JP2010240629A - Carbon dioxide recovery system - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To reduce heat energy required in an absorption liquid regeneration process in a carbon dioxide recovery system. <P>SOLUTION: Between an absorption tower 3 for making an absorption liquid absorb carbon dioxide included in a combustion exhaust gas and a regeneration tower 5 for regenerating the absorption liquid supplied from the absorption tower and discharging a discharge gas containing emitted carbon dioxide gas and steam, a regenerated heat exchanger 7 is provided which heats the absorption liquid which has absorbed the carbon dioxide and supplied from the absorption tower to the regeneration tower with the regenerated absorption liquid supplied from the regeneration tower to the absorption tower as a heat source. Also, between the absorption tower and the regenerated heat exchanger or between the regenerated heat exchanger and the regeneration tower, a heat exchanger 20 is provided which heats the absorption liquid which has absorbed the carbon dioxide and supplied from the absorption tower to the regeneration tower with the discharge gas discharged from the regeneration tower as a heat source. <P>COPYRIGHT: (C)2011,JPO&INPIT

Description

  The present invention relates to a carbon dioxide recovery system.

  In recent years, as one of the causes of global warming, the greenhouse effect of carbon dioxide contained in combustion exhaust gas generated when burning fossil fuel has been pointed out. To address this issue, countries are working to reduce greenhouse gas emissions in accordance with the Kyoto Protocol to the United Nations Framework Convention on Climate Change.

  Under such circumstances, in a thermal power plant that uses a large amount of fossil fuel, the combustion exhaust gas produced by burning fossil fuel is brought into contact with the amine-based absorbent, and carbon dioxide is separated and recovered from the combustion exhaust gas. However, a method for storing the recovered carbon dioxide without releasing it into the atmosphere has been studied.

  Specifically, an absorption tower that absorbs carbon dioxide contained in combustion exhaust gas in an amine-based absorption liquid and an absorption liquid (rich liquid) that has absorbed carbon dioxide are supplied from the absorption tower, the rich liquid is heated, and the rich liquid A carbon dioxide recovery system including a regeneration tower for releasing carbon dioxide gas from the water and regenerating an absorbing solution is known (see, for example, Patent Document 1). A reboiler for supplying a heat source is connected to the regeneration tower. The absorption liquid (lean liquid) regenerated in the regeneration tower is supplied to the absorption tower, and the absorption liquid circulates in this system.

  Since the carbon dioxide recovery system as described above is installed in addition to existing power generation facilities and the like, it is required to reduce its operating cost as much as possible. Particularly, in the regeneration step of the absorbing liquid in the regeneration tower, a large amount of heat energy is required to release carbon dioxide gas from the rich liquid. Therefore, in order to reduce the operating cost of the carbon dioxide recovery system, it is important to reduce the thermal energy required in the absorption liquid regeneration process.

JP-A-2005-254212

  An object of this invention is to provide the carbon dioxide recovery system which reduced the thermal energy required by the reproduction | regeneration process of an absorption liquid, and reduced the operating cost.

  A carbon dioxide recovery system according to an aspect of the present invention is provided with an absorption tower that absorbs carbon dioxide contained in combustion exhaust gas into an absorption liquid, an absorption liquid that absorbs carbon dioxide from the absorption tower, and vapor from the absorption liquid. A regeneration tower for releasing the carbon dioxide gas containing the carbon dioxide gas and regenerating the absorption liquid, and discharging the exhaust gas containing the released carbon dioxide gas and steam; and the regeneration tower is provided between the absorption tower and the regeneration tower. Using the regenerated absorption liquid supplied from the tower to the absorption tower as a heat source, the regenerative heat exchanger for heating the absorption liquid that has absorbed carbon dioxide supplied from the absorption tower to the regeneration tower, the absorption tower, and the Provided between the regenerative heat exchanger or between the regenerative heat exchanger and the regenerator, and supplied from the absorption tower to the regenerator with the exhaust gas discharged from the regenerator as a heat source A heat exchanger for heating the absorbing solution having absorbed carbon dioxide, in which comprises a.

  According to the present invention, it is possible to reduce the thermal energy required in the absorption liquid regeneration step and reduce the operating cost of the carbon dioxide recovery system.

