WO2020203780A1 - Organic solvent recovery system - Google Patents

Organic solvent recovery system Download PDF

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Publication number
WO2020203780A1
WO2020203780A1 PCT/JP2020/014037 JP2020014037W WO2020203780A1 WO 2020203780 A1 WO2020203780 A1 WO 2020203780A1 JP 2020014037 W JP2020014037 W JP 2020014037W WO 2020203780 A1 WO2020203780 A1 WO 2020203780A1
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Prior art keywords
organic solvent
carrier gas
desorption
suction
adsorption
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PCT/JP2020/014037
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French (fr)
Japanese (ja)
Inventor
武将 岡田
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東洋紡株式会社
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Priority to CN202080025320.6A priority Critical patent/CN113677413A/en
Priority to KR1020217030629A priority patent/KR20210137480A/en
Priority to JP2021512005A priority patent/JPWO2020203780A1/ja
Publication of WO2020203780A1 publication Critical patent/WO2020203780A1/en

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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

Definitions

  • the present invention relates to an organic solvent recovery system that separates an organic solvent from a gas to be treated containing an organic solvent, purifies and discharges the gas to be treated, and recovers the separated organic solvent using a carrier gas.
  • an adsorbent is used to adsorb and desorb an organic solvent on a gas to be treated containing an organic solvent, and the organic solvent is moved from the gas to be treated to a carrier gas to purify the gas to be treated.
  • An organic solvent-containing gas treatment system that enables recovery of an organic solvent is known.
  • This type of organic solvent recovery system generally includes an adsorption / desorption treatment device in which a gas to be treated containing an organic solvent and a carrier gas in a high temperature state are alternately brought into contact with the adsorbent in time, and the gas is discharged from the suction / desorption treatment device. It is equipped with a condensate recovery device that condenses and recovers the organic solvent by cooling the carrier gas.
  • Patent Document 1 discloses an organic solvent-containing gas treatment system using water vapor as a carrier gas.
  • Patent Document 2 describes an adsorbent that is indirectly heated to a high temperature.
  • An organic solvent recovery system that supplies carrier gas to the vehicle is disclosed.
  • the carrier gas in order to suppress the running cost of the organic solvent recovery system, it is preferable to configure the carrier gas to be circulated and reused in the organic solvent recovery system.
  • the carrier gas discharged from the condensing recovery device contains an uncondensed organic solvent. Therefore, in the case of a configuration in which the carrier gas is circulated and returned to the adsorption / desorption treatment device, the regeneration of the adsorbent may be insufficient, and there is a problem that the purification capacity for the gas to be treated and the recovery efficiency of the organic solvent are naturally limited. was there.
  • an object of the present invention is to provide an organic solvent recovery system in which the above-mentioned problems are solved, running costs can be suppressed, and the purification capacity of the gas to be treated and the recovery efficiency of the organic solvent are improved. And.
  • the present invention has the following configuration.
  • 1. It is an organic solvent recovery system that separates and recovers an organic solvent from a gas to be treated containing an organic solvent, and has a circulation path for circulating and passing a carrier gas and an adsorption / desorption element, and by introducing the gas to be treated.
  • An adsorption / desorption treatment apparatus that alternately performs adsorption of the organic solvent and desorption of the organic solvent by introduction of the carrier gas, and an adsorption / desorption treatment provided on the downstream side of the adsorption / desorption treatment apparatus on the circulation path.
  • a condensation recovery device that cools the carrier gas discharged from the device and condenses and recovers the organic solvent contained in the carrier gas, and a condensation recovery device provided on the upstream side of the adsorption / desorption treatment device on the circulation path.
  • a heating unit for heating the carrier gas in a low temperature state discharged from the condensation recovery device is provided, and the condensation recovery device has a predetermined vapor pressure of an organic solvent contained in the carrier gas discharged from the condensation recovery device.
  • An organic solvent recovery system characterized in that the temperature of the carrier gas discharged from the condensing recovery device is adjusted so as to be equal to or lower than the value.
  • the concentration of the organic solvent in the discharged carrier gas is kept below a certain level by adjusting the temperature 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. It is not necessary to install another adsorption device for adsorbing and removing the organic solvent in the carrier gas between the condensing recovery device and the adsorption / desorption treatment device. Therefore, the system can be made simple and miniaturized. 2.
  • a temperature measuring means for measuring the temperature of the carrier gas discharged from the condensing recovery device is provided, and the condensing recovery device is provided so that the water vapor pressure becomes a predetermined value or less based on the measured value of the temperature measuring means.
  • the organic solvent recovery system according to 1 above which regulates the temperature of the discharged carrier gas. 3.
  • a vapor pressure measuring means for measuring the vapor pressure of the carrier gas discharged from the condensing recovery device is provided, and the condensing recovery device has the vapor pressure of a predetermined value or less based on the measured value of the vapor pressure measuring means.
  • the organic solvent recovery system according to 1 above which regulates the temperature of the discharged carrier gas. 4.
  • the refrigerant is water, ethylene glycol, propylene glycol, glycerin, ethanol, or a mixture thereof.
  • the concentration of the organic solvent in the discharged carrier gas is kept constant by adjusting the temperature so that the vapor pressure of the organic solvent contained in the carrier gas discharged from the condensation recovery device becomes equal to or lower than a predetermined value. It is possible to do the following, and it is not necessary to install another adsorption device for adsorbing and removing the organic solvent in the carrier gas between the condensation recovery device and the adsorption / desorption treatment device, and the purification capacity can be maintained. .. Therefore, the system can be made simple and miniaturized. As described above, according to the present invention, it is possible to provide an organic solvent recovery system in which the running cost can be suppressed and the purification capacity of the gas to be treated and the recovery efficiency of the organic solvent are improved.
  • the circulation path L1 through which the carrier gas circulates, the adsorption / desorption treatment device 10 provided on the circulation path L1, and the condensation recovery A device 20, a circulation blower 40, and a gas blower 50 to be processed are provided.
  • the carrier gas various types of gases such as steam, heated air, and an inert gas heated to a high temperature can be used.
  • an inert gas which is a gas that does not contain water, is used, the organic solvent recovery system 100A can be configured more simply.
  • the circulation path L1 includes piping lines L4 to L7 shown in the figure.
  • the circulation blower 40 is a blowing means for passing the carrier gas through the circulation path L1
  • the processed gas blower 50 is a blowing means for supplying the treated gas from the piping line L2 to the suction / desorption treatment device 10. is there.
  • the suction / desorption processing device 10 includes a suction / desorption tank A11 and a suction / desorption tank B12, and a heater 30 as a temperature controlling means.
  • the adsorption / desorption tank A11 is filled with an adsorption / desorption element A13 that adsorbs and desorbs an organic solvent
  • the adsorption / desorption tank B12 is filled with an adsorption / desorption element B14 that adsorbs and desorbs an organic solvent.
  • two suction / detachment tanks are provided, but the number may be one or three or more.
  • the heater 30 adjusts the temperature of the carrier gas supplied to the suction / desorption tank A11 or the suction / desorption tank B12 to a high temperature. More specifically, the heater 30 adjusts the temperature of the carrier gas discharged from the condensing recovery device 20 and passing through the circulation blower 40 to a high temperature state and supplies the carrier gas to the suction / desorption tank A11 or the suction / desorption tank B12. Here, the heater 30 adjusts the temperature of the carrier gas introduced into the suction / desorption tank A11 and the suction / desorption tank B12 so that the suction / desorption element A13 and the suction / desorption element B14 are maintained at a predetermined desorption temperature.
  • the adsorption / desorption element A13 and the adsorption / desorption element B14 adsorb the organic solvent contained in the gas to be treated by bringing them into contact with the gas to be treated. Therefore, in the desorption treatment device 10, when the gas to be treated is supplied to the suction / desorption tank A11 or the suction / desorption tank B12, the organic solvent is adsorbed by the suction / desorption element A13 or the suction / desorption element B14, and the organic solvent is removed from the gas to be treated. Then, the gas to be treated is purified and discharged as a clean gas from the suction / desorption tank A11 or the suction / desorption tank B12.
  • the adsorption / desorption element A13 and the adsorption / desorption element B14 desorb the adsorbed organic solvent by contacting the carrier gas in a high temperature state. Therefore, in the suction / desorption treatment device 10, when the carrier gas in a high temperature state is supplied to the suction / desorption tank A11 or the suction / desorption tank B12, the organic solvent is desorbed from the suction / desorption element A13 or the suction / desorption element B14, and the organic solvent is desorbed.
  • the contained carrier gas is discharged from the suction / desorption tank A11 or the suction / desorption tank B12.
