CO2 recovery system

The present invention relates to a CO 2 recovery system that absorbs CO 2 from gas and reduces CO 2 compression power.

As one of the causes of global warming, the greenhouse effect by CO 2 has been identified, and a countermeasure thereof is urgently required internationally from the viewpoint of protecting the global environment. Sources of CO 2 emission spread over various fields of human activity where fossil fuel is burned, and demand on emission reduction of CO 2 tends to increase. As a result, for power generation facilities such as a thermal power plant where a large amount of fossil fuel is used, a CO 2 recovery method has been actively studied in which flue gas of a boiler is brought into contact with an amine-based absorption solution such as an aqueous amine compound solution so as to remove and recover CO 2 from the flue gas.

In the related art, PTL 1 discloses an amine recovery process in which an amine compound accompanying decarbonated flue gas, from which CO 2 has been absorbed and removed by gas-liquid contact with an absorption solution, is sequentially recovered in plural stages of water-washing sections that are provided for bringing the decarbonated flue gas into gas-liquid contact with a washing solution to recover the amine compound.

In addition, in the related art, PTL 2 discloses a configuration including: a cooling unit that cools decarbonated flue gas from which CO 2 has been absorbed and removed by gas-liquid contact with an absorption solution; and a contact unit that brings condensate, which has been condensed in the cooling unit, into counterflow contact with the decarbonated flue gas. Further, PTL 2 discloses a configuration including a water-washing section in which an amine compound accompanying decarbonated flue gas is recovered. In this configuration, condensate, which has been condensed in a cooling tower in which flue gas is cooled before CO 2 is recovered therefrom, is used as washing water.

Patent Literature

[PTL 1] Japanese Unexamined Patent Application Publication No. 2002-126439

[PTL 2] Japanese Unexamined Patent Application Publication No. 8-80421

Technical Problem

However, recently, from the viewpoint of protecting the environment, when a CO 2 recovery device is installed to process flue gas in, for example, a thermal power plant where the flow rate of gas to be processed is high, the amount of CO 2 to be removed is large. Therefore, for example, when the CO 2 recovery device is buried in the ground, it is desired to reduce power relating to CO 2 compression in a CO 2 recovery plant.

The present invention has been made in order to solve the above-described problems, and an object thereof is to provide a CO 2 recovery system that absorbs CO 2 from gas and reduces CO 2 compression power.

Solution to Problem

According to a first aspect of the present invention for solving the above-described problems, there is provided a CO 2 recovery system comprising: an absorption tower that brings gas containing CO 2 into contact with a CO 2 absorption solution to remove CO 2 from the CO 2 -containing gas; a regeneration tower that regenerates a CO 2 -absorbed rich solution; and a compression device that re-uses a lean solution, from which CO 2 has been removed in the regeneration tower, in the absorption tower and compresses CO 2 in gas emitted from the regeneration tower, wherein the rich solution has a high pressure, the high-pressure rich solution is subjected to gas-liquid separation by a flash drum, the rich solution as a liquid component separated in the flash drum is introduced into the regeneration tower, and high-pressure CO 2 gas as a gas component separated in the flash drum is introduced into a compression device having a predetermined compression pressure.

According to a second aspect of the present invention, in the CO 2 recovery system according to the first aspect, plural stages of flash drums may be provided, a pressure-reducing valve may be provided on an upstream side of a gas-liquid separator, and CO 2 gas as a gas component separated in each of the flash drums may be introduced into a compression device having a predetermined compression pressure corresponding to a pressure of the CO 2 gas as the gas component.

According to a third aspect of the present invention, in the CO 2 recovery system according to the second aspect, a heat exchanger which heats the rich solution is provided between the absorption tower and an initial gas-liquid separator.

According to a fourth aspect of the present invention, in the CO 2 recovery system according to the second aspect, an inert gas separator, which separates inert gas, and an inert gas introduction line, which introduces the separated inert gas into the absorption tower, may be provided between the absorption tower and an initial gas-liquid separator.

