WO2024070944A1 - Organic solvent recovery system - Google Patents

Organic solvent recovery system Download PDF

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Publication number
WO2024070944A1
WO2024070944A1 PCT/JP2023/034491 JP2023034491W WO2024070944A1 WO 2024070944 A1 WO2024070944 A1 WO 2024070944A1 JP 2023034491 W JP2023034491 W JP 2023034491W WO 2024070944 A1 WO2024070944 A1 WO 2024070944A1
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Prior art keywords
desorption
organic solvent
heat exchanger
gas
steam
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PCT/JP2023/034491
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French (fr)
Japanese (ja)
Inventor
武将 岡田
敏明 林
啓太郎 幸田
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東洋紡エムシー株式会社
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Publication of WO2024070944A1 publication Critical patent/WO2024070944A1/en

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    • 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

Definitions

  • the present invention relates to an organic solvent recovery system.
  • the organic solvent recovery system is equipped with a pair of treatment tanks that use an adsorbent to adsorb the organic solvents in the gas to be treated, a treatment gas supply device and a desorption gas supply device for each treatment tank, and employs a mechanism for switching between an adsorption process that supplies the gas to be treated to the treatment tank, and a desorption process that supplies the desorption gas.
  • Activated carbon fibers are used as adsorbents in gas treatment devices.
  • Activated carbon fibers have excellent ability to adsorb low-concentration organic solvent-containing gases and are used as adsorbents.
  • JP 2014-147864 A discloses a gas treatment device in which activated carbon fibers are fixed to a support or self-supported into a cylindrical shape and arranged vertically within a core material.
  • Patent Document 2 discloses an activated carbon desorption device that reduces the amount of water vapor used by connecting the condensation side of a heat exchanger to the desorption steam outlet of an activated carbon adsorber (treatment tank), supplying water to the evaporation side of the heat exchanger, and installing a pressure reducing blower in the line connecting the evaporation side of the heat exchanger to the desorption water vapor inlet of the activated carbon adsorber, and evaporating the water on the evaporation side using the heat of the desorption steam to generate water vapor for desorption.
  • JP 2014-147864 A Japanese Utility Model Application Publication No. 58-161636
  • the temperature of the desorption gas discharged from the treatment tank changes from time to time due to fluctuations in the outside air temperature, the organic solvent concentration in the gas being treated, the humidity of the gas being treated, and other factors. Therefore, when generating desorption water vapor using the heat of the desorption gas via a heat exchanger as in Patent Document 2, there is a risk that the flow rate of the desorption water vapor cannot be sufficiently secured.
  • the present invention aims to provide an organic solvent recovery system that has a mechanism for generating desorption steam using the heat of the desorption gas, ensures a sufficient flow rate of the desorption steam supplied to the treatment tank, and improves the efficiency of organic solvent recovery.
  • the organic solvent recovery system of the present invention has the following configuration.
  • an organic solvent recovery apparatus including a treatment tank containing an adsorbent that adsorbs and removes an organic solvent from a gas to be treated that contains the organic solvent, and repeats an adsorption process in which the gas to be treated that is supplied to the treatment tank is brought into contact with the adsorbent to discharge a treated gas, and a desorption process in which the organic solvent is desorbed from the adsorbent by a desorption steam supplied to the treatment tank and a desorbed gas is discharged; a heat exchanger including a heat generating section through which the desorption gas discharged from the organic solvent recovery apparatus passes and an endothermic section to which makeup water is replenished, the heat exchanger indirectly heating the makeup water of the endothermic section with the desorption gas passing through the heat generating section to generate steam, and discharging the indirectly heated desorption gas; a cooling unit that cools the desorption gas discharged from the heat exchanger and discharges a condensate, A water vapor supply unit that supplies water vapor to the heat
  • the organic solvent recovery system may include a pressure measuring unit that measures the pressure of the gas phase of the heat absorption section of the heat exchanger, and may control the flow rate of water vapor supplied from the water vapor supply unit to the heat exchanger based on the measurement results of the pressure measuring unit.
  • the water vapor supply unit may supply water vapor to the heat exchanger in the early stage of the desorption process, and may not supply water vapor to the heat exchanger in the later stage of the desorption process.
  • the organic solvent recovery device may include a condensate reservoir that accumulates the condensate discharged from the cooling section
  • the heat exchanger may include a desorption gas outlet receiving section in which the desorption gas accumulates after indirect heating, a piping path that supplies the uncondensed desorption gas from the desorption gas outlet receiving section to the cooling section, and a piping path that supplies the desorption gas that has become condensed from the desorption gas outlet receiving section to the condensate reservoir.
  • the organic solvent recovery system may include a path for supplying the desorption gas discharged from the treatment tank to the heat exchanger, and a path for supplying the desorption gas discharged from the treatment tank to the cooling section.
  • the organic solvent recovery system described above may supply the desorption gas discharged from the treatment tank to the cooling section and supply water vapor from the water vapor supply section to the heat absorption section of the heat exchanger in the early stage of the desorption process, and may supply the desorption gas discharged from the treatment tank to the heat generation section of the heat exchanger in the later stage of the desorption process, without having to supply water vapor from the water vapor supply section to the heat absorption section of the heat exchanger.
  • the heat exchanger may be a multi-tube heat exchanger having a tube section inside a container section.
  • the water vapor supply unit may be connected to or may share a desorption water vapor supply unit that directly supplies the desorption water vapor to the organic solvent recovery device.
  • an organic solvent recovery system that has a mechanism for generating desorption steam using the heat of the desorption gas, ensures a sufficient flow rate of the desorption steam supplied to the treatment tank, and improves the efficiency of organic solvent recovery.
  • FIG. 1 is a conceptual diagram showing a configuration of an organic solvent recovery system in a first embodiment.
  • FIG. 11 is a conceptual diagram showing the configuration of an organic solvent recovery system in a second embodiment.
  • 10 is a time chart showing the time-dependent switching between an adsorption process and a desorption process of an organic solvent recovery apparatus in accordance with the second embodiment;
  • organic solvents include methylene chloride, chloroform, carbon tetrachloride, ethylene chloride, trichloroethylene, tetrachloroethylene, o-dichlorobenzene, m-dichlorobenzene, fluorocarbon-112, fluorocarbon-113, HCFC, HFC, propyl bromide, butyl iodide, methyl acetate, ethyl acetate, propyl acetate, butyl acetate, vinyl acetate, methyl propionate, methyl acrylate, ethyl acrylate, butyl acrylate, methyl methacrylate, diethyl carbonate, ethyl formate, diethyl ether, dipropyl ether, tetrahydrofuran, dibutyl ether, anisole, methanol, ethanol, isopropanol, n-butanol, 2-butanol, isobutan
  • FIG. 1 is a diagram showing the configuration of an organic solvent recovery system 1A according to the first embodiment.
  • the organic solvent recovery system 1A includes an organic solvent recovery device 100, a heat exchanger 115, and a condenser 111 as a cooling section.
  • the organic solvent recovery apparatus 100 includes a first treatment tank 104A and a second treatment tank 104B.
  • the first treatment tank 104A includes a cylindrical first adsorbent 105A
  • the second treatment tank 104B includes a cylindrical second adsorbent 105B.
  • the first adsorbent 105A and the second adsorbent 105B are passed from the outside to the inside to perform an adsorption process (adsorption process), and water vapor is passed from the inside to the outside to perform a desorption process (desorption process).
  • activated carbon fiber or activated carbon is used for the first adsorbent 105A and the second adsorbent 105B.
  • the first treatment tank 104A and the second treatment tank 104B are connected to the treated gas inlet line 103 and the desorption gas line 110.
  • the first treatment tank 104A and the second treatment tank 104B are provided with a first lower damper 107A and a second lower damper 107B, respectively, to open and close the connection to the treated gas inlet line 103 and the connection to the desorption gas line 110.
  • a first upper damper 106A and a second upper damper 106B that control the flow of the gas I to be treated are provided above the first treatment tank 104A and the second treatment tank 104B, respectively.
  • a heat exchanger 115 is connected to the desorption gas line 110.
  • the heat exchanger 115 has a desorption gas inlet chamber 115C to which the desorption gas line 110 is connected.
  • the heat exchanger 115 also has a desorption gas outlet chamber 115D, which is a desorption gas outlet receiving section to which a heat exchanger outlet gas line 117 and a heat exchanger condensate line 118 are connected.
  • makeup water VI is supplied to the makeup water storage section 115E.
  • the makeup water VI is sent to the makeup water storage section 115E, for example, by a liquid delivery pump or the like.
  • the heat exchanger 115 indirectly heats the make-up water VI in the make-up water storage section 115E with the desorption gas supplied from the desorption gas line 110, thereby evaporating the make-up water VI and generating water vapor.
  • the make-up water storage section 115E is decompressed so that the boiling point is, for example, 70°C to 97°C, preferably 75°C to 95°C, and the generated water vapor is supplied to the steam compressor 122 as regenerated water vapor through the regenerated water vapor line 119 connected to the heat exchanger 115.
  • the steam compressor 122 is a mechanism that uses high-pressure water vapor as a driving source (hereinafter, driving water vapor) to draw in constant-pressure water vapor (hereinafter, sucked water vapor) in a reduced pressure state and increase the pressure to medium-pressure water vapor (hereinafter, discharged water vapor).
  • high-pressure water vapor VIII (a part of water vapor V) is supplied to the steam compressor 122 as driving water vapor through the steam compressor water vapor line 121, so that the regenerated water vapor is sucked in as sucked water vapor through the regenerated water vapor line 119, and the desorption water vapor, which is a mixture of water vapor VIII and regenerated water vapor, is discharged as discharged water vapor through the desorption water vapor line 108.
  • the desorption steam discharged from the steam compressor 122 is supplied to the first treatment tank 104A and the second treatment tank 104B where the desorption process is being carried out through the desorption steam line 108.
  • the steam compressor 122 may be replaced by a compressor having a similar effect, such as a roots blower or a turbo blower.
  • the makeup water storage section 115E is connected to a heat exchanger steam supply line 120, which is a steam supply section for supplying steam VII, which is a part of the steam V.
  • a heat exchanger steam supply line 120 which is a steam supply section for supplying steam VII, which is a part of the steam V.
  • the makeup water storage section 115E can be kept at a predetermined pressure or higher (for example, a gauge pressure of -0.099 MPa or higher), and the flow rate of the suction steam sucked into the steam compressor 122, i.e., the regenerated steam, can be sufficiently ensured.
  • the flow rate of the discharge steam of the steam compressor 122 i.e., the desorption steam
  • the desorption efficiency of the organic solvent in the desorption process of the organic solvent recovery device 100 can be maintained high.
  • the makeup water VI in the heat exchanger 115 body and the makeup water storage section 115E can be maintained at a high temperature, and the makeup water VI can be efficiently evaporated.
  • the makeup water storage section 115E is provided with a pressure sensor 115F, which is a pressure measuring section that measures the pressure inside the heat exchanger 115.
  • an adjustment valve V4 is provided on the heat exchanger steam supply line 120 to adjust the flow rate of the steam VII.
  • the heat exchanger 115 is provided with a control unit 115G that adjusts the flow rate of the water vapor VII. Specifically, the control unit 115G adjusts the opening of the adjustment valve V4 to supply the water vapor VII so that the pressure of the makeup water storage unit 115E detected by the pressure sensor 115F is maintained within a predetermined range (approximately -0.099 to -0.080 MPa in gauge pressure).
  • the heat exchanger 115 is a multi-tube heat exchanger.
  • a multi-tube heat exchanger is a heat exchanger in which a large number of tubes are arranged inside a cylinder called a shell, which is a container part.
  • the surface of the tubes acts as a heat transfer surface, and heat is exchanged between the fluid flowing inside the tube 115B (hereinafter, the tube side) and the fluid flowing between the outside of the tube 115B and the inside of the shell 115A (hereinafter, the shell side).
  • the tube 115B is a heat generating part that provides heat
  • the shell 115A is a heat absorbing part that receives heat.
  • the tube 115B connects the desorption gas inlet chamber 115C and the desorption gas outlet chamber 115D.
  • the heat exchanger 115 of the present invention is arranged so that the tube 115B faces horizontally, and the tube side acts as a condensation side that supplies the desorption gas, and the shell side acts as an evaporation side that supplies makeup water VI and steam VII.
  • makeup water VI In shell 115A, makeup water VI always remains in an amount that contacts a portion of tube 115B. When makeup water VI comes into contact with tube 115B, makeup water VI receives heat from the desorbed gas and evaporates. In addition, tube 115B also serves to heat makeup water up to the evaporation temperature, so there is no need to provide a separate makeup water heating facility to heat makeup water VI.