  • the adsorption / desorption element A13 and the adsorption / desorption element B14 are composed of an adsorbent containing any one of granular activated carbon, activated carbon fiber, zeolite, silica gel, a porous polymer, and a metal-organic framework.
  • activated carbon or zeolite in the form of granules, powder, honeycomb or the like is used, but more preferably, activated carbon fiber is used. Since the activated carbon fiber has a fibrous structure having micropores on its surface, it has high contact efficiency with gas, and realizes higher adsorption efficiency and desorption efficiency than other adsorbents.
  • Piping lines L2 and L3 are connected to the suction / desorption processing device 10, respectively.
  • the piping line L2 is a piping line for supplying the gas to be treated containing an organic solvent to the suction / desorption tank A11 or the suction / desorption tank B12 via the gas blower 40 to be treated.
  • the valve V1 switches the connection / non-connection state of the piping line L2 to the suction / detachment tank A11
  • the valve V3 switches the connection / non-connection state to the suction / detachment tank B12.
  • the piping line L3 is a piping line for discharging clean gas from the suction / desorption tank A11 or the suction / desorption tank B12.
  • connection / non-connection state to the suction / detachment tank A11 is switched by the valve V2
  • connection / non-connection state to the suction / detachment tank B12 is switched by the valve V4.
  • piping lines L5 and L6 are connected to the suction / desorption processing device 10, respectively.
  • the piping line L5 is a piping line for supplying the carrier gas to the suction / desorption tank A11 or the suction / desorption tank B12 via the heater 30.
  • the connection / non-connection state to the suction / detachment tank A11 is switched by the valve V5
  • the connection / non-connection state to the suction / detachment tank B12 is switched by the valve V7.
  • the piping line L6 is a piping line for discharging the carrier gas from the suction / desorption tank A11 or the suction / desorption tank B12.
  • the connection / non-connection state of the piping line L6 to the suction tank A11 is switched by the valve V6, and the connection / non-connection state to the suction / detachment tank B12 is switched by V8.
  • the gas to be treated and the carrier gas in a high temperature state are alternately supplied to the suction / desorption tank A11 and the suction / desorption tank B12 in time. ..
  • the suction / desorption tank A11 and the suction / desorption tank B12 alternately function as an adsorption tank and a desorption tank in time, and the organic solvent changes from the gas to be treated to the carrier gas in a high temperature state.
  • the suction / desorption tank B12 functions as a desorption tank
  • the suction / desorption tank A11 functions as a desorption tank
  • the suction / detachment tank B12 functions as a suction tank.
  • the condensation recovery device 20 includes a condenser (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 suction / desorption tank A11 or the suction / desorption tank B12 to a low temperature state.
  • the capacitor 21 liquefies the organic solvent by indirectly cooling the carrier gas with a refrigerant.
  • the recovery tank 22 stores the organic solvent liquefied by the condenser 21 as a condensate.
  • any one of water, primary alcohol, secondary alcohol, tertiary alcohol, hydrochlorofluorocarbons, hydrofluorocarbons, ammonia or a mixture thereof can be used, and in particular, water, ethylene glycol, propylene glycol and glycerin can be used. , Ethanol, or a mixture thereof, can be used to construct the organic solvent recovery system 100A more simply.
  • Piping lines L6 and L7 are connected to the condensate recovery device 20, respectively.
  • the piping line L6 is a piping line for supplying the carrier gas discharged from the suction / 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.
  • the piping line L9 is connected to the capacitor 21.
  • the piping line L9 is a piping line for introducing the organic solvent condensed by the condenser 21 into the recovery tank 22.
  • FIG. 2 is a time chart showing a state of temporal switching between the adsorption process and the adsorption process using the adsorption / desorption element A13 and the adsorption element B14 in the organic solvent recovery system 100A shown in FIG.
  • FIG. 2 the details of the treatment of the gas to be treated using the organic solvent recovery system 100A in the present embodiment will be described by taking the case where an inert gas is used as the carrier gas as an example.
  • the treatment of the gas to be treated is continuously performed by repeatedly carrying out the cycle with one cycle shown in FIG. 2 as a unit period.
  • the adsorption treatment is carried out in the suction / desorption tank A11 of the suction / desorption processing device 10 filled with the suction / desorption element A13.
  • a purge treatment is performed in which the inside of the suction / desorption tank B12 is replaced with an inert gas (at times t0 to t1 shown in FIG. 2).
  • the desorption process (between times t1 and t2 shown in FIG. 2) is carried out.
  • the adsorption treatment is carried out in the suction / desorption tank B12 of the suction / desorption processing device 10 filled with the suction / desorption element B14.
  • a purge treatment for replacing the inside of the suction / desorption tank A11 with an inert gas is carried out, and then the desorption process (between times t3 and t4 shown in FIG. 2) is carried out.
  • the carrier gas containing the organic solvent discharged from the adsorption / desorption treatment 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.
  • 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 is equal to or less than a predetermined value.
  • a predetermined value For example, it may have a temperature control unit (not shown) that controls the temperature of the capacitor 21.
  • the vapor pressure of the organic solvent contained in the discharged carrier gas becomes a predetermined value or less, and thus the concentration of the organic solvent in the discharged carrier gas can be kept below a certain value. it can. Therefore, the organic solvent adsorbed on the adsorption / desorption element can be efficiently desorbed.
  • the vapor pressure of the organic solvent contained in the carrier gas discharged from the capacitor 21 is 11.4 mmHg or less in the condensation process.
  • the temperature of the carrier gas is preferably adjusted, and more preferably the temperature of the carrier gas is adjusted to 6.1 mmHg or less.
  • the organic solvent contained in the carrier gas circulated and brought into contact with the suction / desorption element A13 and the suction / desorption element B14.
  • 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 is equal to or less than a predetermined value, so that the concentration of the organic solvent in the discharged carrier gas is below a certain level. It is not necessary to install another adsorption device for adsorbing and removing the organic solvent in the carrier gas between the capacitor 21 and the adsorption / desorption processing device 10, and the organic solvent recovery system 100A is simplified. It can be configured and miniaturized.
  • the condensation recovery device 20 may include a temperature measuring device (not shown) for measuring the temperature of the carrier gas discharged from the condenser 21.
  • the condensate recovery device 20 can adjust 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 equal to or less than a predetermined value based on the measured value of the temperature measuring device.
  • the organic solvent recovery system 100A can be configured more simply.
  • the condensation recovery device 20 may include a vapor pressure measuring device (not shown) for measuring the vapor pressure of the carrier gas discharged from the condenser 21.
  • the condensation recovery device 20 can adjust 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 equal to or less than a predetermined value based on the measured value of the water vapor pressure measuring device.
  • the organic solvent recovery system 100A can be configured more simply.
  • the methods for measuring the vapor pressure of carrier gas are hydrogen flame ionization detection method, catalytic oxidation-non-dispersion infrared absorption method, photoionization detection method, detection method using semiconductor sensor, interference amplification reflection method, detection method using detector tube. , Etc., but are not particularly limited.
  • the organic solvent recovery system 100A of the present embodiment described above By using the organic solvent recovery system 100A of the present embodiment described above, the regeneration of the adsorption / desorption element A13 and the adsorption / desorption element B14 is promoted in the desorption treatment, and the adsorption treatment performed thereafter
  • the organic solvent can be efficiently adsorbed and removed from the gas to be treated. Therefore, by using the organic solvent recovery system 100A, the purification ability for the gas to be treated and the recovery efficiency of the organic solvent can be improved, and the system can have a higher performance and a simpler configuration than the conventional system.
  • the organic solvent recovery system 100A of the present embodiment is excellent in economy because the carrier gas can be used repeatedly by constructing a circulation path. Therefore, when an inert gas such as nitrogen gas is used as the carrier gas, the effect of suppressing the running cost can be obtained.
  • a gas containing p-xylene at a concentration of 1500 ppm at 40 ° C. and a relative humidity of 50% RH as an organic solvent was used as the gas to be treated.
  • Nitrogen gas at 120 ° C. was used as the carrier gas.
  • activated carbon fibers having a BET specific surface area of 1500 mg / m 2 were used, and water at 5 ° C. was used as a refrigerant.
  • the suction / desorption tank A12 and the suction / desorption tank B13 of the suction / desorption treatment device 10 are blown at an air volume of 10 Nm 3 / min for 10 minutes by using the gas blower 50 to be treated.
  • the tank was made to function as an adsorption tank, and the adsorption treatment was carried out.
  • the valve was switched to switch one of the suction / detachment tanks to a desorption tank, and the other suction / desorption tank was used as a suction tank.