According to a fifth aspect of the present invention, in the CO 2 recovery system according to the first aspect, when the gas introduced into the absorption tower is normal-pressure gas, a normal-pressure absorption tower may be used, a booster pump that pressurizes the rich solution emitted from the normal-pressure absorption tower may be provided, and the pressurized rich solution may be subjected to gas-liquid separation by the gas-liquid separator.

According to a sixth aspect of the present invention, in the CO 2 recovery system according to the first aspect, when the gas introduced into the absorption tower is high-pressure gas, a pressurization absorption tower may be used, and the pressurized rich solution emitted from the pressurization absorption tower may be subjected to gas-liquid separation by the gas-liquid separator.

Advantageous Effects of Invention

According to the present invention, the flash drum is provided. Therefore, by the pressure being released by the flash operation of the flash drum, a portion of CO 2 absorbed in the pressurized rich solution is released and emitted as high-pressure CO 2 gas. This emitted high-pressure CO 2 gas is introduced into the compressor of the CO 2 compression device that is provided on a gas flow downstream side of the regeneration tower to compress CO 2 . As a result, compression power for compressing CO 2 gas, which is emitted from the regeneration tower, can be significantly saved unlike the related art, and the size of compression facilities can be reduced.

FIG. 1 is a schematic diagram illustrating a CO 2 recovery system according to Embodiment 1.

FIG. 2 is a schematic diagram illustrating the CO 2 recovery system according to Embodiment 1.

FIG. 3 is a schematic diagram illustrating another CO 2 recovery system according to Embodiment 1.

FIG. 4 is a schematic diagram illustrating a CO 2 recovery system according to Embodiment 2.

FIG. 5 is a schematic diagram illustrating the CO 2 recovery system according to Embodiment 2.

FIG. 6 is a schematic diagram illustrating a CO 2 recovery system according to Embodiment 3.

FIG. 7 is a schematic diagram illustrating a CO 2 recovery system according to Embodiment 3.

FIG. 8 is a schematic diagram illustrating a CO 2 recovery system according to Embodiment 4.

FIG. 9 is a schematic diagram illustrating a CO 2 recovery system according to Embodiment 5.

Hereinafter, the present invention will be described with reference to the drawings. The present invention is not limited to the embodiment. In addition, in the case of plural embodiments, combinations of the respective embodiments are included in the present invention. In addition, components in the following embodiment include components which can be easily conceived by those skilled in the art, and substantially identical ones thereto.

A CO 2 recovery system according to Embodiment 1 of the present invention will be described with reference to the drawings.

FIGS. 1 and 2 are schematic diagrams illustrating the CO 2 recovery system according to Embodiment 1. As illustrated in FIG. 1 , a CO 2 recovery system 10 A according to the embodiment includes: a normal-pressure absorption tower 13 that brings normal-pressure flue gas (referred to as “gas (normal-pressure)”) 11 containing CO 2 into contact with a CO 2 absorption solution 12 to remove CO 2 from the normal-pressure flue gas; a normal-pressure regeneration tower 15 that regenerates a CO 2 -absorbed rich solution 14 ; and a CO 2 compression device 16 including a high-pressure compressor 16 H and a low-pressure compressor 16 L that re-uses a lean solution 17 , from which CO 2 has been removed in the normal-pressure regeneration tower 15 , in the absorption tower 13 and gradually compresses CO 2 in gas, which has been emitted from the normal-pressure regeneration tower 15 , at a plurality of predetermined pressures. In the CO 2 recovery system 10 A, the rich solution 14 is pressurized by a booster pump 32 to obtain a pressurized rich solution 14 A, a first flash drum 21 A that separates carbon dioxide gas (CO 2 ) from the pressurized rich solution 14 A through a flash operation is provided, the rich solution 14 B which has been partially regenerated as a liquid component separated in the first flash drum 21 A is introduced into the regeneration tower 15 , and a high-pressure CO 2 gas 22 H as a gas component separated in the first flash drum 21 A is introduced into a high-pressure compressor 16 H having a predetermined pressure.