  • the heat exchanger 115 preferably adjusts the water level of the make-up water VI so that a portion of the tube 115B does not come into contact with the make-up water VI in the make-up water storage section 115E. Specifically, a portion of the tube 115B is located in the gas phase portion of the shell 115A between the water level of the make-up water VI and the regenerated steam line 119. The regenerated steam is heated by the tube 115B located in the gas phase portion of the shell 115A, and this prevents the regenerated steam from condensing before being sucked into the steam compressor 122.
  • possible means for adjusting the water level of the make-up water VI include, for example, a control method using a float type, a spacer type, a differential pressure type, or a capacitance type liquid level gauge.
  • the desorbed gas outlet chamber 115D of the heat exchanger 115 is connected to the heat exchanger outlet gas line 117 and is connected to the condenser 111. Inside the condenser 111, heat exchange occurs between the desorbed gas that has completed heat exchange in the heat exchanger 115 and the cooling water, and the desorbed gas is cooled and condensed.
  • the condensate condensed in the condenser 111 is supplied to the separator 113, which is a condensate reservoir, through the condenser condensate line 112.
  • the separator 113 separates the condensate sent from the condenser condensate line 112 into a layer of recovered solvent 113A and a layer of separated wastewater 113B.
  • the separated wastewater 113B may be aerated in an aeration device before being discharged.
  • a heat exchanger condensate line 118 is connected to the desorption gas outlet chamber 115D of the heat exchanger 115.
  • the heat exchanger condensate line 118 is connected to the separator 113.
  • the desorption gas is separated into uncondensed desorption gas and condensed condensate, and supplied to the desorption gas outlet chamber 115D.
  • the condensate of the desorption gas supplied to the desorption gas outlet chamber 115D is supplied directly to the separator 113 through the heat exchanger condensate line 118.
  • a return gas line 114 is connected to the gas phase portion of the condenser 111 and the gas phase portion of the separator 113.
  • the return gas line 114 is introduced into the treated gas line 101.
  • the gas returned from the return gas line 114 to the treated gas line 101 is preferably introduced so as to flow in a counter flow direction to the flow direction of the treated gas I.
  • the treated gas line 101 is provided with a treated gas blower 102.
  • the treated gas I delivered by the treated gas blower 102 is sent through the treated gas introduction line 103 to the first treatment tank 104A and the second treatment tank 104B.
  • the discharged water vapor from the steam compressor 122 i.e., the desorption water vapor
  • the desorption water vapor line 108 is connected to the first treatment tank 104A, and the desorption water vapor line 108 is provided with a first water vapor on-off valve V1.
  • the desorption water vapor line 108 is connected to the second treatment tank 104B, and the desorption water vapor line 108 is provided with a second water vapor on-off valve V2.
  • the first upper damper 106A, the second upper damper 106B, the first lower damper 107A, the second lower damper 107B, the first steam on-off valve V1, the second steam on-off valve V2, the heat exchanger 115, the steam compressor 122, the condenser 111, the separator 113, and the treated gas blower 102 are appropriately controlled in operation and opening/closing by a control device (not shown) to realize the gas treatment method described below.
  • FIG. 1 A gas treatment method using the organic solvent recovery apparatus 100 having the above-mentioned configuration will be described below.
  • the first treatment tank 104A of the organic solvent recovery apparatus 100 is used for a desorption process
  • the second treatment tank 104B is used for an adsorption process.
  • the treated gas I containing an organic solvent-containing gas is sent from the treated gas line 101 to the second treatment tank 104B, which is in an adsorption process, by the treated gas blower 102.
  • the second lower damper 107B is controlled to open the treated gas inlet line 103 and close the desorption gas line 110.
  • the second upper damper 106B is controlled to an open state that allows the gas I to flow through the second adsorbent 105B.
  • the organic solvent is adsorbed in the second adsorbent 105B of the second treatment tank 104B, and the treated gas II is discharged outside the system.
  • the second steam opening/closing valve 109V2 of the desorption water vapor line 108 is controlled to a closed state.
  • the gas I to be treated is not sent to the first treatment tank 104A, and the first lower damper 107A controls the gas to be treated introduction line 103 to be closed and the desorption gas line 110 to be open.
  • the first lower damper 107A blocks the flow of gas from the outside to the inside of the first adsorbent 105A.
  • the water vapor for desorption is introduced through the water vapor line 108 for desorption so as to be able to flow from the inside to the outside of the first adsorbent 105A.
  • the first water vapor on-off valve V1 of the water vapor line 108 for desorption is controlled to be open.
  • Steam for desorption is generated by mixing steam VIII and regenerated steam in the steam compressor 122.
  • Steam VIII is a part of steam V.
  • the steam compressor 122 is driven by steam VIII supplied through steam line 121 for the steam compressor, sucks in regenerated steam in a reduced pressure state through regenerated steam line 119, and discharges desorption steam, which is a mixture of steam VIII and regenerated steam, through steam line 108 for desorption.
  • the desorption water vapor is ejected, and the organic solvent adsorbed in the first adsorbent 105A is desorbed from the first adsorbent 105A.
  • the desorption gas which is a mixture of the desorbed organic solvent and water vapor, is sent to the heat exchanger 115 through the desorption gas line 110.
  • the desorbed gas is supplied to the tube side of the heat exchanger 115 and exchanges heat with the make-up water VI that is retained on the shell side of the heat exchanger 115. Specifically, the make-up water VI is indirectly heated through the heat transfer surface.
  • the desorption gas After the desorption gas has completed heat exchange with makeup water VI in heat exchanger 115, it is separated into uncondensed desorption gas and condensed condensate.
  • the uncondensed desorption gas is supplied to condenser 111 through heat exchanger outlet gas line 117. Inside condenser 111, heat exchange occurs between the desorption gas and cooling water, and the desorption gas is cooled and condensed. Meanwhile, the condensate of the desorption gas condensed in heat exchanger 115 is supplied to separator 113 through heat exchanger condensate line 118.
  • the condensate of the desorbed gas condensed in the condenser 111 is supplied to the separator 113 through the condenser condensate line 112. In the separator 113, it is separated into a layer of recovered solvent 113A and a layer of separated wastewater 113B.
  • the return gas remaining in the condenser 111 and separator 113 is pushed out by the desorbed gas and introduced into the treated gas line 101 through the return gas line 114, where it is mixed with the treated gas I.
  • the treated gas I and the return gas introduced from the treated gas line 101 are sent to the second treatment tank 104B.
  • the flow rate of the regenerated water vapor sucked into the steam compressor 122 is not insufficient even when the evaporation amount of the makeup water VI fluctuates, and the desorption process of the first treatment tank 104A is efficiently performed.
  • the heat of the desorption steam supplied to the first treatment tank 104A is consumed in large amounts to heat the first adsorbent 105A, the first treatment tank 104A body, the first upper damper 106A, the first lower damper 107A, and each piping line, so the temperature of the desorbed gas discharged from the first treatment tank 104A is low.
  • steam VII is supplied to the shell side of the heat exchanger 115 in the early stage of the desorption process and controlled so that steam VII is not supplied to the shell side of the heat exchanger 115 in the later stage of the desorption process when the desorbed gas discharged from the first treatment tank 104A reaches a high temperature (approximately 70 to 120°C), it is preferable because this ensures a sufficient flow rate of regenerated steam in the early stage of the desorption process and reduces the amount of steam VII used.
  • the organic solvent recovery device 100 continuously recovers the recovered solvent 113A through continuous processing in which the adsorption process and the desorption process are alternately performed.
  • FIG. 2 is a diagram showing the configuration of an organic solvent recovery system 1B according to the second embodiment.
  • the organic solvent recovery system 1B includes an on-off valve V3 and a condenser line 116 in addition to the configuration of the organic solvent recovery system 1A described in the first embodiment.
  • FIG. 3 is a time chart showing the time-dependent switching between the adsorption process and the desorption process of the organic solvent recovery apparatus 100 of the second embodiment shown in FIG. 2.
  • the method of recovering the organic solvent by the organic solvent recovery apparatus 100 of the second embodiment will be described with reference to FIG. 3.
  • the basic configuration of the organic solvent recovery system 1B of the second embodiment is the same as that of the organic solvent recovery system 1A described in the first embodiment above. The difference is that in the organic solvent recovery system 1B of the second embodiment, a three-way open/close valve V3 is provided on the desorption gas line 110 from the organic solvent recovery device 100. One downstream end of the open/close valve V3 is connected to the desorption gas inlet chamber 115C of the heat exchanger 115, and the other downstream end is connected to the condenser 111 via the condenser line 116.
  • the open/close valve V3 can be used to switch between supplying the desorption gas to the heat exchanger 115 or to the condenser 111. Note that a similar switching operation may be performed by using multiple two-way open/close valves instead of the three-way open/close valve V3.
  • the desorption process is divided into a first desorption process in the early stage and a second desorption process in the later stage.
  • the desorption gas is supplied to the condenser 111 through the condenser line 116 by operating the three-way opening and closing valve V3.
  • the heat of the desorption steam supplied to the first treatment tank 104A is largely consumed in heating the first adsorbent 105A, the first treatment tank 104A main body, the first upper damper 106A, the first lower damper 107A, and each piping line, so that the temperature of the desorption gas discharged from the first treatment tank 104A is low. Therefore, by supplying the desorbed gas discharged from the first treatment tank 104A directly to the condenser 111 instead of to the heat exchanger 115, the tube 115B of the heat exchanger 115 can be maintained at a high temperature, resulting in efficient evaporation of the makeup water VI.
  • the three-way open/close valve V3 is operated to supply the desorption gas to the heat exchanger 115, and the second desorption step of the first treatment tank 104A (i.e., between t1 and t2 shown in Figure 3) begins.
  • the timing for switching from the first desorption process to the second desorption process may be determined by measuring in advance the time it takes for the temperature of the desorption gas discharged from the treatment tank to reach a high temperature in the first desorption process.
  • a temperature sensor may be provided to measure the temperature of the desorption gas discharged from the treatment tank, and the process may be controlled to automatically switch from the first desorption process to the second desorption process when the temperature of the desorption gas detected by the temperature sensor reaches a high temperature.
  • steam VII is supplied to the shell side of the heat exchanger 115, and in the second desorption step, steam VII is controlled not to be supplied to the shell side of the heat exchanger 115, which is preferable because it ensures a sufficient flow rate of regenerated steam in the early stage of the desorption step and reduces the amount of steam VII used.
  • the organic solvent recovery system 1B of the second embodiment can achieve the same effects as the organic solvent recovery system 1A of the first embodiment.
  • the organic solvent recovery process is described as using a first treatment tank 104A and a second treatment tank 104B as treatment tanks, and alternately performing an adsorption process and a desorption process.
  • the organic solvent recovery process is not limited to using these two treatment tanks, and there may be three or more treatment tanks.
  • Example> The following treatment was carried out using the organic solvent recovery system 1A shown in Fig. 1 described above.
  • the gas to be treated was 45°C containing 2,000 ppm of toluene and had an air volume of 7 Nm3 /min, and was blown into the second treatment tank 104B, which was in the adsorption process, by the gas to be treated blower 102.
  • 4 kg of activated carbon fiber manufactured by Toyobo Co., Ltd. was used for each of the first adsorbent 105A and the second adsorbent 105B.
  • the adsorption process had been carried out for 11 minutes, the adsorption process and desorption process were switched, and desorption steam was introduced into the second treatment tank 104B, and the desorption process was carried out for 9 minutes.
  • the flow rate of steam VIII was adjusted to 160 g/min. Furthermore, the opening of adjustment valve V4 was automatically adjusted so that the internal pressure on the shell side was maintained at 0.060 MPa by pressure sensor 115F of heat exchanger 115, and steam VII was supplied to the shell side of heat exchanger 115.
  • Make-up water VI was supplied so that half of tube 115B of heat exchanger 115 was immersed in make-up water VI, adjusting the water level and generating regenerated steam. The generated regenerated steam was sucked into steam compressor 122, mixed with steam VIII, and then supplied to second treatment tank 104B as desorption steam.
  • Comparative Example 1 The gas to be treated was treated in the same manner as in the Example, except that steam VII was not supplied to the shell side of the heat exchanger 115. As a result, the recovery efficiency of the organic solvent after 10 cycles was 91%, which was significantly lower than the recovery efficiency in the Example.
  • the present invention makes it possible to provide an organic solvent recovery system that is energy-saving and improves the efficiency of organic solvent recovery, making a great contribution to the industrial world.