1 is a schematic configuration diagram of a carbon dioxide recovery system according to a first embodiment of the present invention. It is a schematic block diagram of the carbon dioxide collection system by a modification. It is a schematic block diagram of the carbon dioxide collection system which concerns on the 2nd Embodiment of this invention. It is a schematic block diagram of the carbon dioxide recovery system which concerns on the 3rd Embodiment of this invention. It is a schematic block diagram of the carbon dioxide collection system which concerns on the 4th Embodiment of this invention. It is a schematic block diagram of the carbon dioxide recovery system which concerns on the 5th Embodiment of this invention. It is a schematic block diagram of the carbon dioxide collection system which concerns on the 6th Embodiment of this invention.

  Hereinafter, embodiments of the present invention will be described with reference to the drawings.

  (First Embodiment) FIG. 1 shows a schematic configuration of a carbon dioxide recovery system according to a first embodiment of the present invention. Here, the carbon dioxide recovery system recovers carbon dioxide contained in combustion exhaust gas generated by the combustion of fossil fuel using an absorbing liquid capable of absorbing carbon dioxide.

  As shown in FIG. 1, the carbon dioxide recovery system 1 includes an absorption tower 3 that absorbs carbon dioxide contained in the combustion exhaust gas 2a into an absorption liquid, and an absorption liquid that absorbs carbon dioxide from the absorption tower 3 (hereinafter, rich liquid 4a and A regenerating tower that heats the rich liquid 4a, releases carbon dioxide gas containing vapor from the absorbing liquid, discharges exhaust gas 2c containing carbon dioxide gas and steam, and regenerates the absorbing liquid 5. For example, the combustion exhaust gas 2a generated in a power generation facility such as a thermal power plant is supplied to the lower part of the absorption tower 3, and the combustion exhaust gas 2b from which carbon dioxide has been removed is discharged from the top of the absorption tower 3. .

  The absorption tower 3 has an absorption tower tank 3a for storing the rich liquid 4a generated by the absorption liquid absorbing carbon dioxide. Similarly, the regeneration tower 5 has a regeneration tower tank 5a that stores an absorbing liquid regenerated by releasing the carbon dioxide gas from the rich liquid 4a (hereinafter referred to as a lean liquid 4b).

  Here, as the absorbing solution capable of absorbing carbon dioxide, for example, an amine compound aqueous solution in which an amine compound is dissolved in water is used.

  As shown in FIG. 1, a reboiler 6 is provided in the regeneration tower 5. The reboiler 6 generates a steam by heating a part of the lean liquid 4b stored in the regeneration tower tank 5a by using plant steam or the like supplied from the power generation equipment as a heat source to increase the temperature thereof. To supply. When heating the lean solution 4b in the reboiler 6, a small amount of carbon dioxide gas is released from the lean solution 4b and supplied to the regeneration tower 5 together with the vapor. Then, the rich liquid 4a is heated in the regeneration tower 5 by this steam, and carbon dioxide gas is released.

  Regeneration heat exchange between the absorption tower 3 and the regeneration tower 5 using the lean liquid 4b supplied from the regeneration tower 5 to the absorption tower 3 as a heat source and heating the rich liquid 4a supplied from the absorption tower 3 to the regeneration tower 5. A vessel 7 is provided and configured to recover the heat of the lean liquid 4b. Here, as described above, when the carbon dioxide gas is released from the rich liquid 4 a in the regeneration tower 5, the rich liquid 4 a is heated using high-temperature steam from the reboiler 6 as a heat source. Accordingly, the temperature of the lean liquid 4b supplied to the regenerative heat exchanger 7 is relatively high, and this lean liquid 4b is used as a heat source.

  A first rich liquid line 8 for supplying the rich liquid 4a from the bottom of the absorption tower tank 3a to the regenerative heat exchanger 7 is connected between the absorption tower 3 and the regenerative heat exchanger 7. A rich liquid pump 9 for sending the rich liquid 4 a from the absorption tower 3 to the regenerative heat exchanger 7 is provided in the first rich liquid line 8.

  Between the regeneration heat exchanger 7 and the regeneration tower 5, a second rich liquid line 10 for supplying the rich liquid 4a from the regeneration heat exchanger 7 to the upper portion of the regeneration tower 5 is connected.

  Between the regeneration tower 5 and the regeneration heat exchanger 7, a first lean liquid line 11 for supplying the lean liquid 4b to the regeneration heat exchanger 7 from the bottom of the regeneration tower tank 5a is connected.

