Classifications

• • 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
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
  • B01J20/20—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbon; comprising carbon obtained by carbonising processes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/30—Processes for preparing, regenerating, or reactivating
  • B01J20/34—Regenerating or reactivating

Definitions

• the present invention relates to an organic solvent recovery system.
• the organic solvent recovery device is equipped with a pair of treatment tanks that use an adsorbent to adsorb the organic solvents in the gas to be treated, a treated 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.
• Patent Document 1 discloses a gas treatment device in which activated carbon fibers are fixed to a support or self-supported in a cylindrical shape and arranged vertically within a core material.
• nonwoven activated carbon fibers are preferably used as an adsorbent capable of adsorbing organic solvents.
• the above-mentioned activated carbon fibers have an extremely fast rate of adsorbing organic solvents compared to granular activated carbon, so they can effectively adsorb and remove organic solvents.
• activated carbon fiber has an extremely fast rate of adsorbing and desorbing organic solvents, the weight of the fiber packed into the treatment tank can be reduced to about 1/15 to 1/100 of that of granular activated carbon.
• activated carbon fiber has a porosity of 90 to 98%, which is very bulky compared to granular activated carbon, which has a porosity of 33 to 45%, so the weight of activated carbon fiber that can be packed per unit volume of the treatment tank is smaller than that of granular activated carbon.
• activated carbon fiber exhibits high removal performance even with a small packed weight, which results in the organic solvent recovery device being made smaller (Non-Patent Document 1).
• Patent Document 2 also 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 a 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.
• 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 a line connecting the evaporation side of the heat exchanger to the desorption water vapor inlet of the activated carbon adsorber, and evaporating
• JP 2014-147864 A Japanese Utility Model Application Publication No. 58-161636
• activated carbon fiber has a higher porosity than general granular activated carbon or powdered activated carbon, so it takes time to replace the gas to be treated remaining in the treatment tank with the desorption water vapor in the desorption process.
• activated carbon fiber has an extremely fast rate of desorbing organic solvents compared to general granular activated carbon or powdered activated carbon, so the organic solvent adsorbed on the activated carbon fiber is rapidly desorbed in the early stage of the desorption process.
• the temperature of the desorption outlet gas discharged from the treatment tank hardly increases until the desorbed organic solvent is replaced by the desorption steam.
• the activated carbon fiber has a large external surface area, it rapidly absorbs the heat of the desorption steam in the early stage of the desorption process. As a result, the temperature of the desorption outlet gas discharged from the treatment tank hardly increases until the temperature of the activated carbon fiber has risen sufficiently.
• the present invention has been developed in consideration of the above problems, and its purpose is to provide an organic solvent recovery system that can improve the efficiency of organic solvent recovery and significantly reduce the amount of water vapor used by the entire facility.
• 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 a heat absorbing section to which makeup water is supplied, the heat exchanger indirectly heating the makeup water in the heat absorbing section with the desorption gas passing through the heat generating section to generate regenerated steam, and discharging the desorption gas after passing through the heat generating section; a regenerated steam supply passage for supplying the regenerated steam generated in the heat exchanger to the organic solvent recovery device as at least a part
• the organic solvent recovery system of the present invention may include a condensate reservoir that stores 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.
• the organic solvent recovery system of the present invention may supply the desorption gas discharged from the treatment tank to the cooling section during the early stage of the desorption process, and supply the desorption gas discharged from the treatment tank to the heat generating section of the heat exchanger during the later stage of the desorption process.
• the water vapor supply unit that supplies the desorption water vapor to the organic solvent recovery device may be connected to a direct path that supplies the desorption water vapor from the water vapor supply unit directly to the organic solvent recovery device, and a mixing path that mixes the desorption water vapor with the regenerated water vapor and 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 according to a first embodiment.
• FIG. 4 is a diagram showing a time chart illustrating the time switching between the adsorption process and the desorption process of the organic solvent recovery system according to the first embodiment. 4 is a graph showing a reduction rate of water vapor usage in the organic solvent recovery system according to the first embodiment.
