Solvent recovery device

Abstract

To improve a condensation efficiency of solvent gas in a solvent recovery device having a multi-tube type heat exchanger that receives supply of mixed gas comprising the solvent gas and a carrier.SOLUTION: A solvent recovery device is configured to liquefy and recover solvent gas from mixed gas comprising the solvent gas and carrier gas. The solvent recovery device includes a multi-tube type heat exchanger, an actuator and a control circuit. The multi-tube type heat exchanger includes: a plurality of tubes that are arranged in parallel and in which the mixed gas flows; and a shell that accommodates the plurality of tubes and in which a refrigerant flows around the plurality of tubes. The actuator is configured to change a total surface area that is a sum of surface areas of inner walls of one or a plurality of tubes in which the mixed gas flows out of the plurality of tubes. The control circuit is configured to control the actuator so as to change the total surface area in accordance with a concentration of the solvent gas in the mixed gas.SELECTED DRAWING: Figure 1

Description

Technical Field

[0001] The present disclosure relates to a solvent recovery device that liquefies and recovers solvent gas.

Background Art

[0002] Patent Document 1 discloses a device for cooling and liquefying natural gas. This device includes a shell-and-tube heat exchanger including a plurality of flow paths through which natural gas flows and a shell that houses the plurality of flow paths. In this device, the number of flow paths through which natural gas flows is controlled according to the flow rate of the natural gas.

[0003] Further, Patent Document 2 discloses a shell-and-tube condenser applied to a water-cooled refrigeration device. In this condenser, a configuration is adopted in which the density of heat transfer tubes on the contact surface with the gas refrigerant is decreased so that the arrangement of the heat transfer tubes in contact with the gas refrigerant near the partition portion that divides the cooling water passage becomes wavy. Furthermore, Patent Document 3 discloses a heat exchanger having a horizontal shell-and-tube structure. This heat exchanger includes a structure for expanding the contact area between the low-temperature heat medium in a liquid phase state and the heating gas in a heating gas transfer space portion that is a space inside an outer cylinder through which the heating gas flows in a low-temperature heat medium transfer space.

Prior Art Documents

Patent Documents

[0004]

Patent Document 1

Patent Document 2

Patent Document 3

Summary of the Invention

Problems to be Solved by the Invention

[0005] As described above, in the shell-and-tube heat exchanger described in Patent Document 1, the number of gas flow paths through which natural gas flows is selected based on the flow rate of natural gas. A shell-and-tube heat exchanger (multi-tube heat exchanger) can also be applied to a solvent recovery device that liquefies and recovers a solvent gas from a mixed gas of a solvent gas (vaporized solvent) and a carrier gas. However, in a solvent recovery device for such a mixed gas, if the number of tubes through which the mixed gas flows is determined based only on the flow rate of the mixed gas, the condensation efficiency of the solvent gas may be insufficient.

[0006] The present disclosure has been made in view of the above problems, and an object thereof is to improve the condensation efficiency of a solvent gas in a solvent recovery device having a multi-tube heat exchanger that receives a supply of a mixed gas of a solvent gas and a carrier.

Means for Solving the Problems

[0007] The solvent recovery device according to the present disclosure is configured to liquefy and recover a solvent gas from a mixed gas of a solvent gas and a carrier gas. The solvent recovery device includes a multi-tube heat exchanger, an actuator, and a control circuit. The multi-tube heat exchanger includes a plurality of tubes arranged in parallel through which the mixed gas flows, and a shell that houses the plurality of tubes and through which a refrigerant flows around the plurality of tubes. The actuator is configured to change the total surface area that is the sum of the surface areas of the inner walls of one or more of the plurality of tubes through which the mixed gas flows. The control circuit is configured to control the actuator so as to change the total surface area according to the concentration of the solvent gas in the mixed gas.

Effects of the Invention

[0008] According to the solvent recovery device of the present disclosure, by changing the above surface area according to the concentration of the solvent gas in the mixed gas, it is possible to improve the condensation efficiency of the solvent gas (in other words, the recovery rate of the solvent).

Brief Description of the Drawings

[0009]

Figure 1

Figure 2

Figure 3

Figure 4

Embodiments for Carrying Out the Invention

[0010] Embodiments of the present disclosure will be described with reference to the accompanying drawings.