  • 1A, 1B organic solvent recovery system 100 organic solvent recovery device, 101 treated gas line, 102 treated gas blower, 103 treated gas introduction line, 104A first treatment tank, 104B second treatment tank, 105A first adsorbent, 105B second adsorbent, 106A first upper damper, 106B second upper damper, 107A first lower damper, 107B second lower damper, 108 desorption water vapor line, 110 desorption gas line, 111 condenser (cooling section), 112 condenser condensate line, 113 separator (condensate reservoir section), 113A recovered solvent, 113B separated wastewater, 114 return gas line, 115 heat exchanger, 115A shell (heat absorption section, container section), 115B tube (heat generating section part, pipe part), 115C desorption gas inlet chamber, 115D desorption gas outlet chamber (desorption gas outlet receiving part), 115E makeup water storage part, 115F pressure sensor (pressure measurement part), 115G control part,

Abstract

This organic solvent recovery system comprises: an organic solvent recovery device that includes a processing vessel storing an adsorbent for adsorbing and removing an organic solvent from gas to be processed that contains the organic solvent, the organic solvent recovery device repeating an adsorption process for bringing the gas to be processed supplied to the processing vessel into contact with the adsorbent, and discharging the processed gas, and a desorption process for desorbing the organic solvent from the adsorbent by means of desorption steam supplied to the processing vessel, and discharging the desorbed gas; a heat exchanger that has a heat generation unit through which the desorbed gas discharged from the organic solvent recovery device passes, and a heat absorption unit replenished with replenishment water, and that generates steam by indirectly heating the replenishment water of the heat absorption unit with the desorbed gas passing through the heat generation unit, and discharges the desorbed gas after the indirect heating; and a cooling unit that cools the desorbed gas discharged from the heat exchanger, and discharges the condensate, wherein the system includes a steam supply unit that supplies steam to the heat absorption unit of the heat exchanger, and the heat exchanger supplies, to the organic solvent recovery device as at least a portion of the desorption steam, recycled steam obtained by mixing the steam generated from the replenishment water and the steam supplied from the steam supply unit.

Description

有機溶剤回収システムOrganic Solvent Recovery System
　本発明は、有機溶剤回収システムに関するものである。 The present invention relates to an organic solvent recovery system.
　有機溶剤回収装置は、吸着材で被処理ガスの有機溶剤を吸着する１対の処理槽と、各処理槽に対する被処理ガス供給装置と脱着用ガス供給装置とを設け、処理槽に被処理ガスを供給する吸着工程と脱着用ガスを供給する脱着工程とに切り替える機構が採用されている。 The organic solvent recovery system is equipped with a pair of treatment tanks that use an adsorbent to adsorb the organic solvents in the gas to be treated, a treatment gas supply device and a desorption gas supply device for each treatment tank, and employs a mechanism for switching between an adsorption process that supplies the gas to be treated to the treatment tank, and a desorption process that supplies the desorption gas.
　ガス処理装置の吸着材として、例えば、活性炭素繊維が使用されている。活性炭素繊維は低濃度の有機溶剤含有ガスを吸着する機能に優れ、吸着材として使用されている。例えば、活性炭素繊維を支持体に固定し、又は自己支持にて円筒状に構成し、芯材内に縦型に配設したガス処理装置が、特開２０１４－１４７８６４号公報（特許文献１）に開示されている。 Activated carbon fibers, for example, are used as adsorbents in gas treatment devices. Activated carbon fibers have excellent ability to adsorb low-concentration organic solvent-containing gases and are used as adsorbents. For example, JP 2014-147864 A (Patent Document 1) discloses a gas treatment device in which activated carbon fibers are fixed to a support or self-supported into a cylindrical shape and arranged vertically within a core material.
　また、実開昭５８－１６１６３６号公報（特許文献２）では活性炭吸着器（処理槽）の脱着蒸気出口に熱交換器の凝縮側を接続すると共に、熱交換器の蒸発側に水を供給し、熱交換器の蒸発側と前記活性炭吸着器の脱着用水蒸気入口を接続したラインに減圧ブロアを介設し、脱着蒸気の熱で蒸発側の水を蒸発させて脱着用水蒸気を発生させることで、水蒸気使用量を削減した活性炭脱着装置が開示されている。 Furthermore, Japanese Utility Model Application Publication No. 58-161636 (Patent Document 2) discloses an activated carbon desorption device that reduces the amount of water vapor used by connecting the condensation side of a heat exchanger to the desorption steam outlet of an activated carbon adsorber (treatment tank), supplying water to the evaporation side of the heat exchanger, and installing a pressure reducing blower in the line connecting the evaporation side of the heat exchanger to the desorption water vapor inlet of the activated carbon adsorber, and evaporating the water on the evaporation side using the heat of the desorption steam to generate water vapor for desorption.
特開２０１４－１４７８６４号公報JP 2014-147864 A 実開昭５８－１６１６３６号公報Japanese Utility Model Application Publication No. 58-161636
　脱着工程において、処理槽から排出される脱着ガスの温度は外気温度や被処理ガスの有機溶剤濃度、被処理ガスの湿度などの変動によって随時変化するため、特許文献２のように熱交換器を介して脱着ガスの熱で脱着用水蒸気を発生させる場合は、脱着用水蒸気の流量を十分確保できない恐れがある。 In the desorption process, the temperature of the desorption gas discharged from the treatment tank changes from time to time due to fluctuations in the outside air temperature, the organic solvent concentration in the gas being treated, the humidity of the gas being treated, and other factors. Therefore, when generating desorption water vapor using the heat of the desorption gas via a heat exchanger as in Patent Document 2, there is a risk that the flow rate of the desorption water vapor cannot be sufficiently secured.
　また、脱着工程の前期において、処理槽に供給される脱着用水蒸気の熱は吸着材や処理槽本体、配管、切り替えバルブの加熱に多く消費されるため、結果として処理槽から排出される脱着ガスの温度が低くなる。そのため、特許文献２のように熱交換器を介して脱着ガスの熱で脱着用水蒸気を発生させる場合は、脱着工程の前期において、脱着用水蒸気がほとんど発生させることができない恐れがある。その結果、脱着工程の前期において、脱着用水蒸気の流量を十分確保できない恐れがある。 In addition, in the early stage of the desorption process, much of the heat of the desorption steam supplied to the treatment tank is consumed in heating the adsorbent, the treatment tank body, the piping, and the switching valve, resulting in a low temperature of the desorption gas discharged from the treatment tank. Therefore, when desorption steam is generated using the heat of the desorption gas via a heat exchanger as in Patent Document 2, there is a risk that almost no desorption steam can be generated in the early stage of the desorption process. As a result, there is a risk that a sufficient flow rate of desorption steam cannot be secured in the early stage of the desorption process.
　これらの問題により、脱着ガスの熱で脱着用水蒸気を発生させる機構を有する有機溶剤回収装置を考えた場合は、脱着工程中の脱着用水蒸気の流量が安定しないことから、有機溶剤の脱着効率が低下し、有機溶剤の回収効率が低下する恐れがある。 When considering an organic solvent recovery device that has a mechanism for generating desorption steam using the heat of the desorption gas due to these problems, the flow rate of the desorption steam during the desorption process is not stable, which may reduce the desorption efficiency of the organic solvent and the recovery efficiency of the organic solvent.
　そこで本発明では、上記課題に鑑みなされ、その目的は、脱着ガスの熱で脱着用水蒸気を発生させる機構を有し、処理槽へ供給される脱着用水蒸気の流量が十分確保され、有機溶剤の回収効率が向上した有機溶剤回収システムを提供することにある。 In view of the above problems, the present invention aims to provide an organic solvent recovery system that has a mechanism for generating desorption steam using the heat of the desorption gas, ensures a sufficient flow rate of the desorption steam supplied to the treatment tank, and improves the efficiency of organic solvent recovery.
　本発明の有機溶剤回収システムは、以下の構成を備える。 The organic solvent recovery system of the present invention has the following configuration.
　有機溶剤を含有する被処理ガスから有機溶剤を吸着除去する吸着材が収容された処理槽を備え、前記処理槽に供給された前記被処理ガスを前記吸着材に接触させて処理ガスを排出する吸着処理と、前記処理槽に供給された脱着用水蒸気により前記吸着材から前記有機溶剤を脱着して脱着ガスを排出する脱着処理とを繰り返す有機溶剤回収装置と、
　前記有機溶剤回収装置から排出された前記脱着ガスが通過する発熱部と、補給水が補給される吸熱部とを有し、当該発熱部を通過する前記脱着ガスにて、当該吸熱部の補給水を間接加熱して水蒸気を発生させ、間接加熱後の前記脱着ガスを排出する熱交換器と、
　前記熱交換器から排出された前記脱着ガスを冷却して凝縮液を排出する冷却部と、を備えた有機溶剤回収システムであって、
　前記熱交換器に水蒸気を供給する水蒸気供給部を備え、
　前記熱交換器は、前記補給水から発生した水蒸気と前記水蒸気供給部から供給された水蒸気とが混合された再生水蒸気を、前記脱着用水蒸気の少なくとも一部として前記有機溶剤回収装置に供給する。 an organic solvent recovery apparatus including a treatment tank containing an adsorbent that adsorbs and removes an organic solvent from a gas to be treated that contains the organic solvent, and repeats an adsorption process in which the gas to be treated that is supplied to the treatment tank is brought into contact with the adsorbent to discharge a treated gas, and a desorption process in which the organic solvent is desorbed from the adsorbent by a desorption steam supplied to the treatment tank and a desorbed gas is discharged;
a heat exchanger including a heat generating section through which the desorption gas discharged from the organic solvent recovery apparatus passes and an endothermic section to which makeup water is replenished, the heat exchanger indirectly heating the makeup water of the endothermic section with the desorption gas passing through the heat generating section to generate steam, and discharging the indirectly heated desorption gas;
a cooling unit that cools the desorption gas discharged from the heat exchanger and discharges a condensate,
A water vapor supply unit that supplies water vapor to the heat exchanger,
The heat exchanger supplies regenerated steam, which is a mixture of steam generated from the make-up water and steam supplied from the steam supply unit, to the organic solvent recovery apparatus as at least a part of the desorption steam.
　上記の有機溶剤回収システムは、前記熱交換器の前記吸熱部の気相部分の圧力を測定する圧力測定部を備え、当該圧力測定部の測定結果により前記水蒸気供給部から前記熱交換器に供給される水蒸気の流量を制御してもよい。 The organic solvent recovery system may include a pressure measuring unit that measures the pressure of the gas phase of the heat absorption section of the heat exchanger, and may control the flow rate of water vapor supplied from the water vapor supply unit to the heat exchanger based on the measurement results of the pressure measuring unit.
　上記の有機溶剤回収システムでは、前記水蒸気供給部は、前記脱着処理の前期には、前記熱交換器に水蒸気を供給し、前記脱着処理の後期には、前記熱交換器に水蒸気を供給しなくてもよい。 In the organic solvent recovery system described above, the water vapor supply unit may supply water vapor to the heat exchanger in the early stage of the desorption process, and may not supply water vapor to the heat exchanger in the later stage of the desorption process.
　上記有機溶剤回収システムでは、前記有機溶剤回収装置は、前記冷却部から排出される凝縮液を溜める凝縮液溜部を備え、前記熱交換器は、間接加熱した後の前記脱着ガスが滞留する脱着ガス出口受部と、当該脱着ガス出口受部から未凝縮の前記脱着ガスを前記冷却部に供給する配管経路と、当該脱着ガス出口受部から凝縮液となった前記脱着ガスを前記凝縮液溜部に供給する配管経路と、を備えてもよい。 In the organic solvent recovery system, the organic solvent recovery device may include a condensate reservoir that accumulates the condensate discharged from the cooling section, and the heat exchanger may include a desorption gas outlet receiving section in which the desorption gas accumulates after indirect heating, a piping path that supplies the uncondensed desorption gas from the desorption gas outlet receiving section to the cooling section, and a piping path that supplies the desorption gas that has become condensed from the desorption gas outlet receiving section to the condensate reservoir.
　上記の有機溶剤回収システムは、前記処理槽から排出される前記脱着ガスを前記熱交換器に供給する経路と、前記処理槽から排出される前記脱着ガスを前記冷却部に供給する経路と、を備えていてもよい。 The organic solvent recovery system may include a path for supplying the desorption gas discharged from the treatment tank to the heat exchanger, and a path for supplying the desorption gas discharged from the treatment tank to the cooling section.
