered organic solvent or simplifying the waste water treatment process is desired, and Patent Document 2 discloses a carrier for supplying an adsorbent that is indirectly heated to a high temperature. Gas organic solvent recovery system. [Prior Technical Literature] [Patent Literature]

[專利文獻1]日本實用新型申請公報「實全平3-32924」。 [專利文獻2]日本公開專利公報「日本特開平7-68127」。[Patent Document 1] Japanese Utility Model Application Publication "Shiquanping 3-32924". [Patent Document 2] Japanese Laid-Open Patent Publication "Japanese Patent Laid-Open No. 7-68127".

[發明所欲解決之課題][The problem to be solved by the invention]

這種有機溶劑回收系統中，為了提高對被處理氣體之淨化能力及有機溶劑的回收效率，必須充分地進行脫附處理中之有機溶劑的脫附(亦即吸附材料之再生)。In this organic solvent recovery system, in order to improve the purification ability of the gas to be processed and the recovery efficiency of the organic solvent, it is necessary to fully desorb the organic solvent in the desorption process (that is, the regeneration of the adsorbent material).

而且，為了抑制有機溶劑回收系統的運轉成本，較佳為構成為使所使用之載體氣體於有機溶劑回收系統內循環並再利用。Furthermore, in order to suppress the operating cost of the organic solvent recovery system, it is preferable to configure the carrier gas used in the organic solvent recovery system to circulate and reuse it.

然而，由於難以在冷凝回收裝置中使有機溶劑從載體氣體完全地分離出，因此從冷凝回收裝置排出之載體氣體中會含有未冷凝的有機溶劑。從而，在使載體氣體循環並返回至吸附脫附處理裝置之構成的情況下，會產生如下問題：吸附材料的再生有時會不充分，且對被處理氣體之淨化能力及有機溶劑的回收效率自然地受到限制。However, since it is difficult to completely separate the organic solvent from the carrier gas in the condensation recovery device, the carrier gas discharged from the condensation recovery device may contain uncondensed organic solvent. Therefore, when the carrier gas is circulated and returned to the structure of the adsorption and desorption treatment device, the following problems may arise: the regeneration of the adsorbent is sometimes insufficient, and the purification ability of the gas to be processed and the recovery efficiency of organic solvents Naturally restricted.

因此，本發明係為了解決上述問題而完成，目的在於提供一種能夠抑制運轉成本並且提高了被處理氣體的淨化能力及有機溶劑的回收效率之有機溶劑回收系統。 [用以解決課題之手段]Therefore, the present invention was completed in order to solve the above-mentioned problems, and the object is to provide an organic solvent recovery system that can suppress operating costs and improve the purification ability of the gas to be processed and the recovery efficiency of the organic solvent. [Means to solve the problem]

本發明者經過積極研究後發現，藉由以下所示之手段可解決上述問題，從而完成本發明。亦即，本發明包含以下構成。 1.一種有機溶劑回收系統，從含有有機溶劑之被處理氣體分離出有機溶劑並進行回收；具備：循環路徑，係使載體氣體循環流通；吸附脫附處理裝置，係具有吸附脫附元件，交替地進行藉由前述被處理氣體的導入所為之前述有機溶劑的吸附、及藉由前述載體氣體的導入所為之前述有機溶劑的脫附；冷凝回收裝置，係設置於前述循環路徑上且為前述吸附脫附處理裝置的下游側，將從該吸附脫附處理裝置排出之前述載體氣體冷卻且將該載體氣體所含有之有機溶劑冷凝並回收；以及加熱部，係設置於前述循環路徑上且為前述吸附脫附處理裝置的上游側，將從前述冷凝回收裝置排出之低溫狀態的前述載體氣體加熱；前述冷凝回收裝置係以從該冷凝回收裝置排出之載體氣體所含有之有機溶劑的蒸氣壓成為預定值以下的方式，來調節從該冷凝回收裝置排出之載體氣體的溫度。 根據上述構成，以從冷凝回收裝置排出之載體氣體中含有之有機溶劑的蒸氣壓成為預定值以下之方式進行溫度調節，藉此能夠使所排出之載體氣體中之有機溶劑的濃度為固定以下，無須在冷凝回收裝置與吸附脫附處理裝置之間設置用以吸附去除載體氣體中之有機溶劑之其他吸附裝置等。藉此，能夠使系統為簡單的構成而能夠小型化。 2.如上述1所記載之有機溶劑回收系統，具備溫度測定機構，係測定從前述冷凝回收裝置排出之載體氣體的溫度；前述冷凝回收裝置係基於前述溫度測定機構的測定值，以前述蒸氣壓成為預定值以下之方式來調節所排出之載體氣體的溫度。 3.如上述1所記載之有機溶劑回收系統，具備蒸氣壓測定機構，係測定從前述冷凝回收裝置排出之載體氣體的蒸氣壓；前述冷凝回收裝置係基於前述蒸氣壓測定機構的測定值，以前述蒸氣壓成為預定值以下之方式來調節所排出之載體氣體的溫度。 4.如上述1至3中任一項所記載之有機溶劑回收系統，其中前述冷凝回收裝置係藉由使用了冷媒之間接冷卻來將前述載體氣體冷卻。 5.如上述4所記載之有機溶劑回收系統，其中前述冷媒係水、乙二醇、丙二醇、甘油、乙醇中之任一者或其混合物。 [發明功效]After active research, the inventor found that the above-mentioned problems can be solved by the means shown below, thereby completing the present invention. That is, the present invention includes the following configurations. 1. An organic solvent recovery system, which separates and recovers the organic solvent from the processed gas containing the organic solvent; equipped with: a circulation path to circulate the carrier gas; an adsorption and desorption treatment device with an adsorption and desorption element, alternately The adsorption of the organic solvent by the introduction of the gas to be treated and the desorption of the organic solvent by the introduction of the carrier gas are performed; the condensation recovery device is installed on the circulation path and is the adsorption On the downstream side of the desorption treatment device, the carrier gas discharged from the adsorption and desorption treatment device is cooled and the organic solvent contained in the carrier gas is condensed and recovered; and the heating part is installed on the circulation path and is the aforementioned The upstream side of the adsorption and desorption treatment device heats the carrier gas in a low-temperature state discharged from the condensation recovery device; the condensation recovery device sets the vapor pressure of the organic solvent contained in the carrier gas discharged from the condensation recovery device to a predetermined value The temperature of the carrier gas discharged from the condensation recovery device can be adjusted in a manner below the value. According to the above configuration, the temperature is adjusted so that the vapor pressure of the organic solvent contained in the carrier gas discharged from the condensation recovery device becomes below a predetermined value, whereby the concentration of the organic solvent in the discharged carrier gas can be kept constant or less. It is not necessary to install other adsorption devices for adsorbing and removing the organic solvent in the carrier gas between the condensation recovery device and the adsorption and desorption processing device. Thereby, the system can be reduced in size with a simple structure. 2. The organic solvent recovery system described in 1 above is equipped with a temperature measuring mechanism that measures the temperature of the carrier gas discharged from the condensation recovery device; the condensation recovery device is based on the value measured by the temperature measuring mechanism and uses the vapor pressure The temperature of the discharged carrier gas is adjusted to be below the predetermined value. 3. The organic solvent recovery system described in 1 above is equipped with a vapor pressure measurement mechanism that measures the vapor pressure of the carrier gas discharged from the condensation recovery device; the condensation recovery device is based on the value measured by the vapor pressure measurement mechanism. The temperature of the discharged carrier gas is adjusted so that the vapor pressure becomes below a predetermined value. 4. The organic solvent recovery system described in any one of 1 to 3 above, wherein the condensation recovery device cools the carrier gas by indirect cooling using a refrigerant. 5. The organic solvent recovery system as described in 4 above, wherein the aforementioned refrigerant is any one of water, ethylene glycol, propylene glycol, glycerol, and ethanol, or a mixture thereof. [Efficacy of invention]