  • nitrogen gas heated to 120 ° C. by the heater 30 is introduced at an air volume of 1.5 Nm 3 / min to desorb the suction / desorption element. went.
  • the adsorption treatment similar to the above-mentioned conditions was performed.
  • the amount of refrigerant supplied to the condenser 21 is adjusted, and p-xylene is condensed while maintaining the temperature of the nitrogen gas containing p-xylene discharged from the desorption tank at 10 ° C., and the recovery tank is used. Recovered from 22.
  • the vapor pressure of p-xylene contained in the nitrogen gas flowing through the piping line L6 of the portion introduced into the condensation recovery device 20 increased to an average of 13.0 mmHg. It was confirmed that the vapor pressure of p-xylene contained in the nitrogen gas flowing through the piping line L7 of the portion discharged from the condensate recovery device 20 was constantly reduced to 3.6 mmHg. In this embodiment, the temperature of the refrigerant was changed, and the temperature of the nitrogen gas was adjusted so that the vapor pressure of p-xylene contained in the nitrogen gas flowing through the piping line L7 was always 3.6 mmHg or less.
  • 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.
  • Adsorption / desorption processing device 11 Adsorption / desorption tank A 12 Adsorption tank B 13 Adsorption element A 14 Adsorption element B 20 Condensation recovery device 21 Condenser 22 Recovery tank 30 Heater 40 Circulation blower 50 Processed gas blower 100A Organic solvent recovery system L1 Circulation path L2 to L11 Piping line V1 to V8 Valve

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

有機溶剤回収システムOrganic solvent recovery system
　本発明は、有機溶剤を含有する被処理ガスから有機溶剤を分離して被処理ガスを清浄化して排出すると共に、分離した有機溶剤をキャリアガスを用いて回収する有機溶剤回収システムに関する。 The present invention relates to an organic solvent recovery system that separates an organic solvent from a gas to be treated containing an organic solvent, purifies and discharges the gas to be treated, and recovers the separated organic solvent using a carrier gas.
　従来、有機溶剤を含有する被処理ガスに吸着材を用いて有機溶剤の吸着処理および脱着処理を行なって、有機溶剤を被処理ガスからキャリアガスに移動させることにより、被処理ガスの清浄化と有機溶剤の回収とを可能にした有機溶剤含有ガス処理システムが知られている。 Conventionally, an adsorbent is used to adsorb and desorb an organic solvent on a gas to be treated containing an organic solvent, and the organic solvent is moved from the gas to be treated to a carrier gas to purify the gas to be treated. An organic solvent-containing gas treatment system that enables recovery of an organic solvent is known.
　この種の有機溶剤回収システムは、一般に有機溶剤を含有する被処理ガスおよび高温の状態にあるキャリアガスを時間的に交互に吸着材に接触させる吸脱着処理装置と、当該吸脱着処理装置から排出されるキャリアガスを冷却することによって有機溶剤を凝縮させて回収する凝縮回収装置とを備えている。 This type of organic solvent recovery system generally includes an adsorption / desorption treatment device in which a gas to be treated containing an organic solvent and a carrier gas in a high temperature state are alternately brought into contact with the adsorbent in time, and the gas is discharged from the suction / desorption treatment device. It is equipped with a condensate recovery device that condenses and recovers the organic solvent by cooling the carrier gas.
　このような有機溶剤回収システムの一つとして、特許文献１には、キャリアガスとして水蒸気を使用した有機溶剤含有ガス処理システムが開示されている。 As one of such organic solvent recovery systems, Patent Document 1 discloses an organic solvent-containing gas treatment system using water vapor as a carrier gas.
　また、最近では回収した有機溶剤の高品質化や排水処理工程の簡略化を目的とした低排水量の有機溶剤回収システムが望まれており、特許文献２には、高温に間接加熱された吸着材にキャリアガスを供給する有機溶剤回収システムが開示されている。 Recently, there has been a demand for an organic solvent recovery system with a low amount of wastewater for the purpose of improving the quality of the recovered organic solvent and simplifying the wastewater treatment process. Patent Document 2 describes an adsorbent that is indirectly heated to a high temperature. An organic solvent recovery system that supplies carrier gas to the vehicle is disclosed.
日本国実用新案出願公報「実全平３－３２９２４」Japan Utility Model Application Bulletin "Jitsuzenpei 3-32924" 日本国公開特許公報「特開平７－６８１２７」Japanese Patent Publication "Japanese Patent Laid-Open No. 7-68127"
　このような有機溶剤回収システムにおいて、被処理ガスに対する浄化能力および有機溶剤の回収効率を向上させるためには、脱着処理における有機溶剤の脱着、すなわち吸着材の再生が、十分に行なわれることが必要になる。 In such an organic solvent recovery system, in order to improve the purification ability for the gas to be treated and the recovery efficiency of the organic solvent, it is necessary that the organic solvent is sufficiently desorbed in the desorption treatment, that is, the adsorbent is sufficiently regenerated. become.
　また、有機溶剤回収システムのランニングコストを抑制するためには、使用したキャリアガスを有機溶剤回収システム内で循環させて再利用するように構成することが好ましい。 Further, in order to suppress the running cost of the organic solvent recovery system, it is preferable to configure the carrier gas to be circulated and reused in the organic solvent recovery system.
　しかしながら、凝縮回収装置において有機溶剤をキャリアガスから完全に分離させることは困難である、そのため、凝縮回収装置から排出されるキャリアガスには、未凝縮の有機溶剤が含まれることになる。よって、キャリアガスを循環させて吸脱着処理装置に戻す構成の場合は吸着材の再生が不十分となる場合があり、被処理ガスに対する浄化能力および有機溶剤の回収効率に自ずと限界が生じるという問題があった。 However, it is difficult to completely separate the organic solvent from the carrier gas in the condensing recovery device. Therefore, the carrier gas discharged from the condensing recovery device contains an uncondensed organic solvent. Therefore, in the case of a configuration in which the carrier gas is circulated and returned to the adsorption / desorption treatment device, the regeneration of the adsorbent may be insufficient, and there is a problem that the purification capacity for the gas to be treated and the recovery efficiency of the organic solvent are naturally limited. was there.
　そこで、本発明は、上述した問題点を解決すべくなされ、ランニングコストが抑制できるとともに、被処理ガスの浄化能力および有機溶剤の回収効率の向上がなされた有機溶剤回収システムを提供することを目的とする。 Therefore, an object of the present invention is to provide an organic solvent recovery system in which the above-mentioned problems are solved, running costs can be suppressed, and the purification capacity of the gas to be treated and the recovery efficiency of the organic solvent are improved. And.
　本発明者は鋭意検討した結果、以下に示す手段により、上記課題を解決できることを見出し、本発明に到達した。すなわち、本発明は、以下の構成からなる。
１．有機溶剤を含有する被処理ガスから有機溶剤を分離して回収する有機溶剤回収システムであって、キャリアガスを循環通流させる循環経路と、吸脱着素子を有し、前記被処理ガスの導入による前記有機溶剤の吸着と、前記キャリアガスの導入による前記有機溶剤の脱着とを交互に行う吸脱着処理装置と、前記循環経路上で前記吸脱着処理装置の下流側に設けられ、当該吸脱着処理装置から排出された前記キャリアガスを冷却して当該キャリアガスに含有される有機溶剤を凝縮して回収する凝縮回収装置と、前記循環経路上で前記吸脱着処理装置の上流側に設けられ、前記凝縮回収装置から排出された低温状態の前記キャリアガスを加熱する加熱部と、を備え、前記凝縮回収装置は、当該凝縮回収装置から排出されるキャリアガスに含有される有機溶剤の蒸気圧が所定値以下となるように、当該凝縮回収装置から排出されるキャリアガスの温度を調節する、ことを特徴とする有機溶剤回収システム。
　上記構成によると、凝縮回収装置から排出されるキャリアガスに含有される有機溶剤の蒸気圧が所定値以下となるように温度調整することで、排出されるキャアリアガス中の有機溶剤の濃度を一定以下にすることができ、凝縮回収装置と吸脱着処理装置との間にキャリアガス中の有機溶剤を吸着除去するための別の吸着装置を設置する必要等がなくなる。よって、システムを簡素な構成にでき小型化できる。
２．前記凝縮回収装置から排出されるキャリアガスの温度を測定する温度測定手段を備え、前記凝縮回収装置は、前記温度測定手段の測定値を基に、前記水蒸気圧が所定値以下になるように、排出されるキャリアガスの温度を調節する上記１に記載の有機溶剤回収システム。
３．前記凝縮回収装置から排出されるキャリアガスの蒸気圧を測定する蒸気圧測定手段を備え、前記凝縮回収装置は、前記蒸気圧測定手段の測定値を基に、前記蒸気圧が所定値以下になるように、排出されるキャリアガスの温度を調節する上記１に記載の有機溶剤回収システム。
４．前記凝縮回収装置は、冷媒を用いた間接冷却によって前記キャリアガスを冷却する、上記１から３のいずれか１つに記載の有機溶剤回収システム。
５．前記冷媒は、水、エチレングリコール、プロピレングリコール、グリセリン、エタノールのいずれかまたはその混合物である、上記４に記載の有機溶剤回収システム。 As a result of diligent studies, the present inventor has found that the above problems can be solved by the means shown below, and has arrived at the present invention. That is, the present invention has the following configuration.