　上記の有機溶剤回収システムは、前記脱着処理の前期において、前記処理槽から排出される前記脱着ガスを前記冷却部に供給するとともに、前記水蒸気供給部から前記熱交換器の前記吸熱部に水蒸気を供給し、前記脱着処理の後期において、前記処理槽から排出される前記脱着ガスを前記熱交換器の前記発熱部に供給するとともに、前記水蒸気供給部から前記熱交換器の前記吸熱部に水蒸気を供給しなくてもよい。 The organic solvent recovery system described above may supply the desorption gas discharged from the treatment tank to the cooling section and supply water vapor from the water vapor supply section to the heat absorption section of the heat exchanger in the early stage of the desorption process, and may supply the desorption gas discharged from the treatment tank to the heat generation section of the heat exchanger in the later stage of the desorption process, without having to supply water vapor from the water vapor supply section to the heat absorption section of the heat exchanger.
　上記の有機溶剤回収システムでは、前記熱交換器は、容器部の内部に管部を備えた多管式熱交換器であってもよい。 In the organic solvent recovery system described above, the heat exchanger may be a multi-tube heat exchanger having a tube section inside a container section.
　上記の有機溶剤回収システムは、前記水蒸気供給部は、前記有機溶剤回収装置に前記脱着用水蒸気を直接供給する脱着用水蒸気供給部と接続している又は兼用されていてもよい。 In the organic solvent recovery system described above, the water vapor supply unit may be connected to or may share a desorption water vapor supply unit that directly supplies the desorption water vapor to the organic solvent recovery device.
　本発明に従えば、脱着ガスの熱で脱着用水蒸気を発生させる機構を有し、処理槽へ供給される脱着用水蒸気の流量が十分確保され、有機溶剤の回収効率が向上した有機溶剤回収システムの提供を可能にする。 According to the present invention, it is possible to provide an organic solvent recovery system that has a mechanism for generating desorption steam using the heat of the desorption gas, ensures a sufficient flow rate of the desorption steam supplied to the treatment tank, and improves the efficiency of organic solvent recovery.
実施の形態１における有機溶剤回収システムの構成を示す概念図である。1 is a conceptual diagram showing a configuration of an organic solvent recovery system in a first embodiment. 実施の形態２における有機溶剤回収システムの構成を示す概念図である。FIG. 11 is a conceptual diagram showing the configuration of an organic solvent recovery system in a second embodiment. 実施の形態２における有機溶剤回収装置の吸着工程及び脱着工程の時間的な切り替わりを示すタイムチャートである。10 is a time chart showing the time-dependent switching between an adsorption process and a desorption process of an organic solvent recovery apparatus in accordance with the second embodiment;
　本発明に基づく実施の形態の有機溶剤回収システムについて、以下、図面を参照しながら説明する。以下に説明する実施の形態において、個数、量などに言及する場合、特に記載がある場合を除き、本発明の範囲は必ずしもその個数、量などに限定されない。同一の部品、相当部品に対しては、同一の参照番号を付し、重複する説明は繰り返さない場合がある。実施の形態における構成を適宜組み合わせて用いることは当初から予定されていることである。 The organic solvent recovery system according to the embodiment of the present invention will be described below with reference to the drawings. In the embodiment described below, when numbers, amounts, etc. are mentioned, the scope of the present invention is not necessarily limited to those numbers, amounts, etc., unless otherwise specified. The same reference numbers are used for the same parts or equivalent parts, and redundant explanations may not be repeated. It is intended from the beginning that the configurations in the embodiment will be used in appropriate combinations.
　ここで、本明細書において有機溶剤とは、塩化メチレン、クロロホルム、四塩化炭素、塩化エチレン、トリクロロエチレン、テトラクロロエチレン、ｏ－ジクロロベンゼン、ｍ－ジクロロベンゼン、フロン－１１２、フロン－１１３、ＨＣＦＣ、ＨＦＣ、臭化プロピル、ヨウ化ブチル、酢酸メチル、酢酸エチル、酢酸プロピル、酢酸ブチル、酢酸ビニル、プロピオン酸メチル、アクリル酸メチル、アクリル酸エチル、アクリル酸ブチル、メタクリル酸メチル、炭酸ジエチル、蟻酸エチル、ジエチルエーテル、ジプロピルエーテル、テトラヒドロフラン、ジブチルエーテル、アニソール、メタノール、エタノール、イソプロパノール、ｎ－ブタノール、２－ブタノール、イソブタノール、ｔ－ブタノール、アリルアルコール、ペンタノール、ヘプタノール、エチレングリコール、ジエチレングリコール、フェノール、ｏ－クレゾール、ｍ－クレゾール、ｐ－クレゾール、キシレノール、アセトン、メチルエチルケトン、メチルイソブチルケトン、シクロヘキサノン、ホロン、アクリロニトリル、ｎ－ヘキサン、イソヘキサン、シクロヘキサン、メチルシクロヘキサン、ｎ－ヘプタン、ｎ－オクタン、ｎ－ノナン、イソノナン、デカン、ドデカン、ウンデカン、テトラデカン、デカリン、ベンゼン、トルエン、ｍ－キシレン、ｐ－キシレン、ｏ－キシレン、エチルベンゼン、１，３，５－トリメチルベンゼン、Ｎ－メチルピロリドン、ジメチルホルムアミド、ジメチルアセトアミド及びジメチルスルホキシド等を指すが、これらには限定されない。 In this specification, organic solvents include methylene chloride, chloroform, carbon tetrachloride, ethylene chloride, trichloroethylene, tetrachloroethylene, o-dichlorobenzene, m-dichlorobenzene, fluorocarbon-112, fluorocarbon-113, HCFC, HFC, propyl bromide, butyl iodide, methyl acetate, ethyl acetate, propyl acetate, butyl acetate, vinyl acetate, methyl propionate, methyl acrylate, ethyl acrylate, butyl acrylate, methyl methacrylate, diethyl carbonate, ethyl formate, diethyl ether, dipropyl ether, tetrahydrofuran, dibutyl ether, anisole, methanol, ethanol, isopropanol, n-butanol, 2-butanol, isobutanol, t-butanol, and allyl alcohol. , pentanol, heptanol, ethylene glycol, diethylene glycol, phenol, o-cresol, m-cresol, p-cresol, xylenol, acetone, methyl ethyl ketone, methyl isobutyl ketone, cyclohexanone, phorone, acrylonitrile, n-hexane, isohexane, cyclohexane, methylcyclohexane, n-heptane, n-octane, n-nonane, isononane, decane, dodecane, undecane, tetradecane, decalin, benzene, toluene, m-xylene, p-xylene, o-xylene, ethylbenzene, 1,3,5-trimethylbenzene, N-methylpyrrolidone, dimethylformamide, dimethylacetamide, and dimethylsulfoxide, but are not limited to these.
　［実施の形態１］
　図１を参照して、本実施の形態１の有機溶剤回収システムについて説明する。図１は、実施の形態１の有機溶剤回収システム１Ａの構成を示す図である。 [First embodiment]
An organic solvent recovery system according to the first embodiment will be described with reference to Fig. 1. Fig. 1 is a diagram showing the configuration of an organic solvent recovery system 1A according to the first embodiment.
　有機溶剤回収システム１Ａは、有機溶剤回収装置１００、熱交換器１１５、及び冷却部としてコンデンサ１１１を備える。
　有機溶剤回収装置１００は、第１処理槽１０４Ａ、及び、第２処理槽１０４Ｂを備える。第１処理槽１０４Ａは、円筒形状の第１吸着材１０５Ａを含み、第２処理槽１０４Ｂは、円筒形状の第２吸着材１０５Ｂを含む。第１吸着材１０５Ａ及び第２吸着材１０５Ｂは、外側から内側に向けて被処理ガスＩが通過して吸着工程（吸着処理）が実施され、内側から外側に向けて水蒸気が通過して脱着工程（脱着処理）が実施される。第１吸着材１０５Ａ及び第２吸着材１０５Ｂには、例えば、活性炭素繊維や活性炭等が用いられる。 The organic solvent recovery system 1A includes an organic solvent recovery device 100, a heat exchanger 115, and a condenser 111 as a cooling section.
The organic solvent recovery apparatus 100 includes a first treatment tank 104A and a second treatment tank 104B. The first treatment tank 104A includes a cylindrical first adsorbent 105A, and the second treatment tank 104B includes a cylindrical second adsorbent 105B. The first adsorbent 105A and the second adsorbent 105B are passed from the outside to the inside to perform an adsorption process (adsorption process), and water vapor is passed from the inside to the outside to perform a desorption process (desorption process). For example, activated carbon fiber or activated carbon is used for the first adsorbent 105A and the second adsorbent 105B.
　第１処理槽１０４Ａ及び第２処理槽１０４Ｂは、被処理ガス導入ライン１０３及び脱着ガスライン１１０に連結されている。被処理ガス導入ライン１０３への連結の開閉、及び、脱着ガスライン１１０への連結の開閉を行なうため、第１処理槽１０４Ａ及び第２処理槽１０４Ｂには、それぞれ第１下ダンパ１０７Ａ及び第２下ダンパ１０７Ｂが設けられている。 The first treatment tank 104A and the second treatment tank 104B are connected to the treated gas inlet line 103 and the desorption gas line 110. The first treatment tank 104A and the second treatment tank 104B are provided with a first lower damper 107A and a second lower damper 107B, respectively, to open and close the connection to the treated gas inlet line 103 and the connection to the desorption gas line 110.
　第１処理槽１０４Ａ及び第２処理槽１０４Ｂの上方には、それぞれ、被処理ガスＩの流通を制御する第１上ダンパ１０６Ａ及び第２上ダンパ１０６Ｂが設けられている。 A first upper damper 106A and a second upper damper 106B that control the flow of the gas I to be treated are provided above the first treatment tank 104A and the second treatment tank 104B, respectively.
　脱着ガスライン１１０には、熱交換器１１５が連結されている。熱交換器１１５は脱着ガスライン１１０が連結される脱着ガス入口チャンバー１１５Ｃを有する。また、熱交換器１１５は熱交換器出口ガスライン１１７、及び、熱交換器凝縮液ライン１１８が連結される脱着ガス出口受部である脱着ガス出口チャンバー１１５Ｄを有する。さらに補給水収容部１１５Ｅには補給水ＶＩが供給される。補給水ＶＩは、例えば、送液ポンプなどによって補給水収容部１１５Ｅに送られる。 A heat exchanger 115 is connected to the desorption gas line 110. The heat exchanger 115 has a desorption gas inlet chamber 115C to which the desorption gas line 110 is connected. The heat exchanger 115 also has a desorption gas outlet chamber 115D, which is a desorption gas outlet receiving section to which a heat exchanger outlet gas line 117 and a heat exchanger condensate line 118 are connected. Furthermore, makeup water VI is supplied to the makeup water storage section 115E. The makeup water VI is sent to the makeup water storage section 115E, for example, by a liquid delivery pump or the like.
　熱交換器１１５は、脱着ガスライン１１０から供給された脱着ガスによって補給水収容部１１５Ｅ中の補給水ＶＩを間接加熱することにより、当該補給水ＶＩを蒸発させて水蒸気を発生させる。 The heat exchanger 115 indirectly heats the make-up water VI in the make-up water storage section 115E with the desorption gas supplied from the desorption gas line 110, thereby evaporating the make-up water VI and generating water vapor.