根據本發明，以從冷凝回收裝置排出之載體氣體中含有之有機溶劑的蒸氣壓成為預定值以下之方式進行溫度調節，藉此，能夠使所排出之載體氣體中之有機溶劑的濃度為固定以下，無須在冷凝回收裝置與吸附脫附處理裝置之間設置用以吸附去除載體氣體中之有機溶劑之其他吸附裝置等，且能夠保持淨化能力。藉此，能夠使系統為簡單的構成而能夠小型化。這樣，根據本發明，能夠提供一種可抑制運轉成本並且可謀求被處理氣體的淨化能力及有機溶劑的回收效率的提高之有機溶劑回收系統。According to the present invention, the temperature is adjusted so that the vapor pressure of the organic solvent contained in the carrier gas discharged from the condensation recovery device becomes below a predetermined value, whereby the concentration of the organic solvent in the discharged carrier gas can be kept below a fixed value , It is not necessary to install other adsorption devices for adsorbing and removing the organic solvent in the carrier gas between the condensation recovery device and the adsorption and desorption processing device, and the purification ability can be maintained. Thereby, the system can be reduced in size with a simple structure. In this way, according to the present invention, it is possible to provide an organic solvent recovery system that can reduce the operating cost and can improve the purification ability of the gas to be processed and the recovery efficiency of the organic solvent.

以下，參照圖對本發明之實施形態進行詳細說明。另外，以下所示之實施形態中，對相同或共通之部分在圖中附上相同之符號，且該部分之說明不再重複。Hereinafter, embodiments of the present invention will be described in detail with reference to the drawings. In addition, in the embodiments shown below, the same or common parts are given the same symbols in the drawings, and the description of the parts will not be repeated.

如圖1所示般，本實施形態中之有機溶劑回收系統100A具備供載體氣體以循環之方式流通之循環路徑L1、設置於循環路徑L1上之吸附脫附處理裝置10、冷凝回收裝置20、循環送風機40、以及被處理氣體送風機50。作為載體氣體，可使用水蒸氣、加熱空氣、加熱至高溫之惰性氣體等各種氣體。尤其，若使用屬於不含水分之氣體之惰性氣體，則能夠更簡單地構成有機溶劑回收系統100A。As shown in FIG. 1, the organic solvent recovery system 100A in this embodiment includes a circulation path L1 for circulating carrier gas in a circulating manner, an adsorption-desorption processing device 10, a condensation recovery device 20, and a condensation recovery device 20 provided on the circulation path L1. Circulation blower 40 and to-be-processed gas blower 50. As the carrier gas, various gases such as water vapor, heated air, and inert gas heated to a high temperature can be used. In particular, if an inert gas that is a gas that does not contain moisture is used, the organic solvent recovery system 100A can be constructed more simply.

循環路徑L1具備圖中所示之配管管線L4至配管管線L7。循環送風機40係用以使載體氣體於循環路徑L1流通之送風機構，被處理氣體送風機50係用以從配管管線L2朝吸附脫附處理裝置10供給被處理氣體之送風機構。The circulation path L1 includes the piping line L4 to the piping line L7 shown in the figure. The circulation blower 40 is a blower mechanism for circulating the carrier gas through the circulation path L1, and the processed gas blower 50 is a blower mechanism for supplying the processed gas from the piping line L2 to the adsorption and desorption processing device 10.

吸附脫附處理裝置10具備吸附脫附槽A11及吸附脫附槽B12、以及作為溫度調節機構之加熱器30。吸附脫附槽A11中填充有用以吸附及脫附有機溶劑之吸附脫附元件A13，吸附脫附槽B12中填充有用以吸附及脫附有機溶劑之吸附脫附元件B14。本實施形態中具備兩個吸附脫附槽，但該吸附脫附槽亦可為一個，還可為三個以上。The adsorption-desorption processing apparatus 10 includes an adsorption-desorption tank A11 and an adsorption-desorption tank B12, and a heater 30 as a temperature adjustment mechanism. The adsorption and desorption tank A11 is filled with an adsorption and desorption element A13 for adsorbing and desorbing an organic solvent, and the adsorption and desorption tank B12 is filled with an adsorption and desorption element B14 for adsorbing and desorbing an organic solvent. In the present embodiment, two adsorption and desorption tanks are provided, but the number of the adsorption and desorption tanks may be one or three or more.