In the absorption tower 13 , the gas (normal-pressure) 11 containing carbon dioxide (CO 2 ) emitted from, for example, a boiler is brought into counterflow contact with the CO 2 absorption solution (amine solution) 12 containing, for example, alkanolamine as a base such that the CO 2 absorption solution 12 absorbs CO 2 from the gas 11 and removes CO 2 from the gas 11 . The rich solution 14 which is the CO 2 -absorbed CO 2 absorption solution emits CO 2 in the regeneration tower 15 . When CO 2 reaches the bottom of the regeneration tower 15 , most of the CO 2 is removed, and the absorption solution is regenerated as the lean solution 17 . This regenerated lean solution 17 is supplied again to the absorption tower 13 to be used as the CO 2 absorption solution 12 .

Here, in FIG. 1 , reference numeral L 1 represents a first liquid feed line that feeds the rich solution from the absorption tower 13 to the regeneration tower 15 , reference numeral L 2 represents a second liquid feed line that feeds the lean solution 17 from the regeneration tower 15 to the absorption tower 13 , reference numeral L 3 represents a gas feed line that feeds the high-pressure CO 2 gas 22 H from the first flash drum 21 A to a first gas-liquid separator 23 A, reference numeral L 4 represents a liquid return line that returns an absorption solution 14 a recovered from the first gas-liquid separator 23 A to the first flash drum 21 A, reference numeral L 5 represents a gas feed line that feeds the high-pressure CO 2 gas 22 H from the first gas-liquid separator 23 A to the high-pressure compressor 16 H, reference numeral L 6 represents a gas feed line that feeds the low-pressure CO 2 gas 22 L from the top portion of the regeneration tower 15 to the low-pressure compressor 16 L, reference numeral 31 represents purified gas from which CO 2 has been removed, reference numeral 32 represents the booster pump for the rich solution 14 that is provided in the first liquid feed line L 1 , reference numeral 33 represents a heat exchanger that exchanges heat between the pressurized rich solution 14 A and the lean solution 17 , reference numeral 36 represents a cooling condenser that cools steam condensate 34 on the top portion of the regeneration tower with cooling water 35 , reference numeral 37 represents a reboiler that reheats a portion 16 a of the lean solution 17 , reference numeral 38 represents saturated steam that is supplied to the reboiler 37 , reference numeral 39 represents the steam condensate, reference numerals 41 A and 41 B represent a pressure-reducing valves that are provided in the first liquid feed line L 1 , reference numeral 42 represents a liquid feed pump that feeds the lean solution 17 from the regeneration tower 15 to the absorption tower 13 , and reference numeral 43 represents cooling means for cooling the lean solution 17 .

The normal-pressure gas 11 is introduced into the absorption tower 13 , the CO 2 absorption solution 12 absorbs CO 2 contained in the gas to obtain the rich solution 14 , and the rich solution 14 is emitted from the bottom portion of the absorption tower. Next, the pressurized rich solution 14 A that is pressurized by the booster pump 32 is controlled to a predetermined pressure by the pressure-reducing valve 41 A and is introduced into the first flash drum 21 A.

Here, it is necessary that the pressure of the pressurized rich solution 14 A pressurized in the booster pump 32 be higher than a compression pressure of the high-pressure compressor 16 H of the CO 2 compression device 16 . For example, when the compression pressure of the high-pressure compressor 16 H is 630 kPaG, the pressure of the pressurized rich solution 14 A is about 800 kPaG (a pressure higher than a predetermined pressure of the compressor by about 50 kPaG to 200 kPaG).

The pressure-reducing valve 41 A that is provided on an upstream side of the first flash drum 21 A is controlled such that the partially regenerated rich solution 14 B has a temperature of about 102° C. and a pressure of about 655 kPaG.

In the first flash drum 21 A, the pressurized rich solution 14 A is flashed at a predetermined pressure, a portion of carbon dioxide (CO 2 ) in the pressurized rich solution 14 A is released, and the pressurized rich solution 14 A is partially regenerated.

In the first flash drum 21 A, the pressurized rich solution 14 A is separated into the high-pressure CO 2 gas 22 H and the partially generated rich absorption solution 14 B.

The separated high-pressure CO 2 gas 22 H having a desired pressure (for example, 630 kPaG) is fed to the first gas-liquid separator 23 A through the gas feed line L 3 . In this gas-liquid separator 23 A, the absorption solution 14 a accompanying the gas during flashing is separated and is fed to the high-pressure compressor 16 H through the gas feed line L 5 . The separated absorption solution 14 a is returned to the first flash drum 21 A.