[0011] 1. Configuration of the Solvent Recovery Apparatus FIG. 1 is a diagram schematically showing an example of the configuration of the solvent recovery apparatus 1 according to the embodiment. The solvent recovery apparatus 1 is configured to liquefy and recover the solvent gas from the mixed gas of the solvent gas (vaporized solvent) and the carrier gas. The upward direction on the paper surface of FIG. 1 corresponds to the vertically upward direction.

[0012] The solvent gas is the one obtained by gasifying the organic solvent (or simply the solvent) contained in the electrolyte of the lithium-ion battery. The solvent contains, for example, low-boiling solvents such as dimethyl carbonate (DMC) and ethyl methyl carbonate (EMC), and high-boiling solvents such as ethylene carbonate (EC). The electrolyte is impregnated in the electrode body. The solvent is gasified in a furnace (not shown) in the drying process of the electrode body performed when disassembling the lithium-ion battery. The solvent recovery apparatus 1 recovers the solvent gas generated in this drying process by distillation (more specifically, for example, vacuum distillation). The carrier gas is, for example, nitrogen.

[0013] The solvent recovery apparatus 1 includes a multi-tube heat exchanger (shell-and-tube heat exchanger) 10, a plurality of valves 20, a gas concentration sensor 31 and a gas flow sensor 32, a control circuit 40, a liquid recovery container 50, a discharge passage 51, a branch passage 52, and a pump 53.

[0014] The multi-tube heat exchanger (or simply heat exchanger) 10 includes an inlet chamber 11, a plurality of tubes (a plurality of heat transfer tubes) 12, a shell 13, and an outlet chamber 14. The inlet chamber 11 has an inlet 11a through which the mixed gas supplied from the furnace flows. Further, the inlet chamber 11 has a plurality of branch pipe portions 11b for flowing the mixed gas into the plurality of tubes 12 respectively. In the example shown in FIG. 1, the plurality of branch pipe portions 11b are arranged to be higher than the plurality of tubes 12 in the vertical direction.

[0015] The plurality of tubes 12 are arranged in parallel. The number of tubes 12 is not particularly limited. The tube 12 is a passage for flowing the mixed gas. The shell 13 is formed to accommodate the plurality of tubes 12 and allow the refrigerant to flow around the plurality of tubes 12. Specifically, the shell 13 has, for example, a cylindrical body portion 13a, and a pair of plates 13b and 13c located at each end of the body portion 13a. The pair of plates 13b and 13c has a plurality of openings for exposing the plurality of tubes 12 to the inlet chamber 11 and the outlet chamber 14 respectively.

[0016] The body portion 13a of the shell 13 has a refrigerant inlet 13d and an outlet 13e. The refrigerant flowing in the shell 13 exchanges heat with the mixed gas flowing in the plurality of tubes 12 through the plurality of tubes 12. The refrigerant is, for example, water. Alternatively, for example, when adopting a configuration in which the liquid recovery container 50 described later is cooled by a refrigeration chiller in order to more surely recover the solvent, an antifreeze liquid may be used as the refrigerant. An air-liquid mixed fluid containing the solvent condensed and liquefied during the passage of the plurality of tubes 12 flows out into the outlet chamber 14 together with the carrier gas.

[0017] The plurality of valves 20 are respectively provided in the plurality of branch pipe portions 11b. The valve 20 is, for example, an electromagnetic valve configured to open and close the branch pipe portion 11b. When the valve 20 is in the open state, the mixed gas is supplied from the inlet chamber 11 to the tube 12 corresponding to the valve 20. Each valve 20 is opened and closed in response to a command (electrical signal) from the control circuit 40. Therefore, by changing the number of valves 20 in the open state, the number of tubes 12 through which the mixed gas flows can be changed.

[0018] Changing the number of tubes 12 through which the mixed gas flows corresponds to changing the total surface area TSA of the plurality of tubes 12. The total surface area TSA here is the sum of the inner wall surface areas of one or more tubes 12 through which the mixed gas actually flows among the plurality of tubes 12 provided in the solvent recovery device 1. Thus, the plurality of valves 20 correspond to an example of the "actuator" according to the present disclosure.

[0019] Note that the change in the total surface area TSA may be performed, for example, by the following method instead of the method of changing the number of tubes 12 through which the mixed gas flows within one shell 13. That is, in an example of a solvent recovery device provided with a plurality of shells 13 configured to be able to change the number of shells 13 through which the mixed gas flows, changing the number of shells 13 through which the mixed gas flows corresponds to changing the total surface area TSA.