加熱器30將供給至吸附脫附槽A11或吸附脫附槽B12之載體氣體溫度調節為高溫狀態。更具體而言，加熱器30將從冷凝回收裝置20排出並經過循環送風機40之載體氣體溫度調節為高溫狀態並供給至吸附脫附槽A11或吸附脫附槽B12。此處，加熱器30以吸附脫附元件A13及吸附脫附元件B14維持為預定之吸附脫附溫度之方式，來對於導入至吸附脫附槽A11及吸附脫附槽B12之載體氣體進行溫度調節。The heater 30 adjusts the temperature of the carrier gas supplied to the adsorption and desorption tank A11 or the adsorption and desorption tank B12 to a high temperature state. More specifically, the heater 30 adjusts the temperature of the carrier gas discharged from the condensation recovery device 20 and passed through the circulating blower 40 to a high temperature state and supplies it to the adsorption and desorption tank A11 or the adsorption and desorption tank B12. Here, the heater 30 adjusts the temperature of the carrier gas introduced into the adsorption and desorption tank A11 and the adsorption and desorption tank B12 so that the adsorption and desorption element A13 and the adsorption and desorption element B14 are maintained at predetermined adsorption and desorption temperatures. .

吸附脫附元件A13及吸附脫附元件B14藉由接觸被處理氣體而吸附被處理氣體所含有之有機溶劑。因此，吸附脫附處理裝置10中，當朝吸附脫附槽A11或吸附脫附槽B12供給被處理氣體時，有機溶劑會被吸附脫附元件A13或吸附脫附元件B14吸附而從被處理氣體中去除有機溶劑並清潔化被處理氣體，且以清潔氣體的形式從吸附脫附槽A11或吸附脫附槽B12排出。The adsorption and desorption element A13 and the adsorption and desorption element B14 adsorb the organic solvent contained in the gas to be processed by contacting the gas to be processed. Therefore, in the adsorption-desorption processing apparatus 10, when the gas to be processed is supplied to the adsorption-desorption tank A11 or the adsorption-desorption tank B12, the organic solvent is adsorbed by the adsorption-desorption element A13 or the adsorption-desorption element B14 and removed from the gas to be processed. The organic solvent is removed from the gas and the gas to be treated is cleaned, and is discharged from the adsorption and desorption tank A11 or the adsorption and desorption tank B12 in the form of clean gas.

而且，吸附脫附元件A13及吸附脫附元件B14係藉由接觸處於高溫狀態之載體氣體而將所吸附之有機溶劑脫附。因此，吸附脫附處理裝置10中，當朝吸附脫附槽A11或吸附脫附槽B12供給處於高溫狀態之載體氣體時，有機溶劑會從吸附脫附元件A13或吸附脫附元件B14脫附，含有有機溶劑之載體氣體從吸附脫附槽A11或吸附脫附槽B12排出。Moreover, the adsorption and desorption element A13 and the adsorption and desorption element B14 desorb the adsorbed organic solvent by contacting the carrier gas in a high temperature state. Therefore, in the adsorption-desorption processing apparatus 10, when the carrier gas in a high-temperature state is supplied to the adsorption-desorption tank A11 or the adsorption-desorption tank B12, the organic solvent is desorbed from the adsorption-desorption element A13 or the adsorption-desorption element B14. The carrier gas containing the organic solvent is discharged from the adsorption and desorption tank A11 or the adsorption and desorption tank B12.

吸附脫附元件A13及吸附脫附元件B14由包含粒狀活性碳、活性碳纖維、沸石、矽膠、多孔質性高分子及金屬有機結構體中之任一種之吸附材料所構成。較佳為利用粒狀、粉體狀、蜂窩狀等之活性碳或沸石，更佳為利用活性碳纖維。活性碳纖維由於具有在表面有微孔之纖維狀構造，因此與氣體之接觸效率高，實現了較其他吸附材料更高之吸附效率及脫附效率。The adsorption and desorption element A13 and the adsorption and desorption element B14 are composed of an adsorption material including any one of granular activated carbon, activated carbon fiber, zeolite, silica gel, porous polymer, and metal organic structure. It is preferable to use granular, powder, honeycomb, etc. activated carbon or zeolite, and more preferably to use activated carbon fiber. Activated carbon fiber has a fibrous structure with micropores on the surface, so it has a high contact efficiency with gas, and achieves higher adsorption and desorption efficiency than other adsorption materials.

吸附脫附處理裝置10分別連接有配管管線L2、L3。配管管線L2係用以經由被處理氣體送風機50將含有有機溶劑之被處理氣體供給至吸附脫附槽A11或吸附脫附槽B12之配管管線。配管管線L2藉由閥V1切換對吸附脫附槽A11之連接/非連接狀態，藉由閥V3切換對吸附脫附槽B12之連接/非連接狀態。配管管線L3係用以將清潔氣體從吸附脫附槽A11或吸附脫附槽B12排出之配管管線。配管管線L3藉由閥V2切換對吸附脫附槽A11之連接/非連接狀態，藉由閥V4切換對吸附脫附槽B12之連接/非連接狀態。Piping lines L2 and L3 are respectively connected to the adsorption and desorption processing device 10. The piping line L2 is a piping line for supplying the processed gas containing an organic solvent to the adsorption and desorption tank A11 or the adsorption and desorption tank B12 via the processed gas blower 50. The piping line L2 switches the connection/non-connection state to the adsorption/desorption tank A11 through the valve V1, and switches the connection/non-connection state to the adsorption/desorption tank B12 through the valve V3. The piping line L3 is a piping line used to discharge clean gas from the adsorption and desorption tank A11 or the adsorption and desorption tank B12. The piping line L3 switches the connection/non-connection state to the adsorption/desorption tank A11 through the valve V2, and switches the connection/non-connection state to the adsorption/desorption tank B12 through the valve V4.