　補給水収容部１１５Ｅは、沸点が例えば７０℃以上９７℃以下、好ましくは７５℃以上９５℃以下になるように減圧されており、発生した水蒸気は熱交換器１１５に連結された再生水蒸気ライン１１９を通じ、再生水蒸気としてスチームコンプレッサー１２２に供給される。スチームコンプレッサー１２２は高圧の水蒸気を駆動源（以下、駆動水蒸気）として定圧の水蒸気（以下、吸引水蒸気）を減圧状態にして吸込み、中圧の水蒸気（以下、吐出水蒸気）へ昇圧する機構である。本発明では、スチームコンプレッサー用水蒸気ライン１２１を通じて高圧の水蒸気ＶＩＩＩ（水蒸気Ｖの一部）を駆動水蒸気としてスチームコンプレッサー１２２に供給することで、再生水蒸気ライン１１９を通じて再生水蒸気を吸引水蒸気として吸込み、脱着用水蒸気ライン１０８を通じて水蒸気ＶＩＩＩと再生水蒸気が混合された脱着用水蒸気を吐出水蒸気として排出する。スチームコンプレッサー１２２から排出された脱着用水蒸気は脱着用水蒸気ライン１０８を通じて脱着工程を行っている第１処理槽１０４Ａ及び第２処理槽１０４Ｂに供給される。なお、スチームコンプレッサー１２２は同様の効果を有する圧縮機を代わりに用いても良く、例えばルーツブロワー、ターボブロワーなどがあげられる。 The make-up water storage section 115E is decompressed so that the boiling point is, for example, 70°C to 97°C, preferably 75°C to 95°C, and the generated water vapor is supplied to the steam compressor 122 as regenerated water vapor through the regenerated water vapor line 119 connected to the heat exchanger 115. The steam compressor 122 is a mechanism that uses high-pressure water vapor as a driving source (hereinafter, driving water vapor) to draw in constant-pressure water vapor (hereinafter, sucked water vapor) in a reduced pressure state and increase the pressure to medium-pressure water vapor (hereinafter, discharged water vapor). In the present invention, high-pressure water vapor VIII (a part of water vapor V) is supplied to the steam compressor 122 as driving water vapor through the steam compressor water vapor line 121, so that the regenerated water vapor is sucked in as sucked water vapor through the regenerated water vapor line 119, and the desorption water vapor, which is a mixture of water vapor VIII and regenerated water vapor, is discharged as discharged water vapor through the desorption water vapor line 108. The desorption steam discharged from the steam compressor 122 is supplied to the first treatment tank 104A and the second treatment tank 104B where the desorption process is being carried out through the desorption steam line 108. Note that the steam compressor 122 may be replaced by a compressor having a similar effect, such as a roots blower or a turbo blower.
　補給水収容部１１５Ｅには、水蒸気Ｖの一部である水蒸気ＶＩＩを供給するための水蒸気供給部である熱交換器用水蒸気供給ライン１２０が連結されている。水蒸気ＶＩＩを供給することで、補給水収容部１１５Ｅを所定の圧力以上（例えばゲージ圧で－０．０９９ＭＰａ以上）に保つことができ、スチームコンプレッサー１２２が吸い込む吸引水蒸気、すなわち再生水蒸気の流量を十分確保することができる。結果としてスチームコンプレッサー１２２の吐出水蒸気、すなわち脱着用水蒸気の流量を十分確保することができ、有機溶剤回収装置１００の脱着工程における有機溶剤の脱着効率が高く維持される。また、熱交換器１１５に供給される脱着ガスの温度が低い時間帯において、水蒸気ＶＩＩを供給することで熱交換器１１５本体や補給水収容部１１５Ｅ中の補給水ＶＩを高温の状態に維持することができ、当該補給水ＶＩを効率よく蒸発させることができる。 The makeup water storage section 115E is connected to a heat exchanger steam supply line 120, which is a steam supply section for supplying steam VII, which is a part of the steam V. By supplying steam VII, the makeup water storage section 115E can be kept at a predetermined pressure or higher (for example, a gauge pressure of -0.099 MPa or higher), and the flow rate of the suction steam sucked into the steam compressor 122, i.e., the regenerated steam, can be sufficiently ensured. As a result, the flow rate of the discharge steam of the steam compressor 122, i.e., the desorption steam, can be sufficiently ensured, and the desorption efficiency of the organic solvent in the desorption process of the organic solvent recovery device 100 can be maintained high. In addition, by supplying steam VII during a time period when the temperature of the desorption gas supplied to the heat exchanger 115 is low, the makeup water VI in the heat exchanger 115 body and the makeup water storage section 115E can be maintained at a high temperature, and the makeup water VI can be efficiently evaporated.
　補給水収容部１１５Ｅには、熱交換器１１５内の圧力を測定する圧力測定部である圧力センサー１１５Ｆが設けられている。また、熱交換器用水蒸気供給ライン１２０上には水蒸気ＶＩＩの流量を調整する調整バルブＶ４が設けられている。 The makeup water storage section 115E is provided with a pressure sensor 115F, which is a pressure measuring section that measures the pressure inside the heat exchanger 115. In addition, an adjustment valve V4 is provided on the heat exchanger steam supply line 120 to adjust the flow rate of the steam VII.
　熱交換器１１５には水蒸気ＶＩＩの流量を調整する制御部１１５Ｇが設けられている。具体的に、制御部１１５Ｇは圧力センサー１１５Ｆで検出される補給水収容部１１５Ｅの圧力が所定範囲（ゲージ圧で－０．０９９～－０．０８０ＭＰａ程度）に維持されるように、調整バルブＶ４の開度を調整して水蒸気ＶＩＩを供給する。 The heat exchanger 115 is provided with a control unit 115G that adjusts the flow rate of the water vapor VII. Specifically, the control unit 115G adjusts the opening of the adjustment valve V4 to supply the water vapor VII so that the pressure of the makeup water storage unit 115E detected by the pressure sensor 115F is maintained within a predetermined range (approximately -0.099 to -0.080 MPa in gauge pressure).
　熱交換器１１５は多管式熱交換器である。多管式熱交換器とは、容器部であるシェルと呼ばれる円筒内に多数の管部であるチューブを配列した熱交換器であり、チューブの表面が伝熱面としてはたらき、チューブ１１５Ｂの内側（以下、チューブ側）に流れる流体とチューブ１１５Ｂの外側とシェル１１５Ａの内側との間（以下、シェル側）に流れる流体との熱交換が行われる。つまり、チューブ１１５Ｂが熱を与える発熱部であり、シェル１１５Ａが熱を受け取る吸熱部である。チューブ１１５Ｂは脱着ガス入口チャンバー１１５Ｃと脱着ガス出口チャンバー１１５Ｄを連結する。さらに本発明の熱交換器１１５は、チューブ１１５Ｂが水平方向を向くように配置され、チューブ側が脱着ガスを供給する凝縮側としてはたらき、シェル側が補給水ＶＩ及び水蒸気ＶＩＩを供給する蒸発側としてはたらく。 The heat exchanger 115 is a multi-tube heat exchanger. A multi-tube heat exchanger is a heat exchanger in which a large number of tubes are arranged inside a cylinder called a shell, which is a container part. The surface of the tubes acts as a heat transfer surface, and heat is exchanged between the fluid flowing inside the tube 115B (hereinafter, the tube side) and the fluid flowing between the outside of the tube 115B and the inside of the shell 115A (hereinafter, the shell side). In other words, the tube 115B is a heat generating part that provides heat, and the shell 115A is a heat absorbing part that receives heat. The tube 115B connects the desorption gas inlet chamber 115C and the desorption gas outlet chamber 115D. Furthermore, the heat exchanger 115 of the present invention is arranged so that the tube 115B faces horizontally, and the tube side acts as a condensation side that supplies the desorption gas, and the shell side acts as an evaporation side that supplies makeup water VI and steam VII.
　シェル１１５Ａ内では補給水ＶＩがチューブ１１５Ｂの一部と接触する水量で常に滞留している。補給水ＶＩとチューブ１１５Ｂが接触することにより、補給水ＶＩが脱着ガスから受熱して蒸発する。また、チューブ１１５Ｂは補給水を蒸発温度まで加熱する役割も果たすため、補給水ＶＩを加温するための補給水加温設備を別途設ける必要がない。 In shell 115A, makeup water VI always remains in an amount that contacts a portion of tube 115B. When makeup water VI comes into contact with tube 115B, makeup water VI receives heat from the desorbed gas and evaporates. In addition, tube 115B also serves to heat makeup water up to the evaporation temperature, so there is no need to provide a separate makeup water heating facility to heat makeup water VI.
　熱交換器１１５は、チューブ１１５Ｂの一部が補給水収容部１１５Ｅ中の補給水ＶＩと接触させないように補給水ＶＩの水面高さを調整することが好ましい。具体的に、チューブ１１５Ｂの一部が補給水ＶＩの水面と再生水蒸気ライン１１９との間の、シェル１１５Ａ内の気相部分に位置する。シェル１１５Ａ内の気相部分に位置するチューブ１１５Ｂによって、再生水蒸気が加熱され、再生水蒸気がスチームコンプレッサー１２２に吸い込まれるまでに凝縮することを防ぐことができる。なお、補給水ＶＩの水面高さを調整する手段として、例えばフロート式、ディスペーサー式、差圧式、静電容量式液面計による制御方法が考えられる。 The heat exchanger 115 preferably adjusts the water level of the make-up water VI so that a portion of the tube 115B does not come into contact with the make-up water VI in the make-up water storage section 115E. Specifically, a portion of the tube 115B is located in the gas phase portion of the shell 115A between the water level of the make-up water VI and the regenerated steam line 119. The regenerated steam is heated by the tube 115B located in the gas phase portion of the shell 115A, and this prevents the regenerated steam from condensing before being sucked into the steam compressor 122. Note that possible means for adjusting the water level of the make-up water VI include, for example, a control method using a float type, a spacer type, a differential pressure type, or a capacitance type liquid level gauge.
　熱交換器１１５の脱着ガス出口チャンバー１１５Ｄは熱交換器出口ガスライン１１７に連結し、コンデンサ１１１と接続される。コンデンサ１１１の内部では、熱交換器１１５で熱交換を終えた脱着ガスと冷却水との熱交換が行われ、脱着ガスが冷却凝縮される。 The desorbed gas outlet chamber 115D of the heat exchanger 115 is connected to the heat exchanger outlet gas line 117 and is connected to the condenser 111. Inside the condenser 111, heat exchange occurs between the desorbed gas that has completed heat exchange in the heat exchanger 115 and the cooling water, and the desorbed gas is cooled and condensed.
　コンデンサ１１１で凝縮した凝縮液はコンデンサ凝縮液ライン１１２を通じて、凝縮液溜部であるセパレータ１１３に供給される。セパレータ１１３は、コンデンサ凝縮液ライン１１２から送られた凝縮液を、回収溶剤１１３Ａの層と分離排水１１３Ｂの層とに分離する。分離排水１１３Ｂについては、曝気装置にて曝気後に排水する構成を採用してもよい。 The condensate condensed in the condenser 111 is supplied to the separator 113, which is a condensate reservoir, through the condenser condensate line 112. The separator 113 separates the condensate sent from the condenser condensate line 112 into a layer of recovered solvent 113A and a layer of separated wastewater 113B. The separated wastewater 113B may be aerated in an aeration device before being discharged.
　熱交換器１１５の脱着ガス出口チャンバー１１５Ｄには熱交換器凝縮液ライン１１８が連結されている。熱交換器凝縮液ライン１１８はセパレータ１１３に連結されている。熱交換器１１５のチューブ１１５Ｂで熱交換を終えた脱着ガスは、未凝縮の脱着ガスと凝縮した凝縮液とに分離され、脱着ガス出口チャンバー１１５Ｄに供給される。脱着ガス出口チャンバー１１５Ｄに供給された脱着ガスの凝縮液は熱交換器凝縮液ライン１１８を通じてセパレータ１１３に直接供給される。熱交換器１１５の凝縮液をコンデンサに通さないことで、コンデンサで使用される冷却水の水量を削減することができる。 A heat exchanger condensate line 118 is connected to the desorption gas outlet chamber 115D of the heat exchanger 115. The heat exchanger condensate line 118 is connected to the separator 113. After completing heat exchange in the tube 115B of the heat exchanger 115, the desorption gas is separated into uncondensed desorption gas and condensed condensate, and supplied to the desorption gas outlet chamber 115D. The condensate of the desorption gas supplied to the desorption gas outlet chamber 115D is supplied directly to the separator 113 through the heat exchanger condensate line 118. By not passing the condensate of the heat exchanger 115 through the condenser, the amount of cooling water used in the condenser can be reduced.
　コンデンサ１１１の気相部分及びセパレータ１１３の気相部分には、戻りガスライン１１４が連結されている。戻りガスライン１１４は、被処理ガスライン１０１に導入されている。戻りガスライン１１４から被処理ガスライン１０１に返送されるガスは、被処理ガスＩの流れ方向に対して、対抗流となるように導入されるとよい。 A return gas line 114 is connected to the gas phase portion of the condenser 111 and the gas phase portion of the separator 113. The return gas line 114 is introduced into the treated gas line 101. The gas returned from the return gas line 114 to the treated gas line 101 is preferably introduced so as to flow in a counter flow direction to the flow direction of the treated gas I.
　被処理ガスライン１０１には、被処理ガス送風機１０２が設けられている。被処理ガス送風機１０２で送り出される被処理ガスＩは、被処理ガス導入ライン１０３を通じて、第１処理槽１０４Ａ及び第２処理槽１０４Ｂに送り込まれる。 The treated gas line 101 is provided with a treated gas blower 102. The treated gas I delivered by the treated gas blower 102 is sent through the treated gas introduction line 103 to the first treatment tank 104A and the second treatment tank 104B.