• FIG. 11 is a conceptual diagram showing a configuration of an organic solvent recovery system according to a second embodiment.
• FIG. 1 is a conceptual diagram showing the configuration of an organic solvent recovery system equipped with three treatment tanks.
• the organic solvent in the present invention is methylene chloride, chloroform, carbon tetrachloride, ethylene chloride, trichloroethylene, tetrachloroethylene, o-dichlorobenzene, m-dichlorobenzene, fluorocarbon-112, fluorocarbon-113, hydrochlorocarbons (HCFCs), hydrofluorocarbons (HFCs), other perfluoroalkyl compounds and polyfluoroalkyl compounds (PFAS), 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, dibuty
• 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 apparatus 100, a heat exchanger unit 200, 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 cylindrical activated carbon fibers 105A
• the second treatment tank 104B includes cylindrical activated carbon fibers 105B.
• the gas I to be treated passes through the activated carbon fibers 105A and 105B from the outside to the inside to perform an adsorption step (adsorption treatment), and water vapor passes through the activated carbon fibers 105A and 105B from the inside to the outside to perform a desorption step (desorption treatment).
• 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 automatic lower damper 107A and a second automatic 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 automatic upper damper 106A and a second automatic 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 evaporation side of the heat exchanger 115.
• the makeup water VI is sent to the evaporation side of the heat exchanger 115 by, for example, a liquid delivery pump.
• the heat exchanger 115 indirectly heats the make-up water VI with the desorption gas supplied from the desorption gas line 110, thereby evaporating the make-up water VI and generating water vapor.
• the evaporation side of the heat exchanger 115 is decompressed so that the boiling point is, for example, 70°C to 99°C, preferably 75°C to 95°C, and the generated water vapor is supplied to the steam compressor 122 as regenerated water vapor IX 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 low-pressure water vapor (hereinafter, sucked water vapor) in a reduced pressure state and boost it 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 IX is sucked in as sucked water vapor through the regenerated water vapor line 119, and the desorption water vapor in which water vapor VIII and regenerated water vapor IX are mixed 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 evaporation side of the heat exchanger 115 is connected to a heat exchanger steam supply line 120, which is a steam supply unit 123 for supplying steam VII, which is a part of the steam V.
• a heat exchanger steam supply line 120 which is a steam supply unit 123 for supplying steam VII, which is a part of the steam V.
• the evaporation side of the heat exchanger 115 can be kept at a predetermined pressure or higher (for example, a gauge pressure of -0.080 MPa or higher), and the flow rate of the suction steam sucked into the steam compressor 122, i.e., the regenerated steam IX, 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 is maintained high.
• the heat exchanger 115 body and the make-up water 115E in the heat exchanger 115 can be maintained at a high temperature, and the make-up water 115E can be efficiently evaporated.
• the heat exchanger 115 is preferably 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. 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.
• makeup water 115E In shell 115A, makeup water 115E always remains in an amount that contacts a part of tube 115B. When makeup water 115E comes into contact with tube 115B, makeup water 115E 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 for heating makeup water VI.
• the heat exchanger 115 preferably adjusts the water level of the make-up water 115E so that a part of the tube 115B does not come into contact with the make-up water 115E. Specifically, a part of the tube 115B is located in the gas phase part in the shell 115A between the water level of the make-up water 115E and the regenerated steam line 119. The regenerated steam IX is heated by the tube 115B located in the gas phase part in the shell 115A, and it is possible to prevent the regenerated steam IX from condensing before being sucked into the steam compressor 122.
• a means for adjusting the water level of the make-up water 115E for example, a control method using a float type, a spacer type, a differential pressure type, or a capacitance type liquid level gauge can be considered.
• 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 discharged after aeration using an aeration device.
• 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 in a counter flow 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 opening and closing 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 opening and closing valve V2.