  The lean liquid 4 b from the regenerative heat exchanger 7 is supplied to the upper part of the absorption tower 3 by the lean liquid pump 12. The lean liquid 4b is cooled by the absorption liquid cooler 13 before being supplied to the absorption tower 3. The absorption liquid cooler 13 uses cooling water (cooling medium) as a cooling source.

  The lean liquid 4b supplied to the upper part of the absorption tower 3 descends from the upper part toward the absorption tower tank 3a in the absorption tower 3. On the other hand, the combustion exhaust gas 2 a supplied to the absorption tower 3 rises from the lower part toward the top in the absorption tower 3. Therefore, the combustion exhaust gas 2a containing carbon dioxide and the lean liquid 4b come into countercurrent contact (direct contact), carbon dioxide is removed from the combustion exhaust gas 2a and absorbed by the lean liquid 4b, and the rich liquid 4a is generated. The combustion exhaust gas 2b from which carbon dioxide has been removed is discharged from the top of the absorption tower 3, and the rich liquid 4a is stored in the absorption tower tank 3a of the absorption tower 3.

  The exhaust gas 2 c containing carbon dioxide gas and steam discharged from the regeneration tower 5 is sent to the gas-liquid separator 21 through the heat exchanger 20 provided in the second rich liquid line 10. The exhaust gas 2 c and the rich liquid 4 a exchange heat with the heat exchanger 20. As a result, the rich liquid 4a is heated before being supplied to the regeneration tower 5.

In the gas-liquid separator 21, the exhaust gas 2 c is separated into a gas (carbon dioxide) 23 and a liquid (water) 24. The gas 23 released from the top of the gas-liquid separator 21 is cooled by the gas cooler 14 and supplied to the gas-liquid separator 15. The gas-liquid separator 15 condenses (cools) the gas 23 to separate the carbon dioxide gas (gas phase component) and the generated condensate (liquid phase component). The carbon dioxide gas 2d discharged from the gas-liquid separator 15 is stored in a storage facility (not shown). The gas cooler 14 cools the gas 23 using cooling water (cooling medium). The condensate 16 in the gas-liquid separator 15 is supplied to the upper part of the regeneration tower 5 by a condensate pump 17.

  The liquid (water) 24 in the gas-liquid separator 21 is discharged from the bottom of the gas-liquid separator 21 and sent to the second rich liquid line 10 by the pump 22. The liquid 24 can be further heated by the liquid 24.

  When the absorption liquid is heated in the regeneration tower 5, the water in the absorption liquid evaporates. Therefore, a part of the heat energy supplied by the reboiler 6 is consumed as latent heat of vaporization of water. That is, a part of the thermal energy supplied by the reboiler 6 is not used for dissociation of carbon dioxide in the absorbing liquid.

  Therefore, in the present embodiment, the latent heat of vaporization of water is used to exchange heat between the exhaust gas 2c from the regeneration tower 5 and the rich liquid 4a to heat the rich liquid 4a. As a result, the rich liquid 4a heated by the regenerative heat exchanger 7 can be further heated, and the necessary heat energy can be reduced by the reboiler 6.

  For example, the rich liquid 4 a is heated by the regenerative heat exchanger 7 to about 100 ° C., and further heated by the heat exchanger 20 to about 105 ° C. The amount of heat energy required by the reboiler 6 can be reduced by the amount of the rich liquid 4a increased by 5 ° C.

  Since the carbon dioxide recovery system according to the present embodiment heats the rich liquid 4a using the residual heat of the exhaust gas 2c, the reboiler 6 is used rather than the case where the exhaust gas 2c from the regeneration tower 5 is sent directly to the gas cooler 14. This reduces the required heat energy.

  In the present embodiment, the pump 22 that sends the liquid (water) 24 in the gas-liquid separator 21 to the second rich liquid line 10 is compared with the case where the exhaust gas 2 c from the regeneration tower 5 is sent to the gas cooler 14. Although the operation cost is excessive, this is smaller than the amount of heat energy required for the reboiler 6 can be reduced, and the operation cost of the entire carbon dioxide recovery system can be reduced.

  In this way, by heating the rich liquid 4a using the heat of the exhaust gas 2c from the regeneration tower 5, the thermal energy required in the regeneration process of the absorbing liquid is reduced, and the operating cost of the carbon dioxide recovery system is reduced. Can be reduced.

  In the first embodiment, as shown in FIG. 1, the heat exchanger 20 is provided between the regeneration heat exchanger 7 and the regeneration tower 5 (second rich liquid line 10). Thus, you may provide between the absorption tower 3 and the regeneration heat exchanger 7 (1st rich liquid line 8). Even if it is such a structure, the same effect can be acquired.