[0020] The gas concentration sensor 31 is configured to detect the concentration of the solvent gas in the mixed gas flowing into the multi-tube heat exchanger 10 (hereinafter, also simply referred to as "gas concentration C"). The gas concentration C is a weight percentage concentration. More specifically, the gas concentration sensor 31 is one or more gas concentration sensors that detect the gas concentration C of the solvent to be recovered (for example, each of DMC, EMC, and EC). As an example, the gas concentration sensor 31 is provided in the inlet chamber 11. As the gas concentration sensor 31, for example, a sensor of a potential detection method or a mass spectrometry method can be used. In addition, the sensor of the mass spectrometry method is suitable for the case of performing liquefaction recovery of the solvent gas in a reduced pressure state lower than the atmospheric pressure. Further, the gas flow rate sensor 32 is configured to detect the flow rate of the mixed gas flowing into the multi-tube heat exchanger 10. As an example, the gas flow rate sensor 32 is also provided in the inlet chamber 11.

[0021] The control circuit 40 controls the opening and closing of each of the plurality of valves 20. The control circuit 40 includes, for example, a switching circuit configured to output an electric signal for opening and closing the plurality of valves 20 in response to signals output from the gas concentration sensor 31 and the gas flow rate sensor 32. Further, the control circuit 40 controls the pump 53. The control circuit 40 includes, for example, a circuit that controls the pump 53 so as to operate when performing liquefaction recovery of the solvent using the heat exchanger 10. In addition, the control of the pump 53 by the control circuit 40 may include control of the carrier gas flow rate for adjusting the degree of vacuum inside the heat exchanger 10 and the furnace connected thereto. The operation of the pump 53 is stopped, for example, when the gas concentration C of the solvent to be recovered detected by the gas concentration sensor 31 drops below a predetermined determination value. That is, the liquefaction recovery of the solvent is completed.

[0022] The liquid recovery container 50 is located vertically below the heat exchanger 10. The liquid recovery container 50 is a container for recovering the liquefied solvent condensed by the heat exchanger 10. The discharge passage 51 connects between the outlet of the heat exchanger 10 (i.e., the outlet 14a of the outlet chamber 14) and the liquid recovery container 50. The discharge passage 51 is a passage through which the discharge fluid from the heat exchanger 10 (i.e., the gas-liquid mixed fluid containing the liquefied solvent and the carrier gas) flows.

[0023] The branch passage 52 communicates with the discharge passage 51. More specifically, in the example shown in FIG. 1, the branch passage 52 branches from the discharge passage 51. The branch passage 52 is a passage through which the carrier gas separated from the liquefied solvent flows. The pump 53 is provided in the branch passage 52. Thereby, among the discharge fluid flowing into the discharge passage 51, the liquefied solvent falls toward the liquid recovery container 50 by gravity and is recovered. On the other hand, by operating the pump 53, the carrier gas contained in the discharge fluid can be caused to flow into the branch passage 52 for degassing.

[0024] FIG. 2 is a diagram schematically showing another example of the gas-liquid separation structure of the discharge fluid. The example shown in FIG. 2 is different from the example shown in FIG. 1 in the configuration of the following liquid recovery container, discharge passage, and branch passage. The upward direction on the paper surface of FIG. 2 also corresponds to the vertically upward direction.

[0025] Similar to the example shown in FIG. 1, also in the example shown in FIG. 2, the liquid recovery container 60 is located vertically below the heat exchanger 10. And the discharge passage 51 connects between the outlet 14a of the heat exchanger 10 and the liquid recovery container 60. Moreover, in the example shown in FIG. 2, the branch passage 62 does not branch from the discharge passage 61 and is connected to the upper wall of the liquid recovery container 60. Also in this example, the branch passage 62 communicates with the discharge passage 61 through the space inside the liquid recovery container 60. The pump 53 is provided in the branch passage 62. Also according to the example shown in FIG. 2, among the discharge fluid flowing into the discharge passage 61, the liquefied solvent falls toward the bottom surface of the liquid recovery container 60 by gravity and is recovered. On the other hand, by operating the pump 53, the carrier gas contained in the discharge fluid can be caused to flow into the branch passage 62 for degassing.