進而，吸附脫附處理裝置10分別連接有配管管線L5、L6。 配管管線L5係用以經由加熱器30將載體氣體供給至吸附脫附槽A11或吸附脫附槽B12之配管管線。配管管線L5藉由閥V5切換對吸附脫附槽A11之連接/非連接狀態，藉由閥V7切換對吸附脫附槽B12之連接/非連接狀態。配管管線L6係用以將載體氣體從吸附脫附槽A11或吸附脫附槽B12排出之配管管線。配管管線L6藉由閥V6切換對吸附槽A11之連接/非連接狀態，藉由V8切換對吸附脫附槽B12之連接/非連接狀態。Furthermore, piping lines L5 and L6 are connected to the adsorption-desorption processing apparatus 10, respectively. The piping line L5 is a piping line for supplying the carrier gas to the adsorption and desorption tank A11 or the adsorption and desorption tank B12 via the heater 30. The piping line L5 switches the connection/non-connection state to the adsorption/desorption tank A11 by the valve V5, and switches the connection/non-connection state to the adsorption/desorption tank B12 by the valve V7. The piping line L6 is a piping line for discharging the carrier gas from the adsorption and desorption tank A11 or the adsorption and desorption tank B12. The piping line L6 switches the connection/non-connection state to the adsorption tank A11 through the valve V6, and switches the connection/non-connection state to the adsorption/desorption tank B12 through the valve V8.

藉由操作上述閥V1至閥V8之開閉，將被處理氣體與處於高溫狀態之載體氣體在時間上交替地分別供給至吸附脫附槽A11及吸附脫附槽B12。藉此，吸附脫附槽A11及吸附脫附槽B12藉由在時間上交替地作為吸附槽及脫附槽發揮功能，伴隨於此，有機溶劑從被處理氣體移動至處於高溫狀態之載體氣體。另外，具體而言，於吸附脫附槽A11作為吸附槽發揮功能之期間，吸附脫附槽B12作為脫附槽發揮功能，於吸附脫附槽A11作為脫附槽發揮功能之期間，吸附脫附槽B12作為吸附槽發揮功能。By operating the opening and closing of the valves V1 to V8, the gas to be processed and the carrier gas in a high temperature state are alternately supplied in time to the adsorption and desorption tank A11 and the adsorption and desorption tank B12, respectively. Thereby, the adsorption and desorption tank A11 and the adsorption and desorption tank B12 function as an adsorption tank and a desorption tank alternately in time, and with this, the organic solvent moves from the gas to be processed to the carrier gas in a high temperature state. In addition, specifically, while the adsorption and desorption tank A11 functions as an adsorption tank, the adsorption and desorption tank B12 functions as a desorption tank, and while the adsorption and desorption tank A11 functions as a desorption tank, the adsorption and desorption The tank B12 functions as an adsorption tank.

冷凝回收裝置20具備冷凝器(condenser)21及回收箱22。冷凝器21藉由將從吸附脫附槽A11或吸附脫附槽B12排出之處於高溫狀態之載體氣體溫度調節為低溫狀態，而使載體氣體所含有之有機溶劑冷凝。具體而言，冷凝器21藉由使用冷媒來間接冷卻載體氣體而使有機溶劑液化。回收箱22係將已由冷凝器21液化之有機溶劑以冷凝液之形式貯存。The condensation recovery device 20 includes a condenser 21 and a recovery tank 22. The condenser 21 condenses the organic solvent contained in the carrier gas by adjusting the temperature of the carrier gas in a high temperature state discharged from the adsorption and desorption tank A11 or the adsorption and desorption tank B12 to a low temperature state. Specifically, the condenser 21 indirectly cools the carrier gas by using a refrigerant to liquefy the organic solvent. The recovery tank 22 stores the organic solvent that has been liquefied by the condenser 21 in the form of condensate.

冷媒能夠使用水、一級醇(primary alcohol)、二級醇(secondary alcohol)、三級醇(tertiary alcohol)、氫氯氟碳化物(hydrochlorofluorocarbons)、氫氟碳化物(hydrofluorocarbons)、氨(ammonia)中之任一種或這些的混合物，尤其，若使用水、乙二醇、丙二醇、甘油、乙醇中之任一種或其混合物，則能夠更簡單地構成有機溶劑回收系統100A。The refrigerant can be used in water, primary alcohol, secondary alcohol, tertiary alcohol, hydrochlorofluorocarbons, hydrofluorocarbons, ammonia Any one or a mixture of these, especially, if any one or a mixture of water, ethylene glycol, propylene glycol, glycerin, and ethanol is used, the organic solvent recovery system 100A can be constructed more simply.

冷凝回收裝置20分別連接有配管管線L6、L7。配管管線L6係用以將從吸附脫附處理裝置10排出之載體氣體供給至冷凝器21之配管管線。配管管線L7係用以將載體氣體從冷凝器21排出之配管管線。Piping lines L6 and L7 are connected to the condensation recovery device 20, respectively. The piping line L6 is a piping line for supplying the carrier gas discharged from the adsorption-desorption processing device 10 to the condenser 21. The piping line L7 is a piping line for discharging the carrier gas from the condenser 21.

而且，冷凝器21連接有配管管線L9。配管管線L9係用以將已由冷凝器21冷凝之有機溶劑導入至回收箱22之配管管線。In addition, the condenser 21 is connected to a piping line L9. The piping line L9 is a piping line for introducing the organic solvent condensed by the condenser 21 to the recovery tank 22.