  In the first embodiment, the gas-liquid separator 21 may not be provided, and the exhaust gas 2c that has passed through the heat exchanger 20 may be sent directly to the gas cooler 14.

  When the gas-liquid separator 21 has high gas-liquid separation performance, the gas-liquid separator 15 is not provided, the gas (carbon dioxide gas) 23 that has passed through the gas cooler 14 is discharged, and storage equipment (not shown) You may make it store it.

  (Second Embodiment) FIG. 3 shows a schematic configuration of a carbon dioxide recovery system according to a second embodiment of the present invention. In the present embodiment, the rich liquid 4 a is separated into a gas phase component (carbon dioxide) and a liquid phase component by the gas-liquid separator 201, the gas phase component is sent to the gas cooler 14, and the liquid phase component is regenerated by the pump 22. The other configuration is supplied to the tower 5 and is the same as that of the first embodiment shown in FIG. In FIG. 3, the same parts as those of the first embodiment shown in FIG.

  A part of the carbon dioxide contained in the rich liquid 4 a is released by the gas-liquid separator 201 and sent to the gas cooler 14. That is, the liquid phase component discharged from the lower part of the gas-liquid separator 201 is a part of carbon dioxide released from the rich liquid 4a.

  In the present embodiment, the amount of carbon dioxide in the rich liquid supplied to the regeneration tower 5 can be reduced as compared with the first embodiment. Therefore, in the regeneration tower 5, the amount of carbon dioxide released from the absorption liquid can be reduced. Therefore, the resorption of the carbon dioxide in the absorption liquid in the regeneration tower 5 can be reduced, so that the necessary thermal energy of the reboiler 6 is obtained. Can be further reduced.

  Thus, the rich liquid 4a is heated using the heat of the exhaust gas 2c from the regeneration tower 5, and a part of the carbon dioxide in the rich liquid 4a after heating is separated and released by the gas-liquid separator 201. Thus, it is possible to further reduce the thermal energy required in the absorption liquid regeneration process and further reduce the operating cost of the carbon dioxide recovery system.

  (Third Embodiment) FIG. 4 shows a schematic configuration of a carbon dioxide recovery system according to a third embodiment of the present invention. In this embodiment, the liquid (water) 24 in the gas-liquid separator 21 is sent to the reboiler 6 by the pump 22, and the other configuration is the same as that of the first embodiment shown in FIG. . In FIG. 4, the same parts as those of the first embodiment shown in FIG.

  The liquid 24 is supplied to the reboiler 6 and carbon dioxide dissolved in the liquid 24 is released. As a result, carbon dioxide released by heating in the regeneration tower 5 can be prevented from being reabsorbed by the liquid 24 supplied to the regeneration tower 5, and the required thermal energy of the reboiler 6 can be further reduced. it can.

  In the present embodiment, as in the first embodiment, the heat of the exhaust gas 2c from the regeneration tower 5 is used to heat the rich liquid 4a, so that the thermal energy required for the absorption liquid regeneration process is obtained. This can reduce the operating cost of the carbon dioxide recovery system.

  Further, it is possible to prevent the carbon dioxide from being reabsorbed into the liquid 24 supplied to the regeneration tower 5, further reduce the thermal energy required in the regeneration process of the absorbent, and further reduce the operating cost of the carbon dioxide recovery system.

  Further, in the present embodiment, when the gas-liquid separator 21 has high gas-liquid separation performance, the gas (carbon dioxide gas) 23 that has passed through the gas cooler 14 is discharged without providing the gas-liquid separator 15, You may make it store with a storage facility (not shown).

  (Fourth Embodiment) FIG. 5 shows a schematic configuration of a carbon dioxide recovery system according to a fourth embodiment of the present invention. In the present embodiment, the rich liquid 4 a is separated into a gas phase component (carbon dioxide) and a liquid phase component by the gas-liquid separator 401, the gas phase component is sent to the gas cooler 14, and the liquid phase component is regenerated by the pump 402. The other components are supplied to the tower 5 and are the same as those of the third embodiment shown in FIG. In FIG. 5, the same parts as those of the third embodiment shown in FIG.

  A part of the carbon dioxide contained in the rich liquid 4 a is released by the gas-liquid separator 401 and sent to the gas cooler 14. That is, the liquid phase component discharged from the lower part of the gas-liquid separator 401 is a part of carbon dioxide released from the rich liquid 4a.