The pressure-reducing valves 41 A and 41 B decrease a pressure to predetermined pressures, respectively, are provided in the first liquid feed line L 1 , and are provided on an upstream side of the first flash drum 21 A and the regeneration tower 15 to control the pressures of the rich solutions 14 A and 14 B to predetermined pressures.

FIG. 2 is a schematic diagram illustrating the CO 2 recovery system to describe a temperature and a pressure of flashed gas according to an example of the embodiment.

The pressurized rich solution 14 A is controlled to have a predetermined pressure (655 kPaG, 102° C.) by the pressure-reducing valve 41 A, is introduced into the first flash drum 21 A, and is partially regenerated to obtain the partially regenerated rich solution 14 B by a portion of CO 2 being released. This partially regenerated rich solution 14 B is fed to the regeneration tower 15 .

The high-pressure CO 2 gas 22 H containing 17% of the total amount of CO 2 which has been released in the first flash drum 21 A is fed to the high-pressure compressor 16 H at a gas pressure of 630 kPaG and 40° C. through the gas feed line L 5 .

In addition, the low-pressure CO 2 gas 22 L containing the rest of the 83% of the total amount of CO 2 which has been emitted from the tower top portion of the regeneration tower 15 is fed to the low-pressure compressor 16 L at a gas pressure of 50 kPaG and 40° C. through the gas feed line L 6 .

The lean solution 17 emitted from the bottom portion of the regeneration tower 15 has a temperature of about 120° C. and a pressure of 80 kPaG. Since this temperature is lower than or equal to a deterioration temperature of the amine solution constituting the absorption solution, the absorption solution does not deteriorate.

On the other hand, as in the case of the related art, when the high-pressure rich solution is directly introduced into the high-pressure regeneration tower, the lean solution which has been regenerated by emitting CO 2 in the high-pressure regeneration tower is emitted from the bottom portion at about 150° C. or higher and a pressure of 380 kPaG. Therefore, the lean solution 17 is in the high-temperature state, and the amine solution which is the composition of the absorption solution deteriorates.

In this way, according to the embodiment, the first flash drum 21 A is provided in the first liquid feed line L 1 . Therefore, by the pressure being released by the flash operation of the first flash drum, a portion of CO 2 absorbed in the pressurized rich solution 14 A is released and emitted as the high-pressure CO 2 gas 22 H. This emitted high-pressure CO 2 gas 22 H is introduced into the high-pressure compressor 16 H of the CO 2 compression device 16 that is provided on a gas flow downstream side of the regeneration tower 15 to compress CO 2 .

As a result, compression power for compressing CO 2 gas, which is emitted from the regeneration tower 15 , can be significantly saved unlike the related art, and the size of compression facilities can be reduced.

FIG. 3 is a schematic diagram illustrating another CO 2 recovery system according to the embodiment.

As illustrated in FIG. 3 , a CO 2 recovery system 10 B according to the embodiment is the same as the CO 2 recovery system 10 A according to Embodiment 1 illustrated in FIG. 1 , except that an inert gas separator 50 is further provided between the booster pump 32 and the heat exchanger 33 .

When inert gas is present, the compression purity of CO 2 gas cannot be improved because inert gas is non-condensable gas. Accordingly, in the embodiment, inert gas (for example, N 2 or H 2 ) 51 present (0.1 wt % or less) in the pressurized rich solution 14 A is removed on an upstream side of the first flash drum 21 A. The removed inert gas 51 is circulated again to the absorption tower 13 through an inert gas circulating line L 20 . In the inert gas circulating line L 20 , a cooler 52 and a gas-liquid separator 53 are provided.

By providing the inert gas separator 50 to remove the inert gas 51 , the purity of compressed and recovered CO 2 gas is improved.

In the embodiment, gas-liquid separation is performed using the flash drum, but the invention is not limited thereto. For example, a distillation tower or a separation column may be used for gas-liquid separation.