1. 1. It is an organic solvent recovery system that separates and recovers an organic solvent from a gas to be treated containing an organic solvent, and has a circulation path for circulating and passing a carrier gas and an adsorption / desorption element, and by introducing the gas to be treated. An adsorption / desorption treatment apparatus that alternately performs adsorption of the organic solvent and desorption of the organic solvent by introduction of the carrier gas, and an adsorption / desorption treatment provided on the downstream side of the adsorption / desorption treatment apparatus on the circulation path. A condensation recovery device that cools the carrier gas discharged from the device and condenses and recovers the organic solvent contained in the carrier gas, and a condensation recovery device provided on the upstream side of the adsorption / desorption treatment device on the circulation path. A heating unit for heating the carrier gas in a low temperature state discharged from the condensation recovery device is provided, and the condensation recovery device has a predetermined vapor pressure of an organic solvent contained in the carrier gas discharged from the condensation recovery device. An organic solvent recovery system characterized in that the temperature of the carrier gas discharged from the condensing recovery device is adjusted so as to be equal to or lower than the value.
According to the above configuration, the concentration of the organic solvent in the discharged carrier gas is kept below a certain level by adjusting the temperature 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. It is not necessary to install another adsorption device for adsorbing and removing the organic solvent in the carrier gas between the condensing recovery device and the adsorption / desorption treatment device. Therefore, the system can be made simple and miniaturized.
2. A temperature measuring means for measuring the temperature of the carrier gas discharged from the condensing recovery device is provided, and the condensing recovery device is provided so that the water vapor pressure becomes a predetermined value or less based on the measured value of the temperature measuring means. The organic solvent recovery system according to 1 above, which regulates the temperature of the discharged carrier gas.
3. 3. A vapor pressure measuring means for measuring the vapor pressure of the carrier gas discharged from the condensing recovery device is provided, and the condensing recovery device has the vapor pressure of a predetermined value or less based on the measured value of the vapor pressure measuring means. The organic solvent recovery system according to 1 above, which regulates the temperature of the discharged carrier gas.
4. The organic solvent recovery system according to 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 according to 4 above, wherein the refrigerant is water, ethylene glycol, propylene glycol, glycerin, ethanol, or a mixture thereof.
　本発明によれば、凝縮回収装置から排出されるキャリアガスに含有される有機溶剤の蒸気圧が所定値以下となるように温度調整することで、排出されるキャアリアガス中の有機溶剤の濃度を一定以下にすることができ、凝縮回収装置と吸脱着処理装置との間にキャリアガス中の有機溶剤を吸着除去するための別の吸着装置を設置する必要等がなく、浄化能力が保つことができる。よって、システムを簡素な構成にでき小型化できる。このように、本発明によれば、ランニングコストが抑制できるとともに、被処理ガスの浄化能力および有機溶剤の回収効率の向上が図られた有機溶剤回収システムを提供できる。 According to the present invention, the concentration of the organic solvent in the discharged carrier gas is kept constant by adjusting the temperature so that the vapor pressure of the organic solvent contained in the carrier gas discharged from the condensation recovery device becomes equal to or lower than a predetermined value. It is possible to do the following, and it is not necessary to install another adsorption device for adsorbing and removing the organic solvent in the carrier gas between the condensation recovery device and the adsorption / desorption treatment device, and the purification capacity can be maintained. .. Therefore, the system can be made simple and miniaturized. As described above, according to the present invention, it is possible to provide an organic solvent recovery system in which the running cost can be suppressed and the purification capacity of the gas to be treated and the recovery efficiency of the organic solvent are improved.
実施の形態における有機溶剤回収システムの構造を示す図である。It is a figure which shows the structure of the organic solvent recovery system in an embodiment. 実施の形態における有機溶剤回収システムにおいて、一対の吸脱着素子を用いた吸着処理および脱着処理の時間的な切り替えの様子を示すタイムチャートを示す図である。It is a figure which shows the state of temporal switching of the adsorption process and desorption process using a pair of adsorption / desorption elements in the organic solvent recovery system of embodiment.
　以下、本発明の実施の形態について、図を参照して詳細に説明する。なお、以下に示す実施の形態においては、同一のまたは共通する部分について図中同一の符号を付し、その説明は繰り返さない。 Hereinafter, embodiments of the present invention will be described in detail with reference to the drawings. In the embodiments shown below, the same or common parts are designated by the same reference numerals in the drawings, and the description thereof will not be repeated.
　図１に示すように、本実施の形態における有機溶剤回収システム１００Ａは、キャリアガスが循環するように通流される循環経路Ｌ１と、循環経路Ｌ１上に設けられた吸脱着処理装置１０、凝縮回収装置２０、循環送風機４０と、被処理ガス送風機５０とを備えている。キャリアガスとしては、水蒸気、加熱空気、高温に加熱した不活性ガス等、様々な種類のガスを使用することが可能である。特に水分を含まないガスである不活性ガスを使用すれば、有機溶剤回収システム１００Ａをより簡素に構成することができる。 As shown in FIG. 1, in the organic solvent recovery system 100A of the present embodiment, the circulation path L1 through which the carrier gas circulates, the adsorption / desorption treatment device 10 provided on the circulation path L1, and the condensation recovery A device 20, a circulation blower 40, and a gas blower 50 to be processed are provided. As the carrier gas, various types of gases such as steam, heated air, and an inert gas heated to a high temperature can be used. In particular, if an inert gas, which is a gas that does not contain water, is used, the organic solvent recovery system 100A can be configured more simply.
　循環経路Ｌ１は、図中に示す配管ラインＬ４～Ｌ７を備えている。循環送風機４０は、循環経路Ｌ１にキャリアガスを通流させるための送風手段であり、被処理ガス送風機５０は、配管ラインＬ２から吸脱着処置装置１０に被処理ガスを供給するための送風手段である。 The circulation path L1 includes piping lines L4 to L7 shown in the figure. The circulation blower 40 is a blowing means for passing the carrier gas through the circulation path L1, and the processed gas blower 50 is a blowing means for supplying the treated gas from the piping line L2 to the suction / desorption treatment device 10. is there.
　吸脱着処理装置１０は、吸脱着槽Ａ１１および吸脱着槽Ｂ１２と、温度調節手段であるヒーター３０とを備えている。吸脱着槽Ａ１１には有機溶剤を吸着および脱着する吸脱着素子Ａ１３が充填されており、吸脱着槽Ｂ１２には有機溶剤を吸着および脱着する吸脱着素子Ｂ１４が充填されている。本実施の形態では２つの吸脱着槽を備えているが、１であっても、３以上であってもよい。 The suction / desorption processing device 10 includes a suction / desorption tank A11 and a suction / desorption tank B12, and a heater 30 as a temperature controlling means. The adsorption / desorption tank A11 is filled with an adsorption / desorption element A13 that adsorbs and desorbs an organic solvent, and the adsorption / desorption tank B12 is filled with an adsorption / desorption element B14 that adsorbs and desorbs an organic solvent. In the present embodiment, two suction / detachment tanks are provided, but the number may be one or three or more.
　ヒーター３０は、吸脱着槽Ａ１１または吸脱着槽Ｂ１２に供給されるキャリアガスを高
温の状態に温度調節する。より具体的には、ヒーター３０は、凝縮回収装置２０から排出されて循環送風機４０を経由したキャリアガスを高温の状態に温度調節して吸脱着槽Ａ１１または吸脱着槽Ｂ１２に供給する。ここで、ヒーター３０は、吸脱着素子Ａ１３および吸脱着素子Ｂ１４が所定の脱着温度に維持されるように、吸脱着槽Ａ１１および吸脱着槽Ｂ１２に導入されるキャリアガスを温度調節する。 The heater 30 adjusts the temperature of the carrier gas supplied to the suction / desorption tank A11 or the suction / desorption tank B12 to a high temperature. More specifically, the heater 30 adjusts the temperature of the carrier gas discharged from the condensing recovery device 20 and passing through the circulation blower 40 to a high temperature state and supplies the carrier gas to the suction / desorption tank A11 or the suction / desorption tank B12. Here, the heater 30 adjusts the temperature of the carrier gas introduced into the suction / desorption tank A11 and the suction / desorption tank B12 so that the suction / desorption element A13 and the suction / desorption element B14 are maintained at a predetermined desorption temperature.