  In the present embodiment, the amount of carbon dioxide in the rich liquid supplied to the regeneration tower 5 can be reduced as compared with the third embodiment. Therefore, in the regeneration tower 5, the amount of carbon dioxide released from the absorption liquid can be reduced. Therefore, the resorption of the carbon dioxide in the absorption liquid in the regeneration tower 5 can be reduced, so that the necessary thermal energy of the reboiler 6 is obtained. Can be further reduced.

  Thus, the rich liquid 4a is heated using the heat of the exhaust gas 2c from the regeneration tower 5, and a part of carbon dioxide in the rich liquid 4a after heating is separated and released by the gas-liquid separator 401, By supplying the liquid 24 in the gas-liquid separator 21 to the reboiler 6, it is possible to further reduce the thermal energy required in the regeneration process of the absorbing liquid and further reduce the operating cost of the carbon dioxide recovery system.

  (Fifth Embodiment) FIG. 6 shows a schematic configuration of a carbon dioxide recovery system according to a fifth embodiment of the present invention. In the present embodiment, the liquid 24 in the gas-liquid separator 21 is sent to the heat exchanger 501 provided in the first rich liquid line 8 by the pump 22, and the other configuration is the first embodiment shown in FIG. It has become the same. In FIG. 6, the same parts as those of the first embodiment shown in FIG.

  The liquid 24 in the gas-liquid separator 21 has a high temperature, and the rich liquid 4a is heated in the heat exchanger 501 using the liquid 24 as a heat source and utilizing sensible heat of water. The liquid 24 after heating the rich liquid 4a is supplied to the gas-liquid separator 15 and reused as a reflux liquid. With such a configuration, the heat of the exhaust gas 2c from the regeneration tower 5 can be recovered to the maximum, and the required thermal energy of the reboiler 6 can be further reduced.

  In the present embodiment, as in the first embodiment, the heat of the exhaust gas 2c from the regeneration tower 5 is used to heat the rich liquid 4a, so that the thermal energy required for the absorption liquid regeneration process is obtained. This can reduce the operating cost of the carbon dioxide recovery system.

  Furthermore, by further heating the rich liquid 4a using the sensible heat of the liquid 24 in the gas-liquid separator 21, the thermal energy required in the regeneration process of the absorbing liquid is reduced, and the operating cost of the carbon dioxide recovery system Can be reduced.

  (Sixth Embodiment) FIG. 7 shows a schematic configuration of a carbon dioxide recovery system according to a sixth embodiment of the present invention. In the present embodiment, the rich liquid 4 a is separated into a gas phase component (carbon dioxide) and a liquid phase component by the gas-liquid separator 601, the gas phase component is sent to the gas cooler 14, and the liquid phase component is regenerated by the pump 602. The other structure is supplied to the tower 5 and is the same as that of the fifth embodiment shown in FIG. In FIG. 7, the same parts as those of the fifth embodiment shown in FIG.

  A part of carbon dioxide contained in the rich liquid 4 a is released by the gas-liquid separator 601 and sent to the gas cooler 14. That is, the liquid phase component discharged from the lower part of the gas-liquid separator 601 is a part of carbon dioxide released from the rich liquid 4a.

  In the present embodiment, the amount of carbon dioxide in the rich liquid supplied to the regeneration tower 5 can be reduced as compared with the fifth embodiment. Therefore, in the regeneration tower 5, the amount of carbon dioxide released from the absorption liquid can be reduced. Therefore, the resorption of the carbon dioxide in the absorption liquid in the regeneration tower 5 can be reduced, so that the necessary thermal energy of the reboiler 6 is obtained. Can be further reduced.

  Thus, the rich liquid 4a is heated using the heat of the exhaust gas 2c from the regeneration tower 5, and a part of carbon dioxide in the rich liquid 4a after heating is separated and released by the gas-liquid separator 601. Heating the rich liquid 4a with the liquid 24 in the gas-liquid separator 21 can further reduce the thermal energy required in the regeneration process of the absorbent and further reduce the operating cost of the carbon dioxide recovery system.

  Note that the present invention is not limited to the above-described embodiment as it is, and can be embodied by modifying the constituent elements without departing from the scope of the invention in the implementation stage. In addition, various inventions can be formed by appropriately combining a plurality of components disclosed in the embodiment. For example, some components may be deleted from all the components shown in the embodiment. Furthermore, constituent elements over different embodiments may be appropriately combined.