A CO 2 recovery system according to Embodiment 2 of the present invention will be described with reference to the drawings.

FIGS. 4 and 5 are schematic diagrams illustrating the CO 2 recovery system according to Embodiment 2. As illustrated in FIG. 4 , a CO 2 recovery system 10 C according to the embodiment is the same as the CO 2 recovery system 10 B illustrated in FIG. 3 , except that a first flash drum 21 A and a second flash drum 21 B are provided in the first liquid feed line L 1 .

In the first flash drum 21 A, by the pressure being released by the flash operation, a portion of CO 2 absorbed in the pressurized rich solution 14 A is released and emitted as the high-pressure CO 2 gas 22 H. This emitted high-pressure CO 2 gas 22 H is introduced into the high-pressure compressor 16 H of the CO 2 compression device 16 that is provided on a gas flow downstream side of the regeneration tower 15 to compress CO 2 .

In the second flash drum 21 B, by the pressure being released by the flash operation, a portion of CO 2 absorbed in the partially regenerated rich solution 14 B is released and emitted as medium-pressure CO 2 gas 22 M. This emitted medium-pressure CO 2 gas 22 M is introduced into a medium-pressure compressor 16 M of the CO 2 compression device 16 that is provided on a gas flow downstream side of the regeneration tower 15 to compress CO 2 .

FIG. 5 is a schematic diagram illustrating the CO 2 recovery system to describe a temperature and a pressure of gas according to an example of the embodiment.

The pressurized rich solution 14 A is controlled to have a predetermined pressure (655 kPaG, 102° C.) by the pressure-reducing valve 41 A, is introduced into the first flash drum 21 A, and is partially regenerated to obtain the partially regenerated rich solution 14 B by a portion of CO 2 being released. This partially regenerated rich solution 14 B is fed to the regeneration tower 15 .

The pressure-reducing valve 41 A that is provided on an upstream side of the first flash drum 21 A is controlled such that the partially regenerated rich solution 14 B has a temperature of about 102° C. and a pressure of about 655 kPaG. The high-pressure CO 2 gas 22 H containing 17% of the total amount of CO 2 which has been released in the first flash drum 21 A is fed to the high-pressure compressor 16 H at a gas pressure of 630 kPaG and 40° C. through the gas feed line L 5 .

The pressure-reducing valve 41 C that is provided on an upstream side of the second flash drum 21 B is controlled such that the partially regenerated rich solution 14 C has a temperature of about 95° C. and a pressure of about 255 kPaG.

The medium-pressure CO 2 gas 22 M containing 19% of the total amount of CO 2 which has been released in the second flash drum 21 B is fed to the medium-pressure compressor 16 M at a gas pressure of 230 kPaG and 40° C. through the gas feed line L 9 .

In addition, the low-pressure CO 2 gas 22 L containing the rest of the 64% of the total amount of CO 2 which have been emitted from the tower top portion of the regeneration tower 15 is fed to the low-pressure compressor 16 L at a gas pressure of 50 kPaG and 40° C. through the gas feed line L 6 .

The lean solution 17 emitted from the bottom portion of the regeneration tower 15 has a temperature of about 120° C. and a pressure of 80 kPaG. Since this temperature is lower than or equal to a deterioration temperature of the amine solution constituting the absorption solution, the absorption solution does not deteriorate.

In this way, in the embodiment, since the first flash drum 21 A and the second flash drum 21 B are provided, the high-pressure CO 2 gas 22 H and the medium-pressure CO 2 gas 22 M can be extracted. As compared to Embodiment 1, compression power for compressing CO 2 gas, which is emitted from the regeneration tower 15 , can be significantly saved, and the size of compression facilities can be reduced.

A CO 2 recovery system according to Embodiment 3 of the present invention will be described with reference to the drawings.

FIGS. 6 and 7 are schematic diagrams illustrating the CO 2 recovery system according to Embodiment 3. As illustrated in FIG. 6 , a CO 2 recovery system 10 D according to the embodiment is the same as the CO 2 recovery system 10 C illustrated in FIG. 4 , except that a heat exchanger 61 that heats the pressurized rich solution 14 A is provided between the heat exchanger 33 and the pressure-reducing valve 41 A which are provided in the first liquid feed line L 1 .