圖2係表示在圖1所示之有機溶劑回收系統100A中，使用了吸附脫附元件A13及吸附脫附元件B14之吸附處理及脫附處理之時間上的切換之情況之時序圖。接下來，參照該圖2，以載體氣體使用了惰性氣體之情形為例，對使用了本實施形態中之有機溶劑回收系統100A之被處理氣體的處理的詳情進行說明。FIG. 2 is a timing chart showing the switching of the time of the adsorption process and the desorption process using the adsorption and desorption element A13 and the adsorption and desorption element B14 in the organic solvent recovery system 100A shown in FIG. 1. Next, referring to FIG. 2, taking a case where an inert gas is used as a carrier gas as an example, the details of the treatment of the gas to be treated using the organic solvent recovery system 100A in this embodiment will be described.

有機溶劑回收系統100A係以圖2所示之一週期為單位期間並重複實施該週期，藉此連續地進行被處理氣體的處理。The organic solvent recovery system 100A uses a cycle as shown in FIG. 2 as a unit period and repeats the cycle, thereby continuously processing the gas to be processed.

於上述一週期之前半部分(圖2中所示之時刻t0至時刻t2之間)，在填充有吸附脫附元件A13之吸附脫附處理裝置10的吸附脫附槽A11中實施吸附處理。與此同時，在填充有吸附脫附元件B14之吸附脫附處理裝置10的吸附脫附槽B12中，實施用惰性氣體置換吸附脫附槽B12內部之沖洗(purge)處理(圖2中所示之時刻t0至時刻t1之間)，之後，實施脫附處理(圖2中所示之時刻t1至時刻t2之間)。In the first half of the above-mentioned cycle (between time t0 and time t2 shown in FIG. 2), the adsorption treatment is performed in the adsorption and desorption tank A11 of the adsorption and desorption treatment device 10 filled with the adsorption and desorption element A13. At the same time, in the adsorption and desorption tank B12 of the adsorption and desorption treatment device 10 filled with the adsorption and desorption element B14, the purge treatment of replacing the inside of the adsorption and desorption tank B12 with an inert gas is performed (shown in Figure 2 (Between time t0 and time t1), and then perform desorption treatment (between time t1 and time t2 shown in FIG. 2).

而且，於上述一週期之後半部分(圖2中所示之時刻t2至時刻t4之間)，在填充有吸附脫附元件B14之吸附脫附處理裝置10的吸附脫附槽B12中實施吸附處理，與此同時，在填充有吸附脫附元件A13之吸附脫附處理裝置10的吸附脫附槽A11中，實施用惰性氣體置換吸附脫附槽A11內部之沖洗處理(圖2中所示之時刻t2至時刻t3之間)，之後，實施脫附處理(圖2中所示之時刻t3至時刻t4之間)。Furthermore, in the latter half of the above-mentioned cycle (between time t2 and time t4 shown in FIG. 2), the adsorption and desorption process is performed in the adsorption and desorption tank B12 of the adsorption and desorption treatment device 10 filled with the adsorption and desorption element B14 At the same time, in the adsorption and desorption tank A11 of the adsorption and desorption treatment device 10 filled with the adsorption and desorption element A13, the flushing process of replacing the inside of the adsorption and desorption tank A11 with an inert gas is carried out (the time shown in Figure 2 Between t2 and time t3), after that, the desorption process is performed (between time t3 and time t4 shown in FIG. 2).

冷凝回收裝置20中，將從吸附脫附處理裝置10排出之包含有機溶劑之載體氣體利用冷凝器21間接冷卻，溫度調節為低溫狀態而使有機溶劑冷凝，並回收有機溶劑。In the condensation recovery device 20, the carrier gas containing the organic solvent discharged from the adsorption and desorption processing device 10 is indirectly cooled by the condenser 21, the temperature is adjusted to a low temperature state to condense the organic solvent, and the organic solvent is recovered.

冷凝回收裝置20以從冷凝器21排出之載體氣體所含有之有機溶劑的蒸氣壓成為預定值以下之方式進行溫度調節。例如，亦可具有調節冷凝器21的溫度之溫度調節部(未圖示)。藉由調節冷凝器21的溫度，被排出之載體氣體所含有之有機溶劑的蒸氣壓成為預定值以下，藉此，能夠使所排出之載體氣體中之有機溶劑的濃度成為固定以下。因此，能夠高效率地使吸附於吸附脫附元件之有機溶劑脫附。 例如，如後述實施例般，於有機溶劑為對二甲苯(p-xylene)之情形下，較佳為在冷凝處理中，以從冷凝器21排出之載體氣體所含有之有機溶劑的蒸氣壓成為11.4mmHg以下之方式來對載體氣體進行溫度調節，更佳為以成為6.1mmHg以下之方式來對載體氣體進行溫度調節。於從冷凝器21排出之載體氣體所含有之有機溶劑的蒸氣壓為11.4mmHg以下之情形下，由於經循環而與吸附脫附元件A13及吸附脫附元件B14接觸之載體氣體所含有之有機溶劑的蒸氣壓亦充分地降低，因此有效地促進了吸附脫附元件A13及吸附脫附元件B14之再生。另一方面，於從冷凝器21排出之載體氣體所含有之有機溶劑的蒸氣壓超過11.4mmHg之情形下，經循環而與吸附脫附元件A13及吸附脫附元件B14接觸之載體氣體所含有之有機溶劑的蒸氣壓亦為較高的值，因此難以充分地進行吸附脫附元件A13及吸附脫附元件B14之再生，就系統而言性能下降。該11.4mmHg、6.1mmHg之值係根據後述之實施例中之實驗結果導出之值。The condensation recovery device 20 performs temperature adjustment so that the vapor pressure of the organic solvent contained in the carrier gas discharged from the condenser 21 becomes a predetermined value or less. For example, it may have a temperature adjustment part (not shown) which adjusts the temperature of the condenser 21. By adjusting the temperature of the condenser 21, the vapor pressure of the organic solvent contained in the discharged carrier gas becomes below a predetermined value, whereby the concentration of the organic solvent in the discharged carrier gas can be kept below a fixed value. Therefore, it is possible to efficiently desorb the organic solvent adsorbed on the adsorption-desorption element. For example, as in the embodiments described later, when the organic solvent is p-xylene, it is preferable to use the vapor pressure of the organic solvent contained in the carrier gas discharged from the condenser 21 in the condensation treatment as The temperature of the carrier gas is adjusted to be 11.4 mmHg or less, and it is more preferable to adjust the temperature of the carrier gas to be 6.1 mmHg or less. When the vapor pressure of the organic solvent contained in the carrier gas discharged from the condenser 21 is below 11.4 mmHg, the organic solvent contained in the carrier gas that is in contact with the adsorption and desorption element A13 and the adsorption and desorption element B14 due to circulation The vapor pressure is also sufficiently reduced, thus effectively promoting the regeneration of the adsorption-desorption element A13 and the adsorption-desorption element B14. On the other hand, when the vapor pressure of the organic solvent contained in the carrier gas discharged from the condenser 21 exceeds 11.4 mmHg, the carrier gas contained in the carrier gas that is in contact with the adsorption and desorption element A13 and the adsorption and desorption element B14 through circulation The vapor pressure of the organic solvent is also a high value, so it is difficult to fully regenerate the adsorption and desorption element A13 and the adsorption and desorption element B14, and the performance of the system is reduced. The values of 11.4mmHg and 6.1mmHg are derived from the experimental results in the examples described later.