• the first automatic upper damper 106A, the second automatic upper damper 106B, the first automatic lower damper 107A, the second automatic lower damper 107B, the first water vapor opening/closing valve V1, the second water vapor opening/closing 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) so as to realize the gas treatment method described below.
• FIG. 1 shows that a desorption process is carried out in a first treatment tank 104A of an organic solvent recovery apparatus 100, and an adsorption process is carried out in a second treatment tank 104B. The adsorption process and the desorption process are switched over in time according to the time chart shown in Fig. 2.
• the treated gas I containing an organic solvent-containing gas is sent from the treated gas line 101 to the second treatment tank 104B in the adsorption process by the treated gas blower 102.
• the second automatic lower damper 107B is controlled to open the treated gas inlet line 103 and close the desorption gas line 110.
• the second automatic upper damper 106B is controlled to an open state that allows the gas I to flow through the activated carbon fiber 105B.
• the organic solvent is adsorbed by the activated carbon fiber 105B in the second treatment tank 104B, and the treated gas II is discharged outside the system.
• the second water vapor opening/closing valve V2 in 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 automatic 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 automatic lower damper 107A blocks the flow of gas from the outside to the inside of the activated carbon fiber 105A.
• the water vapor for desorption is introduced through the water vapor line 108 to enable flow from the inside to the outside of the activated carbon fiber 105A.
• the first water vapor opening/closing valve V1 of the water vapor line 108 for desorption is controlled to be open.
• the steam for desorption is generated by mixing steam V and regenerated steam IX in the steam compressor 122.
• the steam compressor 122 is driven by steam supplied through the steam line 121 for the steam compressor, sucks in regenerated steam IX, which has been reduced in pressure, through the regenerated steam line 119, and discharges the desorption steam, which is a mixture of steam V and regenerated steam IX, through the desorption steam line 108.
• desorption steam is ejected, and the organic solvent adsorbed on the activated carbon fibers 105A becomes gas and is desorbed from the activated carbon fibers 105A.
• the desorption gas which is a mixture of the desorbed organic solvent and water vapor, is supplied to the tube side of the heat exchanger 115 and exchanges heat with the make-up water 115E that is retained on the shell side of the heat exchanger 115. Specifically, the make-up water 115E is indirectly heated through the heat transfer surface.
• the desorption gas After the desorption gas has completed heat exchange with makeup water 115E 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 return gas J introduced from the treated gas line 101 are sent to the second treatment tank 104B.
• the desorption outlet gas is supplied to the condensation side of the heat exchanger 115, and regenerated steam IX is generated by the evaporation of the makeup water 115E.
• the regenerated steam IX generated by the evaporation of the makeup water 115E is sucked into the steam compressor 122 through the regenerated steam line 119.
• a three-way regulating valve V3 is provided on the desorption gas line 110.
• One downstream end of the regulating 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 regulating 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 opening and closing valves instead of the three-way regulating valve V3.
• Figure 3 is a time chart showing the time-dependent switching between the adsorption process and the desorption process in the organic solvent recovery device 100. Below, the method in which the organic solvent recovery device 100 recovers the organic solvent will be described with reference to Figure 3.
• the organic solvent recovery apparatus 100 operates with the desorption process divided into desorption process 1 and desorption process 2.
• Desorption process 1 is the early stage of the desorption process
• desorption process 2 is the later stage of the desorption process.
• the desorption gas is supplied to the condenser 111 through the condenser line 116 by operating the adjustment valve V3.
• the adjustment valve V3 is operated to supply the desorption gas to the heat exchanger 115, and desorption process 2 in the first treatment tank 104A (i.e., between t1 and t2 shown in Figure 3) begins.
• the timing for switching from desorption process 1 to desorption process 2 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 desorption process 1. 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 control may be performed so that the desorption process is automatically switched from desorption process 1 to desorption process 2 when the temperature of the desorption gas detected by the temperature sensor reaches a high temperature.