　スチームコンプレッサー１２２の吐出水蒸気、すなわち脱着用水蒸気は、脱着用水蒸気ライン１０８を通じて、第１処理槽１０４Ａ及び第２処理槽１０４Ｂに供給される。第１処理槽１０４Ａには、脱着用水蒸気ライン１０８が連結し、脱着用水蒸気ライン１０８には、第１水蒸気開閉弁Ｖ１が設けられている。第２処理槽１０４Ｂには、脱着用水蒸気ライン１０８が連結し、脱着用水蒸気ライン１０８には、第２水蒸気開閉弁Ｖ２が設けられている。 The discharged water vapor from the steam compressor 122, i.e., the desorption water vapor, is supplied to the first treatment tank 104A and the second treatment tank 104B through the desorption water vapor line 108. The desorption water vapor line 108 is connected to the first treatment tank 104A, and the desorption water vapor line 108 is provided with a first water vapor on-off valve V1. The desorption water vapor line 108 is connected to the second treatment tank 104B, and the desorption water vapor line 108 is provided with a second water vapor on-off valve V2.
　上記構成を有する有機溶剤回収装置１００において、第１上ダンパ１０６Ａ、第２上ダンパ１０６Ｂ、第１下ダンパ１０７Ａ、第２下ダンパ１０７Ｂ、第１水蒸気開閉弁Ｖ１、第２水蒸気開閉弁Ｖ２、熱交換器１１５、スチームコンプレッサー１２２、コンデンサ１１１、セパレータ１１３、及び、被処理ガス送風機１０２は、図示しない制御装置により、以下に示すガス処理方法を実現するように運転及び開閉が適宜制御される。 In the organic solvent recovery apparatus 100 having the above configuration, the first upper damper 106A, the second upper damper 106B, the first lower damper 107A, the second lower damper 107B, the first steam on-off valve V1, the second steam on-off valve V2, the heat exchanger 115, the steam compressor 122, the condenser 111, the separator 113, and the treated gas blower 102 are appropriately controlled in operation and opening/closing by a control device (not shown) to realize the gas treatment method described below.
　（ガス処理方法）
　上記構成を有する有機溶剤回収装置１００を用いたガス処理方法について説明する。図１において、有機溶剤回収装置１００の第１処理槽１０４Ａは脱着工程が実施され、第２処理槽１０４Ｂは吸着工程が実施される。 (Gas Treatment Method)
A gas treatment method using the organic solvent recovery apparatus 100 having the above-mentioned configuration will be described below. In Fig. 1, the first treatment tank 104A of the organic solvent recovery apparatus 100 is used for a desorption process, and the second treatment tank 104B is used for an adsorption process.
（第２処理槽１０４Ｂの吸着工程）
　有機溶剤含有ガスを含んだ被処理ガスＩは、被処理ガスライン１０１から、被処理ガス送風機１０２にて吸着工程となっている第２処理槽１０４Ｂに送られる。第２下ダンパ１０７Ｂは、被処理ガス導入ライン１０３を開放し、脱着ガスライン１１０を閉鎖するように制御される。 (Adsorption step in second treatment tank 104B)
The treated gas I containing an organic solvent-containing gas is sent from the treated gas line 101 to the second treatment tank 104B, which is in an adsorption process, by the treated gas blower 102. The second lower damper 107B is controlled to open the treated gas inlet line 103 and close the desorption gas line 110.
　第２上ダンパ１０６Ｂは、第２吸着材１０５Ｂにおける被処理ガスＩの流通を可能とする開状態に制御される。 The second upper damper 106B is controlled to an open state that allows the gas I to flow through the second adsorbent 105B.
　第２処理槽１０４Ｂの第２吸着材１０５Ｂで有機溶剤の吸着が行なわれ、処理ガスＩＩとして、システム外へ導出される。脱着用水蒸気ライン１０８の第２蒸気開閉弁１０９Ｖ２は、閉状態に制御される。 The organic solvent is adsorbed in the second adsorbent 105B of the second treatment tank 104B, and the treated gas II is discharged outside the system. The second steam opening/closing valve 109V2 of the desorption water vapor line 108 is controlled to a closed state.
　（第１処理槽１０４Ａの脱着工程）
　第１処理槽１０４Ａには被処理ガスＩを送ることはなく、第１下ダンパ１０７Ａで、被処理ガス導入ライン１０３は閉鎖され、脱着ガスライン１１０が開放された状態に制御される。第１下ダンパ１０７Ａは、第１吸着材１０５Ａの外側から内側へのガスの流通が閉鎖される。脱着用水蒸気が、脱着用水蒸気ライン１０８を通じて、第１吸着材１０５Ａの内側から外側への流通を可能に導入される。脱着用水蒸気ライン１０８の第１水蒸気開閉弁Ｖ１は、開状態に制御される。 (Desorption process of first treatment tank 104A)
The gas I to be treated is not sent to the first treatment tank 104A, and the first lower damper 107A controls the gas to be treated introduction line 103 to be closed and the desorption gas line 110 to be open. The first lower damper 107A blocks the flow of gas from the outside to the inside of the first adsorbent 105A. The water vapor for desorption is introduced through the water vapor line 108 for desorption so as to be able to flow from the inside to the outside of the first adsorbent 105A. The first water vapor on-off valve V1 of the water vapor line 108 for desorption is controlled to be open.
　脱着用水蒸気は水蒸気ＶＩＩＩと再生水蒸気とがスチームコンプレッサー１２２で混合されて生成される。水蒸気ＶＩＩＩは水蒸気Ｖの一部である。スチームコンプレッサー１２２はスチームコンプレッサー用水蒸気ライン１２１を通じて供給される水蒸気ＶＩＩＩを駆動源とし、再生水蒸気ライン１１９を通じて減圧状態にした再生水蒸気を吸込み、脱着用水蒸気ライン１０８を通じて水蒸気ＶＩＩＩと再生水蒸気とが混合された脱着用水蒸気を吐出する。 　Steam for desorption is generated by mixing steam VIII and regenerated steam in the steam compressor 122. Steam VIII is a part of steam V. The steam compressor 122 is driven by steam VIII supplied through steam line 121 for the steam compressor, sucks in regenerated steam in a reduced pressure state through regenerated steam line 119, and discharges desorption steam, which is a mixture of steam VIII and regenerated steam, through steam line 108 for desorption.
　第１処理槽１０４Ａ内では、脱着用水蒸気が噴出し、第１吸着材１０５Ａに吸着された有機溶剤が、第１吸着材１０５Ａから脱着される。脱着された有機溶剤と水蒸気が混合された脱着ガスは、脱着ガスライン１１０を通って熱交換器１１５へ送られる。 In the first treatment tank 104A, the desorption water vapor is ejected, and the organic solvent adsorbed in the first adsorbent 105A is desorbed from the first adsorbent 105A. The desorption gas, which is a mixture of the desorbed organic solvent and water vapor, is sent to the heat exchanger 115 through the desorption gas line 110.
　脱着ガスは熱交換器１１５のチューブ側へ供給され、熱交換器１１５のシェル側に滞留している補給水ＶＩと熱交換される。具体的に、伝熱面を通じて補給水ＶＩを間接加熱する。 The desorbed gas is supplied to the tube side of the heat exchanger 115 and exchanges heat with the make-up water VI that is retained on the shell side of the heat exchanger 115. Specifically, the make-up water VI is indirectly heated through the heat transfer surface.
　熱交換器１１５で補給水ＶＩとの熱交換を終えた脱着ガスは、未凝縮の脱着ガスと凝縮した凝縮液とに分離される。未凝縮の脱着ガスは熱交換器出口ガスライン１１７を通じてコンデンサ１１１に供給される。コンデンサ１１１の内部では、脱着ガスと冷却水との熱交換が行われ、脱着ガスが冷却凝縮される。一方、熱交換器１１５で凝縮した脱着ガスの凝縮液は熱交換器凝縮液ライン１１８を通じてセパレータ１１３に供給される。 After the desorption gas has completed heat exchange with makeup water VI in heat exchanger 115, it is separated into uncondensed desorption gas and condensed condensate. The uncondensed desorption gas is supplied to condenser 111 through heat exchanger outlet gas line 117. Inside condenser 111, heat exchange occurs between the desorption gas and cooling water, and the desorption gas is cooled and condensed. Meanwhile, the condensate of the desorption gas condensed in heat exchanger 115 is supplied to separator 113 through heat exchanger condensate line 118.
　コンデンサ１１１で凝縮した脱着ガスの凝縮液はコンデンサ凝縮液ライン１１２を通じてセパレータ１１３に供給される。セパレータ１１３において、回収溶剤１１３Ａの層と分離排水１１３Ｂの層とに分離する。 The condensate of the desorbed gas condensed in the condenser 111 is supplied to the separator 113 through the condenser condensate line 112. In the separator 113, it is separated into a layer of recovered solvent 113A and a layer of separated wastewater 113B.
　コンデンサ１１１及びセパレータ１１３内に滞留している戻りガスは、脱着ガスによって押し出され、戻りガスライン１１４を通って被処理ガスライン１０１に導入され、被処理ガスＩに混合される。被処理ガスライン１０１から導入される被処理ガスＩ及び戻りガスは、第２処理槽１０４Ｂに送られる。 The return gas remaining in the condenser 111 and separator 113 is pushed out by the desorbed gas and introduced into the treated gas line 101 through the return gas line 114, where it is mixed with the treated gas I. The treated gas I and the return gas introduced from the treated gas line 101 are sent to the second treatment tank 104B.
　脱着ガスが熱交換器１１５のチューブ側へ供給されている間、熱交換器１１５のシェル側では補給水ＶＩの蒸発により水蒸気が発生する。さらに熱交換器１１５のシェル側には熱交換器用水蒸気供給ライン１２０を通じて水蒸気Ｖの一部である水蒸気ＶＩＩが供給される。補給水ＶＩの蒸発により発生した水蒸気と水蒸気ＶＩＩとが混合した再生水蒸気が再生水蒸気ライン１１９を通じてスチームコンプレッサー１２２に吸い込まれる。水蒸気ＶＩＩの供給によって、補給水ＶＩの蒸発量が変動する場合においてもスチームコンプレッサー１２２に吸い込まれる再生水蒸気の流量が不足することなく、第１処理槽１０４Ａの脱着工程が効率よく行われる。 While the desorption gas is being supplied to the tube side of the heat exchanger 115, water vapor is generated on the shell side of the heat exchanger 115 due to the evaporation of the makeup water VI. In addition, water vapor VII, which is a part of the water vapor V, is supplied to the shell side of the heat exchanger 115 through a heat exchanger water vapor supply line 120. Regenerated water vapor, which is a mixture of the water vapor generated by the evaporation of the makeup water VI and the water vapor VII, is sucked into the steam compressor 122 through the regenerated water vapor line 119. By supplying water vapor VII, the flow rate of the regenerated water vapor sucked into the steam compressor 122 is not insufficient even when the evaporation amount of the makeup water VI fluctuates, and the desorption process of the first treatment tank 104A is efficiently performed.
　脱着工程の前期において、第１処理槽１０４Ａに供給された脱着用水蒸気の熱は第１吸着材１０５Ａや第１処理槽１０４Ａ本体、第１上ダンパ１０６Ａ、第１下ダンパ１０７Ａ、及び各配管ラインの加熱に多く消費されるため、第１処理槽１０４Ａから排出される脱着ガスの温度は低くなる。そのため、脱着工程の前期において、熱交換器１１５のシェル側に水蒸気ＶＩＩを供給し、第１処理槽１０４Ａから排出される脱着ガスが高温の状態（７０～１２０℃程度）になる脱着工程の後期において、熱交換器１１５のシェル側に水蒸気ＶＩＩを供給しないように制御すれば、脱着工程の前期の再生水蒸気の流量を十分確保できる上に水蒸気ＶＩＩの使用量を削減できるため、好ましい。 In the early stage of the desorption process, the heat of the desorption steam supplied to the first treatment tank 104A is consumed in large amounts to heat the first adsorbent 105A, the first treatment tank 104A body, the first upper damper 106A, the first lower damper 107A, and each piping line, so the temperature of the desorbed gas discharged from the first treatment tank 104A is low. Therefore, if steam VII is supplied to the shell side of the heat exchanger 115 in the early stage of the desorption process and controlled so that steam VII is not supplied to the shell side of the heat exchanger 115 in the later stage of the desorption process when the desorbed gas discharged from the first treatment tank 104A reaches a high temperature (approximately 70 to 120°C), it is preferable because this ensures a sufficient flow rate of regenerated steam in the early stage of the desorption process and reduces the amount of steam VII used.