　吸脱着素子Ａ１３および吸脱着素子Ｂ１４は、被処理ガスを接触させることで被処理ガスに含有される有機溶剤を吸着する。したがって、脱着処理装置１０においては、吸脱着槽Ａ１１または吸脱着槽Ｂ１２に被処理ガスを供給すると、有機溶剤が吸脱着素子Ａ１３または吸脱着素子Ｂ１４に吸着されて被処理ガスから有機溶剤が除去されて被処理ガスが清浄化され、清浄ガスとして吸脱着槽Ａ１１または吸脱着槽Ｂ１２から排出される。 The adsorption / desorption element A13 and the adsorption / desorption element B14 adsorb the organic solvent contained in the gas to be treated by bringing them into contact with the gas to be treated. Therefore, in the desorption treatment device 10, when the gas to be treated is supplied to the suction / desorption tank A11 or the suction / desorption tank B12, the organic solvent is adsorbed by the suction / desorption element A13 or the suction / desorption element B14, and the organic solvent is removed from the gas to be treated. Then, the gas to be treated is purified and discharged as a clean gas from the suction / desorption tank A11 or the suction / desorption tank B12.
　また、吸脱着素子Ａ１３および吸脱着素子Ｂ１４は、高温の状態にあるキャリアガスを接触させることで吸着した有機溶剤を脱着する。したがって、吸脱着処理装置１０においては、吸脱着槽Ａ１１または吸脱着槽Ｂ１２に高温の状態にあるキャリアガスを供給すると、有機溶剤が吸脱着素子Ａ１３または吸脱着素子Ｂ１４から脱着され、有機溶剤を含有するキャリアガスが吸脱着槽Ａ１１または吸脱着槽Ｂ１２から排出される。 Further, the adsorption / desorption element A13 and the adsorption / desorption element B14 desorb the adsorbed organic solvent by contacting the carrier gas in a high temperature state. Therefore, in the suction / desorption treatment device 10, when the carrier gas in a high temperature state is supplied to the suction / desorption tank A11 or the suction / desorption tank B12, the organic solvent is desorbed from the suction / desorption element A13 or the suction / desorption element B14, and the organic solvent is desorbed. The contained carrier gas is discharged from the suction / desorption tank A11 or the suction / desorption tank B12.
　吸脱着素子Ａ１３および吸脱着素子Ｂ１４は、粒状活性炭、活性炭素繊維、ゼオライト、シリカゲル、多孔質性高分子および金属有機構造体のいずれかを含む吸着材にて構成される。好適には、粒状、粉体状、ハニカム状等の活性炭やゼオライトが利用されるが、より好適には、活性炭素繊維が利用される。活性炭素繊維は、表面にミクロ孔を有する繊維状構造を有しているため、ガスとの接触効率が高く、他の吸着材に比べて高い吸着効率および脱着効率を実現する。 The adsorption / desorption element A13 and the adsorption / desorption element B14 are composed of an adsorbent containing any one of granular activated carbon, activated carbon fiber, zeolite, silica gel, a porous polymer, and a metal-organic framework. Preferably, activated carbon or zeolite in the form of granules, powder, honeycomb or the like is used, but more preferably, activated carbon fiber is used. Since the activated carbon fiber has a fibrous structure having micropores on its surface, it has high contact efficiency with gas, and realizes higher adsorption efficiency and desorption efficiency than other adsorbents.
　吸脱着処理装置１０には、配管ラインＬ２，Ｌ３がそれぞれ接続されている。配管ラインＬ２は、被処理ガス送風機４０を経由して有機溶剤を含有する被処理ガスを吸脱着槽Ａ１１または吸脱着槽Ｂ１２に供給するための配管ラインである。配管ラインＬ２は、バルブＶ１によって吸脱着槽Ａ１１に対する接続／非接続状態が切り替えられ、バルブＶ３によって吸脱着槽Ｂ１２に対する接続／非接続状態が切り替えられる。配管ラインＬ３は、清浄ガスを吸脱着槽Ａ１１または吸脱着槽Ｂ１２から排出するための配管ラインである。配管ラインＬ３は、バルブＶ２によって吸脱着槽Ａ１１に対する接続／非接続状態が切り替えられ、バルブＶ４によって吸脱着槽Ｂ１２に対する接続／非接続状態が切り替えられる。 Piping lines L2 and L3 are connected to the suction / desorption processing device 10, respectively. The piping line L2 is a piping line for supplying the gas to be treated containing an organic solvent to the suction / desorption tank A11 or the suction / desorption tank B12 via the gas blower 40 to be treated. The valve V1 switches the connection / non-connection state of the piping line L2 to the suction / detachment tank A11, and the valve V3 switches the connection / non-connection state to the suction / detachment tank B12. The piping line L3 is a piping line for discharging clean gas from the suction / desorption tank A11 or the suction / desorption tank B12. In the piping line L3, the connection / non-connection state to the suction / detachment tank A11 is switched by the valve V2, and the connection / non-connection state to the suction / detachment tank B12 is switched by the valve V4.
　さらに、吸脱着処理装置１０には、配管ラインＬ５，Ｌ６がそれぞれ接続されている。
配管ラインＬ５は、キャリアガスをヒーター３０を介して吸脱着槽Ａ１１または吸脱着槽Ｂ１２に供給するための配管ラインである。配管ラインＬ５は、バルブＶ５によって吸脱着槽Ａ１１に対する接続／非接続状態が切り替えられ、バルブＶ７によって吸脱着槽Ｂ１２に対する接続／非接続状態が切り替えられる。配管ラインＬ６は、キャリアガスを吸脱着槽Ａ１１または吸脱着槽Ｂ１２から排出するための配管ラインである。配管ラインＬ６は、バルブＶ６よって吸着槽Ａ１１に対する接続／非接続状態が切り替えられ、Ｖ８によって吸脱着槽Ｂ１２に対する接続／非接続状態が切り替えられる。 Further, piping lines L5 and L6 are connected to the suction / desorption processing device 10, respectively.
The piping line L5 is a piping line for supplying the carrier gas to the suction / desorption tank A11 or the suction / desorption tank B12 via the heater 30. In the piping line L5, the connection / non-connection state to the suction / detachment tank A11 is switched by the valve V5, and the connection / non-connection state to the suction / detachment tank B12 is switched by the valve V7. The piping line L6 is a piping line for discharging the carrier gas from the suction / desorption tank A11 or the suction / desorption tank B12. The connection / non-connection state of the piping line L6 to the suction tank A11 is switched by the valve V6, and the connection / non-connection state to the suction / detachment tank B12 is switched by V8.
　吸脱着槽Ａ１１および吸脱着槽Ｂ１２のそれぞれには、上述したバルブＶ１～Ｖ８の開閉を操作することにより、被処理ガスと高温の状態にあるキャリアガスとが、時間的に交互に供給される。これにより、吸脱着槽Ａ１１および吸脱着槽Ｂ１２は、時間的に交互に吸着槽および脱着槽として機能することになり、これに伴って有機溶剤が被処理ガスから高温の状態にあるキャリアガスに移動する。なお、具体的には、吸脱着槽Ａ１１が吸着槽として機能している間には、吸脱着槽Ｂ１２が脱着槽として機能し、吸脱着槽Ａ１１が脱着槽として機能している間には、吸脱着槽Ｂ１２が吸着槽として機能する。 By operating the opening and closing of the valves V1 to V8 described above, the gas to be treated and the carrier gas in a high temperature state are alternately supplied to the suction / desorption tank A11 and the suction / desorption tank B12 in time. .. As a result, the suction / desorption tank A11 and the suction / desorption tank B12 alternately function as an adsorption tank and a desorption tank in time, and the organic solvent changes from the gas to be treated to the carrier gas in a high temperature state. Moving. Specifically, while the suction / desorption tank A11 functions as an adsorption tank, the suction / desorption tank B12 functions as a desorption tank, and while the suction / desorption tank A11 functions as a desorption tank, The suction / detachment tank B12 functions as a suction tank.