[0026] 2. Control of the Number of Tubes (Total Surface Area) The concentration of the solvent gas (gas concentration C) in the mixed gas flowing into the multi-tube heat exchanger changes during the operation of the solvent recovery device 1. For example, the gas concentration C changes according to the change in the generation amount of the solvent gas during the period from the start to the end of the generation of the solvent gas in the furnace. Also, the gas concentration C changes according to the change in the carrier gas flow rate for adjusting the degree of vacuum.

[0027] As a result of the intensive research by the present inventors, it has been found that if the gas concentration C is too low or too high, the condensation efficiency of the solvent gas significantly decreases. Therefore, in a solvent recovery device targeting a mixed gas such as the solvent recovery device 1 of the present embodiment, if the number of tubes through which the mixed gas flows is determined based only on the flow rate of the mixed gas, the condensation efficiency may become insufficient.

[0028] More specifically, for example, when the number of tubes is increased when the gas concentration C is low and the carrier gas flow rate is large, the concentration of the solvent gas per tube may become excessively low. As a result, the condensation efficiency significantly decreases. Also, when the number of tubes is decreased when the gas concentration C is high and the carrier gas flow rate is small, the concentration of the solvent gas per tube may become excessively high. Also in this case, the condensation efficiency significantly decreases.

[0029] In view of the above problems, in the present embodiment, when liquefying and recovering the solvent gas from the mixed gas, the control circuit 40 controls the plurality of valves 20 so as to change the number of tubes 12 through which the mixed gas flows according to the gas concentration C. In other words, the control circuit 40 controls the plurality of valves 20 so as to change the total surface area TSA according to the gas concentration C. More specifically, the control circuit 40 transmits an electric signal for controlling the plurality of valves 20 in this way to the plurality of valves 20.

[0030] The control of the number of tubes 12 according to the gas concentration C is executed, for example, as in the following first and second control examples.

[0031] 2-1. First Control Example FIG. 3 is a diagram for explaining a first control example of the number of tubes 12 through which a mixed gas flows. In the first control example, the number of tubes 12 is controlled based only on the gas concentration C detected by the gas concentration sensor 31.

[0032] Specifically, the assumed maximum concentration value (or simply the maximum value) Cmax shown in FIG. 2 corresponds to the maximum value of the gas concentration C assumed during the operation of the solvent recovery apparatus 1. The heat exchanger 10 including the plurality of tubes 12 and the shell 13 is designed to have a heat exchange capacity capable of appropriately condensing the solvent gas below the maximum value Cmax in consideration of the type of the solvent to be recovered together with the maximum value Cmax.

[0033] In the first control example, three threshold values Cth1 to Cth3 are used as the threshold value Cth of the gas concentration C. In FIG. 2, four ranges R1 to R4 of the gas concentration C are specified by the maximum value Cmax and the three threshold values Cth1 to Cth3. That is, the first concentration range R1 includes the maximum value Cmax (for example, with the maximum value Cmax as the upper limit) and indicates a range higher than the threshold value Cth1. The second concentration range R2 indicates a range below the threshold value Cth1 and higher than the threshold value Cth2. The third concentration range R3 indicates a range below the threshold value Cth2 and higher than the threshold value Cth3. The fourth concentration range R4 indicates a range below the threshold value Cth3.

[0034] When the gas concentration C is within the first concentration range R1, the control circuit 40 controls the plurality of valves 20 to open all of the tubes 12 having the maximum number Nmax, that is, all of the plurality of tubes 12. In other words, the control circuit 40 controls the plurality of valves 20 so as to obtain the maximum value among a plurality of values selectable as the total surface area TSA.

[0035] On the one hand, when the gas concentration C is lower than the first concentration range R1, the control circuit 40 controls the plurality of valves 20 to open a number of tubes 12 that is less than the maximum number Nmax among the plurality of tubes 12. In other words, the control circuit 40 controls the plurality of valves 20 so that a value lower than the maximum value is obtained among the plurality of values selectable as the total surface area TSA.

[0036] More specifically, in an example shown in FIG. 3, in the second concentration range R2, the first intermediate number Nmed1 of tubes 12 that is less than the maximum number Nmax is opened. In the third concentration range R3, the second intermediate number Nmed2 of tubes 12 that is less than the first intermediate number Nmed1 is opened. In the fourth concentration range R4, the minimum number Nmin of tubes 12 that is less than the second intermediate number Nmed2 is opened. Note that the minimum number Nmin is not limited to one, and may be less than the second intermediate number Nmed2. Also, the number of threshold values Cth is not limited to three, and may be one or a plurality other than three.