　一定時間が経過すると吸着工程と脱着工程が切り替わり、第１処理槽１０４Ａが吸着工程、第２処理槽１０４Ｂが脱着工程となる。このように、吸着工程と脱着工程を交互に行なわれる連続的な処理により、有機溶剤回収装置１００によって、連続的に回収溶剤１１３Ａが回収される。 After a certain period of time has passed, the adsorption process and the desorption process are switched over, with the first treatment tank 104A performing the adsorption process and the second treatment tank 104B performing the desorption process. In this way, the organic solvent recovery device 100 continuously recovers the recovered solvent 113A through continuous processing in which the adsorption process and the desorption process are alternately performed.
　［実施の形態２］
　図２を参照して、実施の形態２の有機溶剤回収システムについて説明する。図２は、実施の形態２の有機溶剤回収システム１Ｂの構成を示す図である。図２に示すように、有機溶剤回収システム１Ｂは、実施の形態１で説明した有機溶剤回収システム１Ａの構成に加え、開閉バルブＶ３及びコンデンサライン１１６が備えられている。 [Embodiment 2]
An organic solvent recovery system according to the second embodiment will be described with reference to Fig. 2. Fig. 2 is a diagram showing the configuration of an organic solvent recovery system 1B according to the second embodiment. As shown in Fig. 2, the organic solvent recovery system 1B includes an on-off valve V3 and a condenser line 116 in addition to the configuration of the organic solvent recovery system 1A described in the first embodiment.
　図３は、図２に示す実施の形態２の有機溶剤回収装置１００の吸着工程及び脱着工程の時間的な切り替わりを示すタイムチャートである。以下では、図３を参照して、実施の形態２の有機溶剤回収装置１００が有機溶剤を回収する方法を説明する。 FIG. 3 is a time chart showing the time-dependent switching between the adsorption process and the desorption process of the organic solvent recovery apparatus 100 of the second embodiment shown in FIG. 2. In the following, the method of recovering the organic solvent by the organic solvent recovery apparatus 100 of the second embodiment will be described with reference to FIG. 3.
　実施の形態２の有機溶剤回収システム１Ｂの基本的構成は、上記実施の形態１で説明した有機溶剤回収システム１Ａと同じである。相違点として、実施の形態２の有機溶剤回収システム１Ｂでは、有機溶剤回収装置１００からの脱着ガスライン１１０上に三方式の開閉バルブＶ３を設けている。開閉バルブＶ３の下流側の一方は熱交換器１１５の脱着ガス入口チャンバー１１５Ｃに接続され、下流側のもう一方はコンデンサライン１１６を経由してコンデンサ１１１に接続される。開閉バルブＶ３によって脱着ガスの熱交換器１１５への供給、又はコンデンサ１１１への供給を切り替えることができる。なお、三方式の開閉バルブＶ３の代わりに二方式の開閉バルブを複数用いて同様の切り替え動作を行ってもよい。 The basic configuration of the organic solvent recovery system 1B of the second embodiment is the same as that of the organic solvent recovery system 1A described in the first embodiment above. The difference is that in the organic solvent recovery system 1B of the second embodiment, a three-way open/close valve V3 is provided on the desorption gas line 110 from the organic solvent recovery device 100. One downstream end of the open/close valve V3 is connected to the desorption gas inlet chamber 115C of the heat exchanger 115, and the other downstream end is connected to the condenser 111 via the condenser line 116. The open/close valve V3 can be used to switch between supplying the desorption gas to the heat exchanger 115 or to the condenser 111. Note that a similar switching operation may be performed by using multiple two-way open/close valves instead of the three-way open/close valve V3.
　実施の形態２の有機溶剤回収装置１００は脱着工程が前期の第１脱着工程と後期の第２脱着工程に分かれて動作する。第１処理槽１０４Ａの第１脱着工程（すなわち、図３に示すｔ０～ｔ１の間）においては、三方式の開閉バルブＶ３を操作することによって、脱着ガスがコンデンサライン１１６を通じてコンデンサ１１１に供給される。脱着工程の前期において、第１処理槽１０４Ａに供給された脱着用水蒸気の熱は第１吸着材１０５Ａや第１処理槽１０４Ａ本体、第１上ダンパ１０６Ａ、第１下ダンパ１０７Ａ、及び各配管ラインの加熱に多く消費されるため、第１処理槽１０４Ａから排出される脱着ガスの温度は低くなる。そのため、第１処理槽１０４Ａから排出される脱着ガスを熱交換器１１５に供給せず、コンデンサ１１１に直接供給することで、熱交換器１１５のチューブ１１５Ｂを高温の状態に維持することができ、結果として補給水ＶＩの蒸発が効率よく行われる。 In the organic solvent recovery apparatus 100 of the second embodiment, the desorption process is divided into a first desorption process in the early stage and a second desorption process in the later stage. In the first desorption process of the first treatment tank 104A (i.e., between t0 and t1 shown in FIG. 3), the desorption gas is supplied to the condenser 111 through the condenser line 116 by operating the three-way opening and closing valve V3. In the early stage of the desorption process, the heat of the desorption steam supplied to the first treatment tank 104A is largely consumed in heating the first adsorbent 105A, the first treatment tank 104A main body, the first upper damper 106A, the first lower damper 107A, and each piping line, so that the temperature of the desorption gas discharged from the first treatment tank 104A is low. Therefore, by supplying the desorbed gas discharged from the first treatment tank 104A directly to the condenser 111 instead of to the heat exchanger 115, the tube 115B of the heat exchanger 115 can be maintained at a high temperature, resulting in efficient evaporation of the makeup water VI.
　脱着ガスの温度が高温の状態（７０～１２０℃程度）になった時点で、三方式の開閉バルブＶ３を操作することによって、脱着ガスを熱交換器１１５に供給し、第１処理槽１０４Ａの第２脱着工程（すなわち、図３に示すｔ１～ｔ２の間）を開始する。 When the temperature of the desorption gas reaches a high temperature (approximately 70 to 120°C), the three-way open/close valve V3 is operated to supply the desorption gas to the heat exchanger 115, and the second desorption step of the first treatment tank 104A (i.e., between t1 and t2 shown in Figure 3) begins.
　第１脱着工程から第２脱着工程へ切り替えるタイミングは、第１脱着工程において処理槽から排出される脱着ガスの温度が高温の状態に達するまでの時間をあらかじめ測定しておいて決定すればよい。また、外気温の変動等により処理槽から排出される脱着ガスの温度が高温の状態に達するまでの時間が変動する場合は、処理槽から排出される脱着ガスの温度を測定する温度センサーを設け、温度センサーで検出された脱着ガスの温度が高温の状態に達した時点で自動的に第１脱着工程から第２脱着工程へ切り替えるように制御してもよい。 The timing for switching from the first desorption process to the second desorption process may be determined by measuring in advance the time it takes for the temperature of the desorption gas discharged from the treatment tank to reach a high temperature in the first desorption process. In addition, if the time it takes for the temperature of the desorption gas discharged from the treatment tank to reach a high temperature varies due to fluctuations in the outside air temperature, etc., a temperature sensor may be provided to measure the temperature of the desorption gas discharged from the treatment tank, and the process may be controlled to automatically switch from the first desorption process to the second desorption process when the temperature of the desorption gas detected by the temperature sensor reaches a high temperature.
　第１脱着工程において、熱交換器１１５のシェル側に水蒸気ＶＩＩを供給し、第２脱着工程において、熱交換器１１５のシェル側に水蒸気ＶＩＩを供給しないように制御すれば、脱着工程の前期の再生水蒸気の流量を十分確保できる上に水蒸気ＶＩＩの使用量を削減できるため、好ましい。 In the first desorption step, steam VII is supplied to the shell side of the heat exchanger 115, and in the second desorption step, steam VII is controlled not to be supplied to the shell side of the heat exchanger 115, which is preferable because it ensures a sufficient flow rate of regenerated steam in the early stage of the desorption step and reduces the amount of steam VII used.
　実施の形態２の有機溶剤回収システム１Ｂによっても、上記実施の形態１の有機溶剤回収システム１Ａと同様の作用効果を得ることができる。 The organic solvent recovery system 1B of the second embodiment can achieve the same effects as the organic solvent recovery system 1A of the first embodiment.
　上記開示における有機溶剤回収装置１００においては、処理槽として、第１処理槽１０４Ａ及び第２処理槽１０４Ｂを用いて、吸着工程と脱着工程を交互に行なう有機溶剤の回収処理について説明したが、この２つの処理槽を用いる有機溶剤回収処理に限定されるものではなく、処理槽は３槽以上あってもよい。 In the organic solvent recovery device 100 disclosed above, the organic solvent recovery process is described as using a first treatment tank 104A and a second treatment tank 104B as treatment tanks, and alternately performing an adsorption process and a desorption process. However, the organic solvent recovery process is not limited to using these two treatment tanks, and there may be three or more treatment tanks.
　以上に開示された実施の形態はすべての点で例示であって制限的なものではないと考えられるべきである。本発明の範囲は上記した説明ではなくて請求の範囲によって示され、請求の範囲と均等の意味及び範囲内でのすべての変更が含まれることが意図される。 The embodiments disclosed above should be considered to be illustrative in all respects and not restrictive. The scope of the present invention is indicated by the claims, not the above description, and is intended to include all modifications within the meaning and scope of the claims.
＜実施例＞
　上記説明した図１に示す有機溶剤回収システム１Ａを用いて以下の処理を実施した。トルエンを２，０００ｐｐｍ含む４５℃、風量７Ｎｍ３／ｍｉｎを被処理ガスとし、被処理ガス送風機１０２により吸着工程となっている第２処理槽１０４Ｂに送風した。第１吸着材１０５Ａ及び第２吸着材１０５Ｂにはそれぞれ東洋紡社製の活性炭素繊維４ｋｇを使用した。吸着工程を１１分間実施した時点で吸着工程と脱着工程を切り替え、第２処理槽１０４Ｂには脱着用水蒸気を導入して脱着工程を９分間行った。 <Example>
The following treatment was carried out using the organic solvent recovery system 1A shown in Fig. 1 described above. The gas to be treated was 45°C containing 2,000 ppm of toluene and had an air volume of 7 Nm3 /min, and was blown into the second treatment tank 104B, which was in the adsorption process, by the gas to be treated blower 102. 4 kg of activated carbon fiber manufactured by Toyobo Co., Ltd. was used for each of the first adsorbent 105A and the second adsorbent 105B. When the adsorption process had been carried out for 11 minutes, the adsorption process and desorption process were switched, and desorption steam was introduced into the second treatment tank 104B, and the desorption process was carried out for 9 minutes.
　脱着工程中は水蒸気ＶＩＩＩが流量１６０ｇ／ｍｉｎで供給されるように調整した。さらに熱交換器１１５の圧力センサー１１５Ｆでシェル側の内圧が０．０６０ＭＰａを維持するように調整バルブＶ４の開度を自動調整し、水蒸気ＶＩＩを熱交換器１１５のシェル側へ供給した。補給水ＶＩは熱交換器１１５のチューブ１１５Ｂの半分が補給水ＶＩに浸漬するように補給水ＶＩを供給して水面高さを調整し、再生水蒸気を発生させた。発生した再生水蒸気はスチームコンプレッサー１２２に吸い込まれ、水蒸気ＶＩＩＩと混合された後、脱着用水蒸気として第２処理槽１０４Ｂに供給された。 During the desorption process, the flow rate of steam VIII was adjusted to 160 g/min. Furthermore, the opening of adjustment valve V4 was automatically adjusted so that the internal pressure on the shell side was maintained at 0.060 MPa by pressure sensor 115F of heat exchanger 115, and steam VII was supplied to the shell side of heat exchanger 115. Make-up water VI was supplied so that half of tube 115B of heat exchanger 115 was immersed in make-up water VI, adjusting the water level and generating regenerated steam. The generated regenerated steam was sucked into steam compressor 122, mixed with steam VIII, and then supplied to second treatment tank 104B as desorption steam.
　上記説明した吸着工程と脱着工程をそれぞれ１０サイクルずつ繰り返し実施した。１０サイクル後の有機溶剤の回収効率は９７％であった。 The adsorption and desorption processes described above were each repeated 10 cycles. After 10 cycles, the organic solvent recovery efficiency was 97%.
＜比較例＞
　水蒸気ＶＩＩを熱交換器１１５のシェル側へ供給しないこと以外は実施例と同様の方法で被処理ガスの処理を行った。その結果、１０サイクル後の有機溶剤の回収効率は９１％であり、実施例に対して回収効率が大幅に低下した。 Comparative Example
The gas to be treated was treated in the same manner as in the Example, except that steam VII was not supplied to the shell side of the heat exchanger 115. As a result, the recovery efficiency of the organic solvent after 10 cycles was 91%, which was significantly lower than the recovery efficiency in the Example.