　凝縮回収装置２０は、コンデンサ（凝縮器）２１と、回収タンク２２とを備えている。コンデンサ２１は、吸脱着槽Ａ１１または吸脱着槽Ｂ１２から排出された高温の状態にあるキャリアガスを低温の状態に温度調節することによって、キャリアガスに含有される有機溶剤を凝縮させるものである。コンデンサ２１は、具体的には、冷媒を用いてキャリアガスを間接冷却することで有機溶剤を液化させる。回収タンク２２は、コンデンサ２１にて液化された有機溶剤を凝縮液として貯留するものである。 The condensation recovery device 20 includes a condenser (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 suction / desorption tank A11 or the suction / desorption tank B12 to a low temperature state. Specifically, the capacitor 21 liquefies the organic solvent by indirectly cooling the carrier gas with a refrigerant. The recovery tank 22 stores the organic solvent liquefied by the condenser 21 as a condensate.
　冷媒は、水、一級アルコール、二級アルコール、三級アルコール、ハイドロクロロフルオロカーボン類、ハイドロフルオロカーボン類、アンモニアのいずれかまたはそれらの混合物を用いることができるが、特に水、エチレングリコール、プロピレングリコール、グリセリン、エタノールのいずれかまたはその混合物を用いれば、有機溶剤回収システム１００Ａをより簡素に構成することができる。 As the refrigerant, any one of water, primary alcohol, secondary alcohol, tertiary alcohol, hydrochlorofluorocarbons, hydrofluorocarbons, ammonia or a mixture thereof can be used, and in particular, water, ethylene glycol, propylene glycol and glycerin can be used. , Ethanol, or a mixture thereof, can be used to construct the organic solvent recovery system 100A more simply.
　凝縮回収装置２０には、配管ラインＬ６，Ｌ７がそれぞれ接続されている。配管ラインＬ６は、吸脱着処理装置１０から排出されたキャリアガスをコンデンサ２１に供給すための配管ラインである。配管ラインＬ７は、キャリアガスをコンデンサ２１から排出するための配管ラインである。 Piping lines L6 and L7 are connected to the condensate recovery device 20, respectively. The piping line L6 is a piping line for supplying the carrier gas discharged from the suction / 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.
　また、コンデンサ２１には、配管ラインＬ９が接続されている。配管ラインＬ９は、コンデンサ２１で凝縮させた有機溶剤を回収タンク２２に導入するための配管ラインである。 Further, the piping line L9 is connected to the capacitor 21. The piping line L9 is a piping line for introducing the organic solvent condensed by the condenser 21 into the recovery tank 22.
　図２は、図１に示す有機溶剤回収システム１００Ａにおいて、吸脱着素子Ａ１３と吸着素子Ｂ１４とを用いた吸着処理および脱着処理の時間的な切り替えの様子を示すタイムチャートである。次に、この図２を参照して、本実施の形態における有機溶剤回収システム１００Ａを用いた被処理ガスの処理の詳細について、キャリアガスに不活性ガスを用いた場合を例にして説明する。 FIG. 2 is a time chart showing a state of temporal switching between the adsorption process and the adsorption process using the adsorption / desorption element A13 and the adsorption element B14 in the organic solvent recovery system 100A shown in FIG. Next, with reference to FIG. 2, the details of the treatment of the gas to be treated using the organic solvent recovery system 100A in the present embodiment will be described by taking the case where an inert gas is used as the carrier gas as an example.
　有機溶剤回収システム１００Ａは、図２に示す１サイクルを単位期間として当該サイクルが繰り返し実施さることにより、被処理ガスの処理が連続して行なわれるものである。 In the organic solvent recovery system 100A, the treatment of the gas to be treated is continuously performed by repeatedly carrying out the cycle with one cycle shown in FIG. 2 as a unit period.
　上記１サイクルの前半（図２中に示す時刻ｔ０～ｔ２の間）においては、吸脱着素子Ａ１３が充填された吸脱着処理装置１０の吸脱着槽Ａ１１において吸着処理が実施される。これと並行して、吸脱着素子Ｂ１４が充填された吸脱着処理装置１０の吸脱着槽Ｂ１２において吸脱着槽Ｂ１２内を不活性ガスで置換するパージ処理（図２中に示す時刻ｔ０～ｔ１の間）が実施された後、脱着処理（図２中に示す時刻ｔ１～ｔ２の間）が実施される。 In the first half of the above one cycle (between times t0 and t2 shown in FIG. 2), the adsorption treatment is carried out in the suction / desorption tank A11 of the suction / desorption processing device 10 filled with the suction / desorption element A13. In parallel with this, in the suction / desorption tank B12 of the suction / desorption processing device 10 filled with the suction / desorption element B14, a purge treatment is performed in which the inside of the suction / desorption tank B12 is replaced with an inert gas (at times t0 to t1 shown in FIG. 2). After that, the desorption process (between times t1 and t2 shown in FIG. 2) is carried out.
　また、上記１サイクルの後半（図２中に示す時刻ｔ２～ｔ４の間）においては、吸脱着素子Ｂ１４が充填された吸脱着処理装置１０の吸脱着槽Ｂ１２において吸着処理が実施され、これと並行して、吸脱着素子Ａ１３が充填された吸脱着処理装置１０の吸脱着槽Ａ１１において吸脱着槽Ａ１１内を不活性ガスで置換するパージ処理（図２中に示す時刻ｔ２～ｔ３の間）が実施された後、脱着処理（図２中に示す時刻ｔ３～ｔ４の間）が実施される。 Further, in the latter half of the above one cycle (between times t2 and t4 shown in FIG. 2), the adsorption treatment is carried out in the suction / desorption tank B12 of the suction / desorption processing device 10 filled with the suction / desorption element B14. At the same time, in the suction / desorption tank A11 of the suction / desorption processing device 10 filled with the suction / desorption element A13, a purge treatment for replacing the inside of the suction / desorption tank A11 with an inert gas (between times t2 and t3 shown in FIG. 2). Is carried out, and then the desorption process (between times t3 and t4 shown in FIG. 2) is carried out.
　凝縮回収装置２０において、吸脱着処理装置１０から排出された有機溶剤を含むキャリアガスをコンデンサ２１で間接冷却し、低温の状態に温度調節して有機溶剤を凝縮させ、有機溶剤が回収される。 In the condensation recovery device 20, the carrier gas containing the organic solvent discharged from the adsorption / desorption treatment 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.
　凝縮回収装置２０は、コンデンサ２１から排出されるキャリアガスに含有される有機溶剤の蒸気圧が所定値以下となるよう温度調整する。例えば、コンデンサ２１の温度を調節する温度調節部（図示しない）を有していてもよい。コンデンサ２１の温度を調節することで、排出されるキャリアガスに含有される有機溶剤の蒸気圧が所定値以下になり、よって、排出されるキャアリアガス中の有機溶剤の濃度を一定以下にすることができる。そのため、吸脱着素子に吸着した有機溶剤を効率よく脱着させることができる。
　例えば、後述の実施例のように、有機溶剤がｐ－キシレンである場合、凝縮処理において、コンデンサ２１から排出されるキャリアガスに含有される有機溶剤の蒸気圧が、１１．４ｍｍＨｇ以下となるようにキャリアガスを温度調節することが好ましく、さらに６．１ｍｍＨｇ以下となるようにキャリアガスを温度調整することがより好ましい。コンデンサ２１から排出されるキャリアガスに含有される有機溶剤の蒸気圧が１１．４ｍｍＨｇ以下の場合、循環して吸脱着素子Ａ１３および吸脱着素子Ｂ１４に接触させられるキャリアガスに含有される有機溶剤の蒸気圧もまた十分に低下するため、吸脱着素子Ａ１３および吸脱着素子Ｂ１４の再生が効果的に促進される。一方、コンデンサ２１から排出されるキャリアガスに含有される有機溶剤の蒸気圧が１１．４ｍｍＨｇを超える場合、循環して吸脱着素子Ａ１３および吸脱着素子Ｂ１４に接触させられるキャリアガスに含有される有機溶剤の蒸気圧もまた高値のため、吸脱着素子Ａ１３および吸脱着素子Ｂ１４の再生が十分に行われ難く、システムとして性能低下が生じる。この１１．４ｍｍＨｇ、６．１ｍｍＨｇという値は、後述の実施例における実験結果から導き出した値である。 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 is equal to or less than a predetermined value. For example, it may have a temperature control unit (not shown) that controls the temperature of the capacitor 21. By adjusting the temperature of the condenser 21, the vapor pressure of the organic solvent contained in the discharged carrier gas becomes a predetermined value or less, and thus the concentration of the organic solvent in the discharged carrier gas can be kept below a certain value. it can. Therefore, the organic solvent adsorbed on the adsorption / desorption element can be efficiently desorbed.