[0037] In addition, the number of tubes 12 through which the mixed gas flows in each threshold value Cth1 to Cth3 of the gas concentration C and each concentration range R1 to R4 is determined in advance so that the concentration of the solvent gas per tube 12 can be maintained within an appropriate range in each concentration range R1 to R4.

[0038] 2-2. Second control example FIG. 4 is a diagram for explaining a second control example of the number of tubes 12 through which the mixed gas flows. In the second control example, the number of tubes 12 is controlled based on the gas concentration C detected by the gas concentration sensor 31 and the gas flow rate F detected by the gas flow rate sensor 32.

[0039] Also in the second control example, three threshold values Cth1 to Cth3 are used as the threshold value Cth of the gas concentration C. Further, in the second control example, three threshold values Fth1 to Fth3 are used as the threshold value Fth of the gas flow rate F. Among the three threshold values Fth1 to Fth3, the threshold value Fth1 is the highest, followed by the threshold values Fth2 and Fth3 in that order. Note that, similar to the threshold value Cth, the number of the threshold values Fth is not limited to three, and may be one or a plurality other than three.

[0040] In the second control example, even if the gas concentration C is the same value, the number of tubes 12 through which the mixed gas flows may be changed according to the flow rate of the mixed gas (gas flow rate F) flowing into the heat exchanger 10. Specifically, even if the gas concentration C is the same value, when the gas flow rate F is high, the control circuit 40 may control the plurality of valves 20 so that the number of tubes 12 is smaller (in other words, the total surface area TSA is smaller) than when the gas flow rate F is low.

[0041] In an example shown in FIG. 4, when the gas concentration C is within the first concentration range R1, if the gas flow rate F is equal to or less than the threshold value Fth3, the maximum number Nmax is selected. On the other hand, if the gas flow rate F is higher than the threshold value Fth3 and equal to or less than the threshold value Fth2, the first intermediate number Nmed1 is selected. If the gas flow rate F is higher than the threshold value Fth2 and equal to or less than the threshold value Fth1, the second intermediate number Nmed2 is selected. If the gas flow rate F is higher than the threshold value Fth1, the minimum number Nmin is selected.

[0042] Also, in an example shown in FIG. 4, when the gas concentration C is within the second concentration range R2, if the gas flow rate F is equal to or less than the threshold value Fth3, the first intermediate number Nmed1 is selected. On the other hand, if the gas flow rate F is higher than the threshold value Fth3 and equal to or less than the threshold value Fth2, the second intermediate number Nmed2 is selected. If the gas flow rate F is higher than the threshold value Fth2, the minimum number Nmin is selected.

[0043] Also, in an example shown in FIG. 4, when the gas concentration C is within the third concentration range R3, if the gas flow rate F is equal to or less than the threshold value Fth3, the second intermediate number Nmed2 is selected. On the other hand, if the gas flow rate F is higher than the threshold value Fth3, the minimum number Nmin is selected.

[0044] In addition, the number of tubes 12 through which the mixed gas flows in each threshold value Cth1 to Cth3 of the gas concentration C, each threshold value Fth1 to Fth3 of the gas flow rate F, and each concentration range R1 to R4 is determined in advance so that the concentration of the solvent gas per tube 12 can be maintained within an appropriate range in each concentration range R1 to R4.

[0045] 3. Effects As described above, according to the solvent recovery apparatus 1 according to the present embodiment, the control circuit 40 controls the plurality of valves 20 so as to change the number of tubes 12 (i.e., the total surface area TSA) through which the mixed gas flows according to the gas concentration C. As a result, under various gas concentrations C, the heat exchange area with the mixed gas in the heat exchanger 10 can be controlled to an appropriate state. Thereby, it becomes possible to improve the condensation efficiency of the solvent gas (in other words, the solvent recovery rate).

[0046] More specifically, according to the first control example, when the gas concentration C is within the first concentration range R1, the maximum number Nmax is selected as the number of tubes 12 through which the mixed gas flows. On the other hand, when the gas concentration C is lower than the first concentration range R1, a number of tubes 12 less than the maximum number Nmax are selected. In this way, when the gas concentration C is low, by flowing the mixed gas intensively through some of the tubes 12, the concentration of the solvent gas per tube 12 can be appropriately controlled from the viewpoint of condensation efficiency.