　これら結果より、実施例では脱着用水蒸気の流量が十分確保され、有機溶剤の回収効率を向上させることが可能であることが分かる。 These results show that in the embodiment, the flow rate of water vapor for desorption is sufficiently ensured, making it possible to improve the recovery efficiency of organic solvents.
　本発明により、省エネルギーで有機溶剤の回収効率が向上した有機溶剤回収システムを提供することが可能となり、産業界へ大いに貢献できる。 The present invention makes it possible to provide an organic solvent recovery system that is energy-saving and improves the efficiency of organic solvent recovery, making a great contribution to the industrial world.
１Ａ，１Ｂ　有機溶剤回収システム、１００　有機溶剤回収装置、１０１　被処理ガスライン、１０２　被処理ガス送風機、１０３　被処理ガス導入ライン、１０４Ａ　第１処理槽、１０４Ｂ　第２処理槽、１０５Ａ　第１吸着材、１０５Ｂ　第２吸着材、１０６Ａ　第１上ダンパ、１０６Ｂ　第２上ダンパ、１０７Ａ　第１下ダンパ、１０７Ｂ　第２下ダンパ、１０８　脱着用水蒸気ライン、１１０　脱着ガスライン、１１１　コンデンサ（冷却部）、１１２　コンデンサ凝縮液ライン、１１３　セパレータ（凝縮液溜部）、１１３Ａ　回収溶剤、１１３Ｂ　分離排水、１１４　戻りガスライン、１１５　熱交換器、１１５Ａ　シェル（吸熱部、容器部）、１１５Ｂ　チューブ（発熱部、管部）、１１５Ｃ　脱着ガス入口チャンバー、１１５Ｄ　脱着ガス出口チャンバー（脱着ガス出口受部）、１１５Ｅ　補給水収容部、１１５Ｆ　圧力センサー（圧力測定部）、１１５Ｇ　制御部、１１６　コンデンサライン、１１７　熱交換器出口ガスライン、１１８　熱交換器凝縮液ライン、１１９　再生水蒸気ライン、１２０　熱交換器用水蒸気供給ライン（水蒸気供給部）、１２１　スチームコンプレッサー用水蒸気ライン、１２２　スチームコンプレッサー、Ｖ１　第１水蒸気開閉弁、Ｖ２　第２水蒸気開閉弁、Ｖ３　開閉バルブ、Ｖ４　調整バルブ、Ｉ　被処理ガス、ＩＩ　処理ガス、ＩＩＩ　回収溶剤、ＩＶ　分離排水、Ｖ，ＶＩＩ，ＶＩＩＩ　水蒸気、ＶＩ　補給水 1A, 1B organic solvent recovery system, 100 organic solvent recovery device, 101 treated gas line, 102 treated gas blower, 103 treated gas introduction line, 104A first treatment tank, 104B second treatment tank, 105A first adsorbent, 105B second adsorbent, 106A first upper damper, 106B second upper damper, 107A first lower damper, 107B second lower damper, 108 desorption water vapor line, 110 desorption gas line, 111 condenser (cooling section), 112 condenser condensate line, 113 separator (condensate reservoir section), 113A recovered solvent, 113B separated wastewater, 114 return gas line, 115 heat exchanger, 115A shell (heat absorption section, container section), 115B tube (heat generating section part, pipe part), 115C desorption gas inlet chamber, 115D desorption gas outlet chamber (desorption gas outlet receiving part), 115E makeup water storage part, 115F pressure sensor (pressure measurement part), 115G control part, 116 condenser line, 117 heat exchanger outlet gas line, 118 heat exchanger condensate line, 119 regenerated steam line, 120 heat exchanger steam supply line (steam supply part), 121 steam line for steam compressor, 122 steam compressor, V1 first steam on-off valve, V2 second steam on-off valve, V3 on-off valve, V4 adjustment valve, I gas to be treated, II treated gas, III recovered solvent, IV separated wastewater, V, VII, VIII steam, VI makeup water

Claims (8)

  1. 　有機溶剤を含有する被処理ガスから有機溶剤を吸着除去する吸着材が収容された処理槽を備え、前記処理槽に供給された前記被処理ガスを前記吸着材に接触させて処理ガスを排出する吸着処理と、前記処理槽に供給された脱着用水蒸気により前記吸着材から前記有機溶剤を脱着して脱着ガスを排出する脱着処理とを繰り返す有機溶剤回収装置と、
    　前記有機溶剤回収装置から排出された前記脱着ガスが通過する発熱部と、補給水が補給される吸熱部とを有し、当該発熱部を通過する前記脱着ガスにて、当該吸熱部の補給水を間接加熱して水蒸気を発生させ、間接加熱後の前記脱着ガスを排出する熱交換器と、
    　前記熱交換器から排出された前記脱着ガスを冷却して凝縮液を排出する冷却部と、を備えた有機溶剤回収システムであって、
    　前記熱交換器の前記吸熱部に水蒸気を供給する水蒸気供給部を備え、
    　前記熱交換器は、前記補給水から発生した水蒸気と前記水蒸気供給部から供給された水蒸気とが混合された再生水蒸気を、前記脱着用水蒸気の少なくとも一部として前記有機溶剤回収装置に供給する、有機溶剤回収システム。     an organic solvent recovery apparatus including a treatment tank containing an adsorbent that adsorbs and removes an organic solvent from a gas to be treated that contains the organic solvent, and repeats an adsorption process in which the gas to be treated that is supplied to the treatment tank is brought into contact with the adsorbent to discharge a treated gas, and a desorption process in which the organic solvent is desorbed from the adsorbent by a desorption steam supplied to the treatment tank and a desorbed gas is discharged;
    a heat exchanger including a heat generating section through which the desorption gas discharged from the organic solvent recovery apparatus passes and an endothermic section to which makeup water is replenished, the heat exchanger indirectly heating the makeup water of the endothermic section with the desorption gas passing through the heat generating section to generate steam, and discharging the indirectly heated desorption gas;
    a cooling unit that cools the desorption gas discharged from the heat exchanger and discharges a condensate,
    a water vapor supply unit that supplies water vapor to the heat absorption unit of the heat exchanger,
    the heat exchanger supplies regenerated steam, which is a mixture of steam generated from the make-up water and steam supplied from the steam supply unit, to the organic solvent recovery device as at least a part of the desorption steam.
  2. 　前記熱交換器の前記吸熱部の気相部分の圧力を測定する圧力測定部を備え、当該圧力測定部の測定結果により前記水蒸気供給部から前記熱交換器に供給される水蒸気の流量を制御する、請求項１に記載の有機溶剤回収システム。 The organic solvent recovery system according to claim 1, further comprising a pressure measuring unit that measures the pressure of the gas phase of the heat absorbing unit of the heat exchanger, and controls the flow rate of the water vapor supplied from the water vapor supply unit to the heat exchanger based on the measurement result of the pressure measuring unit.
  3. 　前記水蒸気供給部は、前記脱着処理の前期には、前記熱交換器に水蒸気を供給し、前記脱着処理の後期には、前記熱交換器に水蒸気を供給しない、請求項１又は２に記載の有機溶剤回収システム。 The organic solvent recovery system according to claim 1 or 2, wherein the water vapor supply unit supplies water vapor to the heat exchanger in the early stage of the desorption process and does not supply water vapor to the heat exchanger in the later stage of the desorption process.
  4. 　前記有機溶剤回収装置は、前記冷却部から排出される凝縮液を溜める凝縮液溜部を備え、
    　前記熱交換器は、間接加熱した後の前記脱着ガスが滞留する脱着ガス出口受部と、当該脱着ガス出口受部から未凝縮の前記脱着ガスを前記冷却部に供給する配管経路と、当該脱着ガス出口受部から凝縮液となった前記脱着ガスを前記凝縮液溜部に供給する配管経路と、を備える、請求項１又は２に記載の有機溶剤回収システム。     the organic solvent recovery apparatus includes a condensate reservoir that accumulates the condensate discharged from the cooling unit,
    3. The organic solvent recovery system according to claim 1, wherein the heat exchanger comprises: a desorbed gas outlet receiving section in which the desorbed gas after indirect heating accumulates; a piping path for supplying the uncondensed desorbed gas from the desorbed gas outlet receiving section to the cooling section; and a piping path for supplying the desorbed gas that has become a condensed liquid from the desorbed gas outlet receiving section to the condensed liquid reservoir section.
  5. 　前記処理槽から排出される前記脱着ガスを前記熱交換器の前記発熱部に供給する経路と、前記処理槽から排出される前記脱着ガスを前記冷却部に供給する経路と、を備える、請求項１又は２に記載の有機溶剤回収システム。 The organic solvent recovery system according to claim 1 or 2, comprising a path for supplying the desorption gas discharged from the treatment tank to the heat generating part of the heat exchanger, and a path for supplying the desorption gas discharged from the treatment tank to the cooling part.
  6. 　前記脱着処理の前期において、前記処理槽から排出される前記脱着ガスを前記冷却部に供給するとともに、前記水蒸気供給部から前記熱交換器の前記吸熱部に水蒸気を供給し、
    　前記脱着処理の後期において、前記処理槽から排出される前記脱着ガスを前記熱交換器の前記発熱部に供給するとともに、前記水蒸気供給部から前記熱交換器の前記吸熱部に水蒸気を供給しない、請求項５に記載の有機溶剤回収システム。     In an early stage of the desorption treatment, the desorption gas discharged from the treatment tank is supplied to the cooling section, and water vapor is supplied from the water vapor supply section to the heat absorption section of the heat exchanger;
    6. The organic solvent recovery system according to claim 5, wherein, in a later stage of the desorption treatment, the desorption gas discharged from the treatment tank is supplied to the heat generating section of the heat exchanger, and water vapor is not supplied from the water vapor supply section to the heat absorbing section of the heat exchanger.
  7. 　前記熱交換器は、前記吸熱部である容器部の内部に前記発熱部である管部を備えた多管式熱交換器である、請求項１又は２に記載の有機溶剤回収システム。 The organic solvent recovery system according to claim 1 or 2, wherein the heat exchanger is a multi-tube heat exchanger having a tube section, which is the heat generating section, inside a container section, which is the heat absorbing section.
  8. 　前記水蒸気供給部は、前記有機溶剤回収装置に前記脱着用水蒸気を直接供給する脱着用水蒸気供給部と接続している又は兼用されている、請求項１又は２に記載の有機溶剤回収システム。 The organic solvent recovery system according to claim 1 or 2, wherein the water vapor supply unit is connected to or serves as a desorption water vapor supply unit that directly supplies the desorption water vapor to the organic solvent recovery device.
PCT/JP2023/034491 2022-09-30 2023-09-22 Organic solvent recovery system WO2024070944A1 (en)

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS54149378A (en) * 1978-05-12 1979-11-22 Boewe Boehler & Weber Kg Masch Method and apparatus for regenerating adsorbent
JPS59115724A (en) * 1982-12-24 1984-07-04 Nittetsu Kakoki Kk Cooling method of adsorption tank using activated carbon
JPS62221418A (en) * 1986-03-24 1987-09-29 トレトマン・ド・ガ−ズ・エ・ジエニ・エンデユストリエル Method and apparatus for regenerating solvent adsorbed activated carbon
JPS6341702A (en) * 1986-08-06 1988-02-23 三菱重工業株式会社 Steam regenerating facility
JPS6425320U (en) * 1987-08-06 1989-02-13
JP2009072671A (en) * 2007-09-19 2009-04-09 Tsukishima Kankyo Engineering Ltd Gas treatment method

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS54149378A (en) * 1978-05-12 1979-11-22 Boewe Boehler & Weber Kg Masch Method and apparatus for regenerating adsorbent
JPS59115724A (en) * 1982-12-24 1984-07-04 Nittetsu Kakoki Kk Cooling method of adsorption tank using activated carbon
JPS62221418A (en) * 1986-03-24 1987-09-29 トレトマン・ド・ガ−ズ・エ・ジエニ・エンデユストリエル Method and apparatus for regenerating solvent adsorbed activated carbon
JPS6341702A (en) * 1986-08-06 1988-02-23 三菱重工業株式会社 Steam regenerating facility
JPS6425320U (en) * 1987-08-06 1989-02-13
JP2009072671A (en) * 2007-09-19 2009-04-09 Tsukishima Kankyo Engineering Ltd Gas treatment method

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