Due to the provided heat exchanger 61 , the pressurized rich solution 14 A is heated to around 120° C. which is a heat resistance temperature thereof.

By the heat exchanger 61 heating the pressurized rich solution 14 A, the temperature of the pressurized rich solution 14 A introduced into the first flash drum 21 A increases, and the amount of CO 2 gas released in the first flash drum 21 A increases.

FIG. 7 is a schematic diagram illustrating the CO 2 recovery system to describe a temperature and a pressure of gas according to an example of the embodiment.

Since being heated by the heat exchanger 61 , the pressurized rich solution 14 A is controlled to have a predetermined pressure (655 kPaG, 120° C.) by the pressure-reducing valve 41 A, is introduced into the first flash drum 21 A, and is partially regenerated to obtain the partially regenerated rich solution 14 B by a portion of CO 2 being released. This partially regenerated rich solution 14 B is fed to the regeneration tower 15 .

The high-pressure CO 2 gas 22 H containing 37% of the total amount of CO 2 which has been released in the first flash drum 21 A is fed to the high-pressure compressor 16 H at a gas pressure of 630 kPaG and 40° C. through the gas feed line L 5 .

The medium-pressure CO 2 gas 22 M containing 28% of the total amount of CO 2 which has been released in the second flash drum 21 B is fed to the medium-pressure compressor 16 M at a gas pressure of 230 kPaG and 40° C. through the gas feed line L 9 .

In addition, the low-pressure CO 2 gas 22 L containing the rest of the 35% of the total amount of CO 2 which has been emitted from the tower top portion of the regeneration tower 15 is fed to the low-pressure compressor 16 L at a gas pressure of 50 kPaG and 40° C. through the gas feed line L 6 .

The lean solution 17 emitted from the bottom portion of the regeneration tower 15 has a temperature of about 120° C. and a pressure of 80 kPaG. Since this temperature is lower than or equal to a deterioration temperature of the amine solution constituting the absorption solution, the absorption solution does not deteriorate.

In this way, in the embodiment, two stages including the first flash drum 21 A and the second flash drum 21 B are continuously provided, and the pressurized rich solution 14 A is heated by the heat exchanger 61 on an upstream side of the first flash drum 21 A. Therefore, the high-pressure CO 2 gas 22 H and the medium-pressure CO 2 gas 22 M can be extracted, and the amount of the CO 2 gas released from the high-pressure gas increases. As compared to Embodiment 2, compression power for compressing CO 2 gas, which is emitted from the regeneration tower 15 , can be significantly saved, and the size of compression facilities can be reduced.

A CO 2 recovery system according to an embodiment of the present invention will be described with reference to the drawings.

FIG. 8 is a schematic diagram illustrating a CO 2 recovery system according to Embodiment 4. As illustrated in FIG. 8 , a CO 2 recovery system 10 E according to the embodiment is the same as the CO 2 recovery system 10 B illustrated in FIG. 3 , except that a pressure-reducing valve 41 D is provided in the gas feed line L 6 extended from the regeneration tower 15 to feed gas, emitted from the tower top portion of the regeneration tower 15 , as the low-pressure CO 2 gas 22 L.

With such a configuration, since the pressurized rich solution is introduced into the regeneration tower, the lean solution 17 emitted from the bottom portion of the regeneration tower 15 has a temperature of about 140° C. and a pressure of about 250 kPaG. However, the absorption solution may be used in this high temperature (140° C.) depending on the type thereof. Therefore, when an absorption solution having such high-temperature resistance is used, the configuration of the embodiment can be applied thereto.

The pressurized rich solution 14 A is controlled to have a predetermined pressure (655 kPaG, 102° C.) by the pressure-reducing valve 41 A, is introduced into the first flash drum 21 A, and is partially regenerated to obtain the partially regenerated rich solution 14 B by a portion of CO 2 being released. This partially regenerated rich solution 14 B is fed to the regeneration tower 15 .

The high-pressure CO 2 gas 22 H containing 36% of the total amount of CO 2 which has been released in the first flash drum 21 A is fed to the high-pressure compressor 16 H at a gas pressure of 630 kPaG and 40° C. through the gas feed line L 5 .