DESCRIPTION OF SYMBOLS 1 Carbon dioxide recovery system 3 Absorption tower 5 Regeneration tower 6 Reboiler 7 Regenerative heat exchanger 13 Absorbent liquid cooler 14 Gas cooler 15, 21 Gas-liquid separator 20 Heat exchanger

Claims (7)

An absorption tower for absorbing carbon dioxide contained in the combustion exhaust gas into the absorption liquid;
An absorption liquid that absorbs carbon dioxide is supplied from the absorption tower, and carbon dioxide gas containing vapor is released from the absorption liquid and the absorption liquid is regenerated, and the discharged carbon dioxide gas and exhaust gas containing vapor are discharged. A regenerating tower,
The carbon dioxide supplied from the absorption tower to the regeneration tower is absorbed by the regenerated absorption liquid provided between the absorption tower and the regeneration tower and supplied from the regeneration tower to the absorption tower as a heat source. A regenerative heat exchanger for heating the absorption liquid;
Provided between the absorption tower and the regeneration heat exchanger, or between the regeneration heat exchanger and the regeneration tower, and using the exhaust gas discharged from the regeneration tower as a heat source, the regeneration from the absorption tower. A heat exchanger for heating the absorption liquid that has absorbed carbon dioxide supplied to the tower;
A carbon dioxide recovery system. A gas-liquid separator that separates the exhaust gas that has passed through the heat exchanger into a liquid phase component and a gas phase component;
A pump for supplying the liquid phase component to the regeneration tower;
The carbon dioxide recovery system according to claim 1, further comprising: A second gas-liquid separator that condenses the gas phase component and separates the generated condensate;
A third gas-liquid separator that separates an absorption liquid that has absorbed carbon dioxide supplied to the regeneration tower from the regeneration heat exchanger and the absorption tower that has passed through the heat exchanger into a liquid phase component and a gas phase component When,
Further comprising
The gas phase component separated by the third gas-liquid separator is supplied to the second gas-liquid separator, and the liquid phase component separated by the third gas-liquid separator is supplied to the regeneration tower by the pump. The carbon dioxide recovery system according to claim 2, wherein the carbon dioxide recovery system is supplied to. A reboiler for heating the absorbent in the regeneration tower;
A gas-liquid separator that separates the exhaust gas that has passed through the heat exchanger into a liquid phase component and a gas phase component;
A pump for supplying the liquid phase component to the reboiler;
The carbon dioxide recovery system according to claim 1, further comprising: A second gas-liquid separator that condenses the gas phase component and separates the generated condensate;
A third gas-liquid separator that separates an absorption liquid that has absorbed carbon dioxide supplied to the regeneration tower from the absorption tower that has passed through the regeneration heat exchanger and the heat exchanger into a liquid phase component and a gas phase component When,
A second pump for supplying the liquid phase component separated by the third gas-liquid separator to the regeneration tower;
Further comprising
The carbon dioxide recovery system according to claim 4, wherein the gas phase component separated by the third gas-liquid separator is supplied to the second gas-liquid separator. A first gas-liquid separator that separates the exhaust gas that has passed through the heat exchanger into a liquid phase component and a gas phase component;
A second gas-liquid separator that condenses the gas phase component and separates the generated condensate;
Provided between the absorption tower and the regeneration heat exchanger, or between the regeneration heat exchanger and the regeneration tower, and supplied from the absorption tower to the regeneration tower using the liquid phase component as a heat source. A second heat exchanger for heating the absorbing liquid that has absorbed carbon;
A pump for supplying the liquid phase component from the first gas-liquid separator to the second heat exchanger;
Further comprising
The carbon dioxide recovery system according to claim 1, wherein the liquid phase component that has passed through the second heat exchanger is supplied to the second gas-liquid separator. An absorption liquid that has absorbed carbon dioxide supplied to the regeneration tower from the absorption tower that has passed through the regeneration heat exchanger, the heat exchanger, and the second heat exchanger is converted into a liquid phase component and a gas phase component. A third gas-liquid separator to be separated;
A second pump for supplying the liquid phase component separated by the third gas-liquid separator to the regeneration tower;
Further comprising
The carbon dioxide recovery system according to claim 6, wherein the gas phase component separated by the third gas-liquid separator is supplied to the second gas-liquid separator.

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