冷凝回收裝置20以從冷凝器21排出之載體氣體所含有之有機溶劑的蒸氣壓成為預定值以下的方式進行溫度調節，藉此，能夠使所排出之載體氣體中之有機溶劑的濃度成為固定以下，無須在冷凝器21與吸附脫附處理裝置10之間設置用以吸附去除載體氣體中之有機溶劑之其他吸附裝置，能夠使有機溶劑回收系統100A為簡單的構成而能夠小型化。The condensation recovery device 20 adjusts the temperature so that the vapor pressure of the organic solvent contained in the carrier gas discharged from the condenser 21 becomes a predetermined value or less, thereby enabling the concentration of the organic solvent in the discharged carrier gas to be fixed or lower There is no need to provide another adsorption device for adsorbing and removing the organic solvent in the carrier gas between the condenser 21 and the adsorption-desorption processing device 10, so that the organic solvent recovery system 100A can be simple in structure and can be miniaturized.

而且，冷凝回收裝置20亦可具備對於從冷凝器21排出之載體氣體的溫度進行測定之溫度測定器(無圖示)。冷凝回收裝置20若基於溫度測定器的測定值，以載體氣體所含有之有機溶劑的蒸氣壓成為預定值以下之方式調節從冷凝器21排出之載體氣體的溫度，則能夠更簡單地構成有機溶劑回收系統100A。Furthermore, the condensation recovery device 20 may include a temperature measuring device (not shown) that measures the temperature of the carrier gas discharged from the condenser 21. If the condensation recovery device 20 adjusts the temperature of the carrier gas discharged from the condenser 21 so that the vapor pressure of the organic solvent contained in the carrier gas becomes less than a predetermined value based on the value measured by the temperature measuring device, the organic solvent can be more easily constructed Recovery system 100A.

而且，冷凝回收裝置20亦可具備對於從冷凝器21排出之載體氣體的蒸氣壓進行測定之蒸氣壓測定器(無圖示)。冷凝回收裝置20若基於蒸氣壓測定器的測定值，以載體氣體所含有之有機溶劑的蒸氣壓成為預定值以下之方式調節從冷凝器21排出之載體氣體的溫度，則能夠更簡單地構成有機溶劑回收系統100A。測定載體氣體的蒸氣壓之方法可列舉氫焰離子化檢測法、觸媒氧化-非分散紅外線吸收法、光離子化檢測法、使用了半導體感測器之檢測法、干涉放大反射法、使用了偵測管之檢測法等，但無特別限定。Furthermore, the condensation recovery device 20 may include a vapor pressure measuring device (not shown) that measures the vapor pressure of the carrier gas discharged from the condenser 21. If the condensation recovery device 20 adjusts the temperature of the carrier gas discharged from the condenser 21 so that the vapor pressure of the organic solvent contained in the carrier gas becomes below a predetermined value based on the measured value of the vapor pressure meter, the organic solvent can be more easily constructed. Solvent recovery system 100A. Methods for measuring the vapor pressure of carrier gas include hydrogen flame ionization detection method, catalyst oxidation-non-dispersive infrared absorption method, photoionization detection method, detection method using a semiconductor sensor, interference amplification reflection method, and The detection method of the detection tube, etc., but not particularly limited.

藉由使用以上所說明之本實施形態之有機溶劑回收系統100A，達成了在脫附處理中促進吸附脫附元件A13及吸附脫附元件B14之再生之結果，且在隨後實施之吸附處理時，能夠更有效率地從被處理氣體吸附去除有機溶劑。因此，藉由使用有機溶劑回收系統100A，能夠謀求對被處理氣體之淨化能力及有機溶劑的回收效率之提高，且能夠成為較以前性能更高且更簡單之構成的系統。By using the organic solvent recovery system 100A of the present embodiment described above, the result of promoting the regeneration of the adsorption and desorption element A13 and the adsorption and desorption element B14 in the desorption process is achieved, and during the subsequent adsorption process, The organic solvent can be adsorbed and removed from the gas to be processed more efficiently. Therefore, by using the organic solvent recovery system 100A, the purification ability of the gas to be processed and the recovery efficiency of the organic solvent can be improved, and it can be a system with higher performance and simpler configuration than before.

而且，本實施形態之有機溶劑回收系統100A由於能夠藉由建構循環路徑來重複使用載體氣體，因此經濟性亦優異。因此，於將以氮氣等為代表之惰性氣體用作載體氣體之情形下，獲得能夠特別抑制運轉成本之效果。Furthermore, the organic solvent recovery system 100A of this embodiment is also excellent in economy because it can reuse the carrier gas by constructing a circulation path. Therefore, when an inert gas typified by nitrogen or the like is used as a carrier gas, the effect of particularly suppressing operating costs can be obtained.