In addition, the low-pressure CO 2 gas 22 L containing the rest of the 64% of the total amount of CO 2 which has been emitted from the tower top portion of the regeneration tower 15 is fed to the low-pressure compressor 16 L at a gas pressure of 50 kPaG and 40° C. through the gas feed line L 6 .

The lean solution 17 emitted from the bottom portion of the regeneration tower 15 has a temperature of about 140° C. and a pressure of 250 kPaG. Since a deterioration temperature of the amine solution constituting the absorption solution is around 150° C., deterioration in the absorption solution is small.

In the embodiment, the lean solution 17 emitted from the bottom portion of the regeneration tower 15 has a temperature of about 140° C. and a pressure of 250 kPaG and thus can be used when the absorption solution has high-temperature resistance.

A CO 2 recovery system according to Embodiment 5 of the present invention will be described with reference to the drawings.

FIG. 9 is a schematic diagram illustrating a CO 2 recovery system according to Embodiment 5. As illustrated in FIG. 9 , in a CO 2 recovery system 10 F according to the embodiment, a pressurization type absorption tower 13 is provided, and pressurized gas is used as the gas to be introduced.

As the pressurized gas containing CO 2 , for example, pressurized gas for fertilizer synthesis or high-pressure natural gas (gas pressure: for example, 3,000 kPaG) may be used.

Since the rich solution 14 emitted from the absorption tower 13 is in the pressurized state, the booster pump is unnecessary unlike Embodiment 1, and a liquid feed pump 32 A is provided for feeding liquid.

In addition, it is necessary that the lean solution 17 regenerated in the regeneration tower 15 be pressurized when being fed to the absorption tower 13 . Therefore, the lean solution 17 is pressurized by a booster pump 42 A provided in a second liquid feed line L 2 .

In the CO 2 recovery system 10 F illustrated in FIG. 9 , by the first flash drum 21 A releasing the pressure through the flash operation, a portion of CO 2 absorbed in the pressurized rich solution 14 A is released and emitted as the high-pressure CO 2 gas 22 H. This emitted high-pressure CO 2 gas 22 H is introduced into the high-pressure compressor 16 H of the CO 2 compression device 16 that is provided on a gas flow downstream side of the regeneration tower 15 to compress CO 2 .

In addition, the low-pressure CO 2 gas 22 L containing the rest of CO 2 which has been emitted from the tower top portion of the regeneration tower 15 is fed to the low-pressure compressor 16 L at a gas pressure of 50 kPaG and 40° C. through the gas feed line L 6 .

The lean solution 17 emitted from the bottom portion of the regeneration tower 15 has a temperature of 120° C. Since this temperature is lower than or equal to a deterioration temperature of the amine solution constituting the absorption solution, the absorption solution does not deteriorate.

In this way, in the embodiment, when pressurized gas is used, since the first flash drum 21 A is provided, the high-pressure CO 2 gas 22 H can be extracted. Compression power for compressing CO 2 gas, which is emitted from the high-pressure regeneration tower 15 , can be significantly saved, and the size of compression facilities can be reduced.

In addition, in the inert gas circulating line L 20 that circulates the inert gas 51 , a compressor 54 is provided on a downstream side of the gas-liquid separator 53 so as to meet the high-pressure gas 11 .

10 A and 10 F: CO 2 RECOVERY SYSTEM

11 : GAS

12 : CO 2 ABSORPTION SOLUTION

13 : ABSORPTION TOWER

14 : RICH SOLUTION

15 : REGENERATION TOWER

16 : CO 2 COMPRESSION DEVICE

16 H: HIGH-PRESSURE COMPRESSOR

16 L: LOW-PRESSURE COMPRESSOR

16 M: MEDIUM-PRESSURE COMPRESSOR

17 : LEAN SOLUTION

21 A: FIRST FLASH DRUM

21 B: SECOND FLASH DRUM

22 H: HIGH-PRESSURE CO 2 GAS

22 L: LOW-PRESSURE CO 2 GAS

22 M: MEDIUM-PRESSURE CO 2 GAS