For example, when the organic solvent is p-xylene as in the examples described later, the vapor pressure of the organic solvent contained in the carrier gas discharged from the capacitor 21 is 11.4 mmHg or less in the condensation process. The temperature of the carrier gas is preferably adjusted, and more preferably the temperature of the carrier gas is adjusted to 6.1 mmHg or less. When the vapor pressure of the organic solvent contained in the carrier gas discharged from the condenser 21 is 11.4 mmHg or less, the organic solvent contained in the carrier gas circulated and brought into contact with the suction / desorption element A13 and the suction / desorption element B14. Since the vapor pressure is also sufficiently lowered, the regeneration of the suction / desorption element A13 and the suction / desorption element B14 is effectively promoted. On the other hand, when the vapor pressure of the organic solvent contained in the carrier gas discharged from the capacitor 21 exceeds 11.4 mmHg, the organic contained in the carrier gas circulated and brought into contact with the suction / desorption element A13 and the suction / desorption element B14. Since the vapor pressure of the solvent is also high, it is difficult for the adsorption / desorption element A13 and the adsorption / desorption element B14 to be sufficiently regenerated, resulting in deterioration of the performance of the system. The values of 11.4 mmHg and 6.1 mmHg are values derived from the experimental results in the examples described later.
　凝縮回収装置２０は、コンデンサ２１から排出されるキャリアガスに含有される有機溶剤の蒸気圧が所定値以下となるように温度調節することで、排出されるキャアリアガス中の有機溶剤の濃度を一定以下にすることができ、コンデンサ２１と吸脱着処理装置１０との間にキャリアガス中の有機溶剤を吸着除去するための別の吸着装置を設置する必要等がなくなり、有機溶剤回収システム１００Ａを簡素な構成にでき小型化できる。 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 is equal to or less than a predetermined value, so that the concentration of the organic solvent in the discharged carrier gas is below a certain level. It is not necessary to install another adsorption device for adsorbing and removing the organic solvent in the carrier gas between the capacitor 21 and the adsorption / desorption processing device 10, and the organic solvent recovery system 100A is simplified. It can be configured and miniaturized.
　また、凝縮回収装置２０は、コンデンサ２１から排出されるキャリアガスの温度を測定する温度測定器（図示無）を備えていてもよい。凝縮回収装置２０は、温度測定器の測定値を基に、キャリアガスに含有される有機溶剤の蒸気圧が所定値以下となるように、コンデンサ２１から排出されるキャリアガスの温度を調節すれば、有機溶剤回収システム１００Ａをより簡素に構成することができる。 Further, the condensation recovery device 20 may include a temperature measuring device (not shown) for measuring the temperature of the carrier gas discharged from the condenser 21. The condensate recovery device 20 can adjust 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 equal to or less than a predetermined value based on the measured value of the temperature measuring device. , The organic solvent recovery system 100A can be configured more simply.
　また、凝縮回収装置２０は、コンデンサ２１から排出されるキャリアガスの蒸気圧を測定する水蒸気圧測定器（図示無）を備えていてもよい。凝縮回収装置２０は、水蒸気圧測定器の測定値を基に、キャリアガスに含有される有機溶剤の蒸気圧が所定値以下となるようにコンデンサ２１から排出されるキャリアガスの温度を調節すれば、有機溶剤回収システム１００Ａをより簡素に構成することができる。キャリアガスの蒸気圧を測定する方法は水素炎イオン化検出法、触媒酸化―非分散赤外線吸収法、光イオン化検出法、半導体センサを用いた検出法、干渉増幅反射法、検知管を用いた検出法、などがあげられるが、特に限定されるものではない。 Further, the condensation recovery device 20 may include a vapor pressure measuring device (not shown) for measuring the vapor pressure of the carrier gas discharged from the condenser 21. The condensation recovery device 20 can adjust 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 equal to or less than a predetermined value based on the measured value of the water vapor pressure measuring device. , The organic solvent recovery system 100A can be configured more simply. The methods for measuring the vapor pressure of carrier gas are hydrogen flame ionization detection method, catalytic oxidation-non-dispersion infrared absorption method, photoionization detection method, detection method using semiconductor sensor, interference amplification reflection method, detection method using detector tube. , Etc., but are not particularly limited.
　以上において説明した本実施の形態の有機溶剤回収システム１００Ａを用いることにより、脱着処理において吸脱着素子Ａ１３および吸脱着素子Ｂ１４の再生が促進される結果となり、その後に実施される吸着処理の際により効率的に被処理ガスから有機溶剤を吸着除去できるようになる。従って、有機溶剤回収システム１００Ａを用いることで、被処理ガスに対する浄化能力および有機溶剤の回収効率の向上が図られ、従来に比して高性能かつ簡素な構成のシステムとすることができる。 By using the organic solvent recovery system 100A of the present embodiment described above, the regeneration of the adsorption / desorption element A13 and the adsorption / desorption element B14 is promoted in the desorption treatment, and the adsorption treatment performed thereafter The organic solvent can be efficiently adsorbed and removed from the gas to be treated. Therefore, by using the organic solvent recovery system 100A, the purification ability for the gas to be treated and the recovery efficiency of the organic solvent can be improved, and the system can have a higher performance and a simpler configuration than the conventional system.
　また、本実施の形態の有機溶剤回収システム１００Ａは、循環経路を構築することでキャリアガスを繰り返し使用できるため、経済性にも優れる。従って、窒素ガス等に代表される不活性ガスをキャリアガスとして使用した場合に、特にランニングコストを抑制できる効果が得られる。 Further, the organic solvent recovery system 100A of the present embodiment is excellent in economy because the carrier gas can be used repeatedly by constructing a circulation path. Therefore, when an inert gas such as nitrogen gas is used as the carrier gas, the effect of suppressing the running cost can be obtained.
　（実施例）
　以下の実施例では、上述した本発明の実施の形態における有機溶剤回収システム１００Ａを用いて被処理ガスの処理を行なった。 (Example)
In the following examples, the gas to be treated was treated using the organic solvent recovery system 100A according to the embodiment of the present invention described above.
　実施例においては、有機溶剤としてｐ－キシレンを１５００ｐｐｍの濃度で含有する４０℃、相対湿度５０％ＲＨのガスを被処理ガスとして使用した。キャリアガスとして１２０℃の窒素ガスを使用した。また、吸脱着素子Ａ１２，吸脱着素子Ｂ１４として、ＢＥＴ比表面積が１５００ｍｇ／ｍ２の活性炭素繊維を使用し、冷媒として５℃の水を使用した。 In the examples, a gas containing p-xylene at a concentration of 1500 ppm at 40 ° C. and a relative humidity of 50% RH as an organic solvent was used as the gas to be treated. Nitrogen gas at 120 ° C. was used as the carrier gas. Further, as the suction / desorption element A12 and the suction / desorption element B14, activated carbon fibers having a BET specific surface area of 1500 mg / m 2 were used, and water at 5 ° C. was used as a refrigerant.
　まず、被処理ガス送風機５０を用いて吸脱着処理装置１０の吸脱着槽Ａ１２および吸脱着槽Ｂ１３のうち一方の吸脱着槽に風量１０Ｎｍ３／ｍｉｎで１０分間送風することで上記一方の吸脱着槽を吸着槽として機能させ、吸着処理を実施した。 First, the suction / desorption tank A12 and the suction / desorption tank B13 of the suction / desorption treatment device 10 are blown at an air volume of 10 Nm 3 / min for 10 minutes by using the gas blower 50 to be treated. The tank was made to function as an adsorption tank, and the adsorption treatment was carried out.
　上記吸着処理の終了後に、バルブを切り替え操作し、上記一方の吸脱着槽を脱着槽に切り替えると共に、他方の吸脱着槽を吸着槽とした。脱着槽においては脱着槽内を窒素ガスで置換するパージ処理を行った後、ヒーター３０で１２０℃に加熱した窒素ガスを風量１．５Ｎｍ３／ｍｉｎで導入することで吸脱着素子の脱着処理を行った。吸着槽においては、上述した条件と同様の吸着処理を行った。凝縮回収装置２０では、コンデンサ２１に供給する冷媒量を調節し、脱着槽から排出されるｐ－キシレンを含有する窒素ガスの温度を１０℃に保った状態でｐ－キシレンを凝縮させ、回収タンク２２から回収した。 After the completion of the adsorption treatment, the valve was switched to switch one of the suction / detachment tanks to a desorption tank, and the other suction / desorption tank was used as a suction tank. In the desorption tank, after purging the inside of the desorption tank with nitrogen gas, nitrogen gas heated to 120 ° C. by the heater 30 is introduced at an air volume of 1.5 Nm 3 / min to desorb the suction / desorption element. went. In the adsorption tank, the adsorption treatment similar to the above-mentioned conditions was performed. In the condensation recovery device 20, the amount of refrigerant supplied to the condenser 21 is adjusted, and p-xylene is condensed while maintaining the temperature of the nitrogen gas containing p-xylene discharged from the desorption tank at 10 ° C., and the recovery tank is used. Recovered from 22.