(實施例) 以下之實施例中，使用上述本發明之實施形態中之有機溶劑回收系統100A進行被處理氣體的處理。(Example) In the following examples, the organic solvent recovery system 100A in the embodiment of the present invention described above is used to process the gas to be processed.

實施例中，使用以1500ppm之濃度含有作為有機溶劑之對二甲苯且處於40℃、相對濕度50%RH(Relative Humidity)之氣體作為被處理氣體。使用120℃之氮氣作為載體氣體。而且，使用BET(Brunauer-Emmet-Teller；布厄特)比表面積為1500mg/m2 之活性碳纖維作為吸附脫附元件A13、吸附脫附元件B14，使用5℃之水作為冷媒。In the examples, a gas containing p-xylene as an organic solvent at a concentration of 1500 ppm and at 40° C. and a relative humidity of 50% RH (Relative Humidity) was used as the gas to be processed. Use nitrogen at 120°C as the carrier gas. In addition, BET (Brunauer-Emmet-Teller; Buert) activated carbon fiber with a specific surface area of 1500 mg/m 2 was used as the adsorption and desorption element A13 and the adsorption and desorption element B14, and water at 5°C was used as the refrigerant.

首先，使用被處理氣體送風機50朝吸附脫附處理裝置10的吸附脫附槽A11及吸附脫附槽B12中之一個吸附脫附槽，以風量10Nm3 /min送風10分鐘，藉此使上述其中之一吸附脫附槽作為吸附槽發揮功能，從而實施了吸附處理。First, use the gas blower 50 to be processed toward one of the adsorption and desorption tank A11 and the adsorption and desorption tank B12 of the adsorption and desorption treatment device 10, and blow air for 10 minutes at an air volume of 10 Nm 3 /min, thereby making the above One of the adsorption and desorption tanks functions as an adsorption tank, and the adsorption treatment is performed.

上述吸附處理結束後，進行閥切換操作，將上述其中之一吸附脫附槽切換為脫附槽，並且將另一吸附脫附槽作為吸附槽。在脫附槽中進行用氮氣置換脫附槽內部之沖洗處理之後，將已利用加熱器30加熱至120℃之氮氣以風量1.5Nm3 /min導入，藉此進行了吸附脫附元件的脫附處理。在吸附槽中進行與上述條件相同之吸附處理。冷凝回收裝置20中，調節供給至冷凝器21之冷媒量，於將從脫附槽排出之含有對二甲苯之氮氣的溫度保持為10℃之狀態下使對二甲苯冷凝，並從回收箱22回收。After the adsorption process is completed, a valve switching operation is performed to switch one of the adsorption and desorption tanks to a desorption tank, and the other adsorption and desorption tank is used as an adsorption tank. After the flushing process of replacing the inside of the desorption tank with nitrogen in the desorption tank, the nitrogen heated to 120°C by the heater 30 is introduced at a flow rate of 1.5 Nm 3 /min, thereby performing the desorption of the adsorption and desorption element deal with. The adsorption treatment is carried out in the adsorption tank under the same conditions as above. In the condensation recovery device 20, the amount of refrigerant supplied to the condenser 21 is adjusted, and the p-xylene is condensed while the temperature of the nitrogen containing p-xylene discharged from the desorption tank is maintained at 10°C, and the p-xylene is condensed from the recovery tank 22 Recycling.

將以上說明之一週期連續地重複實施後，確認從吸附脫附處理裝置10排出之清潔氣體所含有之對二甲苯的濃度降低至約10ppm。亦即，確認在實施例中能夠以約99%的高去除率去除對二甲苯。After repeating one cycle of the above description continuously, it was confirmed that the concentration of p-xylene contained in the cleaning gas discharged from the adsorption-desorption processing device 10 was reduced to about 10 ppm. That is, it was confirmed that p-xylene can be removed with a high removal rate of about 99% in the examples.

而且，上述脫附處理中，確認了導入至冷凝回收裝置20之部分之配管管線L6中流通之氮氣中所含之對二甲苯的蒸氣壓平均上升至13.0mmHg，且確認了從冷凝回收裝置20排出之部分之配管管線L7中流通之氮氣中所含之對二甲苯的蒸氣壓始終降低至3.6mmHg。本實施例中，變更冷媒的溫度，以配管管線L7中流通之氮氣中所含之對二甲苯的蒸氣壓始終為3.6mmHg以下之方式調節氮氣的溫度。In addition, in the above-mentioned desorption treatment, it was confirmed that the vapor pressure of p-xylene contained in the nitrogen flowing through the pipe line L6 introduced to the part of the condensation recovery device 20 increased to 13.0 mmHg on average, and it was confirmed that the vapor pressure from the condensation recovery device 20 The vapor pressure of p-xylene contained in the nitrogen flowing in the piping line L7 of the discharged part is always reduced to 3.6 mmHg. In this embodiment, the temperature of the refrigerant is changed, and the temperature of the nitrogen gas is adjusted so that the vapor pressure of para-xylene contained in the nitrogen gas flowing through the piping line L7 is always 3.6 mmHg or less.

以上揭示之實施形態及實施例在所有方面均為例示，而非限制性說明。本發明之技術範圍由申請專利範圍所界定，且包含與申請專利範圍之記載為均等之含義及範圍內的所有變更。 [產業可利用性]The above-disclosed embodiments and examples are illustrative in all aspects and not restrictive. The technical scope of the present invention is defined by the scope of the patent application, and includes the equivalent meaning and all changes within the scope of the description in the scope of the patent application. [Industry Availability]

本發明例如能夠有效地用於處理從工廠或建築物排出之含有有機溶劑之被處理氣體之系統等。The present invention can be effectively used, for example, in a system for treating a gas to be treated containing an organic solvent discharged from a factory or a building.