[0047] Also, according to the second control example, even when the gas concentration C is the same value, when the gas flow rate F is large, the plurality of valves 20 are controlled so that the number of tubes 12 is smaller than when the gas flow rate F is small (in other words, so that the total surface area TSA becomes smaller). By considering the gas flow rate F together with the gas concentration C in this way, it becomes possible to control the heat exchange area with the mixed gas in the heat exchanger 10 to a more appropriate state. As a result, it becomes possible to more effectively improve the condensation efficiency of the solvent gas.

[0048] In addition, the solvent recovery apparatus 1 according to the present embodiment includes a branch passage 52 or 62 that communicates with the discharge passage 51 or 61 and through which the carrier gas separated from the liquefied solvent flows. Thereby, degassing of the carrier gas can be performed favorably.

[0049] Also, more generally, the plurality of valves 20 (actuators) only need to be able to change the number of tubes 12 through which the mixed gas flows. For example, they may be provided on the plurality of tubes 12 themselves. On the other hand, in the solvent recovery apparatus 1 according to the present embodiment, the plurality of valves 20 are respectively provided in a plurality of branch pipe portions 11b arranged higher than the plurality of tubes (a plurality of heat transfer tubes) 12 in the vertical direction. Thereby, while avoiding the accumulation of the liquefied solvent on the closed valve 20, it becomes possible to change the number of tubes 12 through which the mixed gas flows by controlling the plurality of valves 20.

Explanation of Reference Numerals

[0050] 1 Solvent recovery apparatus, 10 Multi-tubular heat exchanger, 11 Inlet chamber, 11b Branch pipe portion, 12 Tube, 13 Shell, 14 Outlet chamber, 20 Valve, 30 Control circuit, 31 Gas concentration sensor, 32 Gas flow rate sensor, 40 Control circuit, 50, 60 Liquid recovery container, 51, 61 Discharge passage, 52, 62 Branch passage, 53 Pump

Claims

1. A solvent recovery device that liquefies and recovers the solvent gas from a mixed gas of a solvent gas and a carrier gas, comprising: A multi-tube heat exchanger including a plurality of tubes arranged in parallel through which the mixed gas flows, and a shell that houses the plurality of tubes and through which a refrigerant flows around the plurality of tubes; An actuator that changes the total surface area, which is the sum of the surface areas of the inner walls of one or more tubes through which the mixed gas flows among the plurality of tubes; A control circuit that controls the actuator so as to change the total surface area according to the concentration of the solvent gas in the mixed gas; A solvent recovery device comprising: A solvent recovery device.

2. The solvent recovery device according to claim 1, wherein: The control circuit: When the concentration is within a first concentration range including the assumed maximum concentration value, controls the actuator so as to obtain the maximum value among a plurality of selectable values as the total surface area; When the concentration is lower than the first concentration range, controls the actuator so as to obtain a value lower than the maximum value among the plurality of values. A solvent recovery device.

3. The solvent recovery device according to claim 1, wherein: The control circuit controls the actuator so that when the flow rate of the mixed gas flowing into the multi-tube heat exchanger is high even if the concentration is the same value, the total surface area is smaller than when the flow rate is low. A solvent recovery device.

4. The solvent recovery device according to any one of claims 1 to 3, further comprising: A liquid recovery container located vertically below the multi-tube heat exchanger and recovering the liquefied solvent condensed by the multi-tube heat exchanger; A discharge passage connecting between the outlet of the multi-tube heat exchanger and the liquid recovery container through which a discharge fluid containing the liquefied solvent and the carrier gas flows; A branch passage communicating with the discharge passage and through which the carrier gas separated from the liquefied solvent flows. A solvent recovery device further comprising: A solvent recovery device.

5. The solvent recovery device according to any one of claims 1 to 3, wherein: The multi-tube heat exchanger includes an inlet chamber into which the mixed gas flows; The inlet chamber includes a plurality of branch pipe portions for flowing the mixed gas into the plurality of tubes respectively; The plurality of branch pipe portions are arranged higher than the plurality of tubes in the vertical direction; The actuator is a plurality of valves respectively provided on the plurality of branch pipe portions and opening and closing the plurality of branch pipe portions respectively. A solvent recovery device.

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