　以上において説明した１サイクルを連続的に繰り返し実施したところ、吸脱着処理装置１０から排出される清浄ガスに含有されるｐ－キシレンの濃度が、約１０ｐｐｍにまで低減されていることが確認された。すなわち、実施例においては、約９９％の高い除去率でキシレンを除去できることが確認された。 When one cycle described above was continuously repeated, it was confirmed that the concentration of p-xylene contained in the clean gas discharged from the adsorption / desorption treatment device 10 was reduced to about 10 ppm. .. That is, in the examples, it was confirmed that xylene can be removed with a high removal rate of about 99%.
　また、上述した脱着処理において、凝縮回収装置２０に導入される部分の配管ラインＬ６を流通する窒素ガス中に含まれるｐ－キシレンの蒸気圧が平均１３．０ｍｍＨｇに上昇していることが確認され、凝縮回収装置２０から排出される部分の配管ラインＬ７を流通する窒素ガス中に含まれるｐ－キシレンの蒸気圧が常時３．６ｍｍＨｇにまで低下していることが確認された。本実施例は、冷媒の温度を変更して、配管ラインＬ７を流通する窒素ガス中に含まれるｐ－キシレンの蒸気圧が常時３．６ｍｍＨｇ以下となるよう、窒素ガスの温度を調整した。 Further, in the above-mentioned desorption treatment, it was confirmed that the vapor pressure of p-xylene contained in the nitrogen gas flowing through the piping line L6 of the portion introduced into the condensation recovery device 20 increased to an average of 13.0 mmHg. It was confirmed that the vapor pressure of p-xylene contained in the nitrogen gas flowing through the piping line L7 of the portion discharged from the condensate recovery device 20 was constantly reduced to 3.6 mmHg. In this embodiment, the temperature of the refrigerant was changed, and the temperature of the nitrogen gas was adjusted so that the vapor pressure of p-xylene contained in the nitrogen gas flowing through the piping line L7 was always 3.6 mmHg or less.
　以上に開示した実施の形態および実施例はすべての点で例示であって、制限的なものではない。本発明の技術的範囲は特許請求の範囲によって画定され、また特許請求の範囲の記載と均等の意味および範囲内でのすべての変更を含むものである。 The embodiments and examples disclosed above are examples in all respects and are not restrictive. The technical scope of the present invention is defined by the scope of claims and includes all modifications within the meaning and scope equivalent to the description of the scope of claims.
　本発明は、例えば工場やビルから排出される有機溶剤を含有する被処理ガスを処理するシステム等に有効に利用することができる。 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　　吸脱着処理装置
１１　　吸脱着槽Ａ
１２　　吸脱着槽Ｂ
１３　　吸脱着素子Ａ
１４　　吸脱着素子Ｂ
２０　　凝縮回収装置
２１　　コンデンサ
２２　　回収タンク
３０　　ヒーター
４０　　循環送風機
５０　　被処理ガス送風機
１００Ａ　　有機溶剤回収システム
Ｌ１　　循環経路
Ｌ２～Ｌ１１　　配管ライン
Ｖ１～Ｖ８　　バルブ
 
  10 Adsorption / desorption processing device 11 Adsorption / desorption tank A
12 Adsorption tank B
13 Adsorption element A
14 Adsorption element B
20 Condensation recovery device 21 Condenser 22 Recovery tank 30 Heater 40 Circulation blower 50 Processed gas blower 100A Organic solvent recovery system L1 Circulation path L2 to L11 Piping line V1 to V8 Valve

Claims (5)

  1. 　有機溶剤を含有する被処理ガスから有機溶剤を分離して回収する有機溶剤回収システムであって、
    　キャリアガスを循環通流させる循環経路と、
    　吸脱着素子を有し、前記被処理ガスの導入による前記有機溶剤の吸着と、前記キャリアガスの導入による前記有機溶剤の脱着とを交互に行う吸脱着処理装置と、
    　前記循環経路上で前記吸脱着処理装置の下流側に設けられ、当該吸脱着処理装置から排出された前記キャリアガスを冷却して当該キャリアガスに含有される有機溶剤を凝縮して回収する凝縮回収装置と、
    　前記循環経路上で前記吸脱着処理装置の上流側に設けられ、前記凝縮回収装置から排出された低温状態の前記キャリアガスを加熱する加熱部と、を備え、
    　前記凝縮回収装置は、当該凝縮回収装置から排出されるキャリアガスに含有される有機溶剤の蒸気圧が所定値以下となるように、当該凝縮回収装置から排出されるキャリアガスの温度を調節する、ことを特徴とする有機溶剤回収システム。     An organic solvent recovery system that separates and recovers an organic solvent from a gas to be treated containing an organic solvent.
    Circulation route for circulating carrier gas and
    An adsorption / desorption treatment device having an adsorption / desorption element that alternately adsorbs the organic solvent by introducing the gas to be treated and desorbs the organic solvent by introducing the carrier gas.
    Condensation recovery provided on the downstream side of the suction / desorption treatment device on the circulation path to cool the carrier gas discharged from the suction / desorption treatment device to condense and recover the organic solvent contained in the carrier gas. With the device
    A heating unit provided on the upstream side of the suction / desorption treatment device on the circulation path and heating the carrier gas in a low temperature state discharged from the condensation recovery device is provided.
    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. An organic solvent recovery system characterized by this.
  2. 　前記凝縮回収装置から排出されるキャリアガスの温度を測定する温度測定手段を備え、
    　前記凝縮回収装置は、前記温度測定手段の測定値を基に、前記水蒸気圧が所定値以下になるように、排出されるキャリアガスの温度を調節する請求項１に記載の有機溶剤回収システム。     A temperature measuring means for measuring the temperature of the carrier gas discharged from the condensing recovery device is provided.
    The organic solvent recovery system according to claim 1, wherein the condensation recovery device adjusts the temperature of the discharged carrier gas so that the water vapor pressure becomes a predetermined value or less based on the measured value of the temperature measuring means.
  3. 　前記凝縮回収装置から排出されるキャリアガスの蒸気圧を測定する蒸気圧測定手段を備え、
    　前記凝縮回収装置は、前記蒸気圧測定手段の測定値を基に、前記蒸気圧が所定値以下になるように、排出されるキャリアガスの温度を調節する請求項１に記載の有機溶剤回収システム。     A vapor pressure measuring means for measuring the vapor pressure of the carrier gas discharged from the condensing recovery device is provided.
    The organic solvent recovery system according to claim 1, wherein the condensation recovery device adjusts the temperature of the discharged carrier gas so that the vapor pressure becomes a predetermined value or less based on the measured value of the vapor pressure measuring means. ..
  4. 　前記凝縮回収装置は、冷媒を用いた間接冷却によって前記キャリアガスを冷却する、請求項１から３のいずれか1項に記載の有機溶剤回収システム。 The organic solvent recovery system according to any one of claims 1 to 3, wherein the condensation recovery device cools the carrier gas by indirect cooling using a refrigerant.
  5. 前記冷媒は、水、エチレングリコール、プロピレングリコール、グリセリン、エタノールのいずれかまたはその混合物である、請求項４に記載の有機溶剤回収システム。
     
          The organic solvent recovery system according to claim 4, wherein the refrigerant is water, ethylene glycol, propylene glycol, glycerin, ethanol, or a mixture thereof.
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JP2015000381A (en) * 2013-06-17 2015-01-05 東洋紡株式会社 Organic solvent recovery system
JP2016195969A (en) * 2015-04-03 2016-11-24 東洋紡株式会社 Organic solvent recovery system

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JPH0332924A (en) 1989-06-30 1991-02-13 Suzuki Motor Corp Air conditioner
JPH0768127A (en) 1993-06-15 1995-03-14 Toho Kako Kensetsu Kk Hot-air desorption type solvent recovering device
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JPH02129240U (en) * 1989-03-29 1990-10-24
JPH119952A (en) * 1997-06-18 1999-01-19 Toyo Eng Works Ltd Solvent recovery apparatus
JP2015000381A (en) * 2013-06-17 2015-01-05 東洋紡株式会社 Organic solvent recovery system
JP2016195969A (en) * 2015-04-03 2016-11-24 東洋紡株式会社 Organic solvent recovery system

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