• Figure 3 is a graph showing the reduction rate of water vapor usage in organic solvent recovery system 1A.
• the horizontal axis in the graph of Fig. 3 indicates the value of A/B, which is the ratio of the weight A [kg] of the activated carbon fiber contained in the treatment tank of the organic solvent recovery apparatus 100 to the internal volume B [ m3 ] of the treatment tank.
• the vertical axis in the graph of Fig. 3 indicates the reduction rate (%) of the amount of water steam used.
• the amount of water vapor desorbed can be measured, for example, by an ultrasonic, orifice, vortex, or area-type water vapor flow meter.
• the amount of regenerated water vapor can be measured, for example, by an ultrasonic, orifice, vortex, or area-type water vapor flow meter, or by a method for measuring the flow rate of make-up water.
• the reduction rate in water vapor usage is greater than 0%, it indicates that regenerated water vapor is being generated, and energy savings can be achieved.
• energy savings can be achieved when the A/B value is in the range of 12.0 or more.
• FIG. 4 is a diagram showing the configuration of the organic solvent recovery system 1B according to the second embodiment.
• 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 the organic solvent recovery system 1B of the second embodiment is provided with a steam compressor bypass line 124 that directly connects the water vapor supply unit 123 and the organic solvent recovery device 100.
• the opening of the adjustment valve V4 on the steam compressor bypass line is adjusted to supplement the desorption steam, thereby stabilizing the flow rate of the desorption steam.
• 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 above describes an organic solvent recovery process in which two treatment tanks, a first treatment tank 104A and a second treatment tank 104B, are used in the organic solvent recovery apparatus 100 to alternate between an adsorption process and a desorption process.
• the present invention is not limited to organic solvent recovery apparatuses that use two treatment tanks, and can be applied to, for example, an apparatus having three or more treatment tanks as shown in Figure 5.
• 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. and contained 4,000 ppm of ethyl acetate, and was blown into the second treatment tank 104B by the gas blower 102.
• 4 kg of activated carbon fiber manufactured by Toyobo Co., Ltd. was used for the activated carbon fibers 105A and 105B.
• the A/B ratios of the first treatment tank 104A and the second treatment tank 104B were all set to 19.0 by reducing the dead space of the opening and closing dampers of the first treatment tank 104A and the second treatment tank 104B.
• the flow rate of steam VIII was adjusted to 284 g/min.
• Make-up water VI was supplied so that half of the tubes 115B of the heat exchanger 115 were immersed in the make-up water 115E, and the water level was adjusted to generate regenerated steam IX.
• the generated regenerated steam IX was sucked into the steam compressor 122, mixed with steam V, and then supplied to the 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 a treatment tank having a larger dead space, such as an open/close damper, was used and A/B was set to 11.0. As a result, the recovery efficiency of the organic solvent after 10 cycles was 87%, which was significantly lower than that of the example.
• a treatment tank having a larger dead space such as an open/close damper
• the present invention makes it possible to provide an organic solvent recovery system that saves energy and improves the efficiency of organic solvent recovery, making a great contribution to the industrial sector.
• 1A, 1B organic solvent recovery system 100 organic solvent recovery device, 101 treated gas line, 102 treated gas blower, 103 treated gas inlet line, 104A first treatment tank, 104B second treatment tank, 105A activated carbon fiber, 105B activated carbon fiber, 106A first automatic upper damper, 106B second automatic upper damper, 107A first automatic lower damper, 10 7B second automatic lower damper, 108 desorption steam line, 110 desorption gas line, 111 condenser (cooling section), 112 condenser condensate line, 113 separator (condensate reservoir section), 113A recovery solvent, 113B separated drainage, 114 return gas line, 115 heat exchanger, 115A shell (heat absorption section, container section), 115B tube (heat generation section, tube section), 115C: desorption gas inlet chamber, 115D: desorption gas outlet chamber (desorption gas outlet receiving part), 115E: make-up water, 117: heat exchanger outlet gas line, 118: heat exchanger con

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