10:吸附脫附處理裝置 11:吸附脫附槽A 12:吸附脫附槽B 13:吸附脫附元件A 14:吸附脫附元件B 20:冷凝回收裝置 21:冷凝器 22:回收箱 30:加熱器 40:循環送風機 50:被處理氣體送風機 100A:有機溶劑回收系統 L1:循環路徑 L2至L9:配管管線 t0至t4:時刻 V1至V8:閥10: Adsorption and desorption treatment device 11: Adsorption and desorption tank A 12: Adsorption and desorption tank B 13: Adsorption and desorption element A 14: Adsorption and desorption element B 20: Condensation recovery device 21: Condenser 22: Recycle bin 30: heater 40: Circulating blower 50: Air blower for processed gas 100A: Organic solvent recovery system L1: Loop path L2 to L9: Piping lines t0 to t4: time V1 to V8: Valve

[圖1]係表示實施形態中之有機溶劑回收系統之構造之圖。 [圖2]係表示在實施形態中之有機溶劑回收系統中，使用了一對吸附脫附元件之吸附處理及脫附處理之時間上的切換之情況之時序圖。[Figure 1] is a diagram showing the structure of the organic solvent recovery system in the embodiment. [Fig. 2] is a time chart showing the switching of the time of the adsorption process and the desorption process using a pair of adsorption and desorption elements in the organic solvent recovery system of the embodiment.

10:吸附脫附處理裝置 10: Adsorption and desorption treatment device

11:吸附脫附槽A 11: Adsorption and desorption tank A

12:吸附脫附槽B 12: Adsorption and desorption tank B

13:吸附脫附元件A 13: Adsorption and desorption element A

14:吸附脫附元件B 14: Adsorption and desorption element B

20:冷凝回收裝置 20: Condensation recovery device

21:冷凝器 21: Condenser

22:回收箱 22: Recycle bin

30:加熱器 30: heater

40:循環送風機 40: Circulating blower

50:被處理氣體送風機 50: Air blower for processed gas

100A:有機溶劑回收系統 100A: Organic solvent recovery system

L1:循環路徑 L1: Loop path

L2至L9:配管管線 L2 to L9: Piping lines

V1至V8:閥 V1 to V8: Valve

Claims (5)

一種有機溶劑回收系統，從含有有機溶劑之被處理氣體分離出有機溶劑並進行回收；具備： 循環路徑，係使載體氣體循環流通； 吸附脫附處理裝置，係具有吸附脫附元件，交替地進行藉由前述被處理氣體的導入所為之前述有機溶劑的吸附、及藉由前述載體氣體的導入所為之前述有機溶劑的脫附； 冷凝回收裝置，係設置於前述循環路徑上且為前述吸附脫附處理裝置的下游側，將從該吸附脫附處理裝置排出之前述載體氣體冷卻且將該載體氣體所含有之有機溶劑冷凝並回收；以及 加熱部，係設置於前述循環路徑上且為前述吸附脫附處理裝置的上游側，將從前述冷凝回收裝置排出之低溫狀態的前述載體氣體加熱； 前述冷凝回收裝置係以從該冷凝回收裝置排出之載體氣體所含有之有機溶劑的蒸氣壓成為預定值以下的方式，來調節從該冷凝回收裝置排出之載體氣體的溫度。An organic solvent recovery system that separates and recovers organic solvents from the processed gas containing organic solvents; equipped with: The circulation path is to circulate the carrier gas; The adsorption and desorption processing device has an adsorption and desorption element, which alternately performs the adsorption of the organic solvent by the introduction of the gas to be processed and the desorption of the organic solvent by the introduction of the carrier gas; The condensation recovery device is installed on the circulation path and downstream of the adsorption and desorption processing device, and cools the carrier gas discharged from the adsorption and desorption processing device and condenses and recovers the organic solvent contained in the carrier gas ;as well as The heating part is arranged on the circulation path and is on the upstream side of the adsorption and desorption treatment device, and heats the carrier gas in the low temperature state discharged from the condensation recovery device; The condensation recovery device adjusts the temperature of the carrier gas discharged from the condensation recovery device so that the vapor pressure of the organic solvent contained in the carrier gas discharged from the condensation recovery device becomes a predetermined value or less. 如請求項1所記載之有機溶劑回收系統，具備溫度測定機構，係測定從前述冷凝回收裝置排出之載體氣體的溫度； 前述冷凝回收裝置係基於前述溫度測定機構的測定值，以前述蒸氣壓成為預定值以下之方式來調節所排出之載體氣體的溫度。The organic solvent recovery system described in claim 1 has a temperature measuring mechanism that measures the temperature of the carrier gas discharged from the aforementioned condensation recovery device; The condensation recovery device adjusts the temperature of the discharged carrier gas based on the measurement value of the temperature measurement mechanism so that the vapor pressure becomes equal to or less than a predetermined value. 如請求項1所記載之有機溶劑回收系統，具備蒸氣壓測定機構，係測定從前述冷凝回收裝置排出之載體氣體的蒸氣壓； 前述冷凝回收裝置係基於前述蒸氣壓測定機構的測定值，以前述蒸氣壓成為預定值以下之方式來調節所排出之載體氣體的溫度。The organic solvent recovery system described in claim 1 is equipped with a vapor pressure measurement mechanism that measures the vapor pressure of the carrier gas discharged from the aforementioned condensation recovery device; The condensation recovery device adjusts the temperature of the discharged carrier gas based on the measurement value of the vapor pressure measuring mechanism so that the vapor pressure becomes equal to or less than a predetermined value. 如請求項1至3中任一項所記載之有機溶劑回收系統，其中前述冷凝回收裝置係藉由使用了冷媒之間接冷卻來將前述載體氣體冷卻。The organic solvent recovery system according to any one of claims 1 to 3, wherein the condensation recovery device cools the carrier gas by using a refrigerant indirect cooling. 如請求項4所記載之有機溶劑回收系統，其中前述冷媒係水、乙二醇、丙二醇、甘油、乙醇中之任一者或其混合物。The organic solvent recovery system described in claim 4, wherein the aforementioned refrigerant is any one of water, ethylene glycol, propylene glycol, glycerol, and ethanol, or a mixture thereof.
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