Carbon dioxide capture system and a method of operating a carbon dioxide capture system

This application is based upon and claims the benefit of priority from Japanese Patent Application No. 2015-243406, filed on Dec. 14, 2015, the entire content of which is incorporated herein by reference.

The present invention disclosures are directed to a carbon dioxide capture system that captures carbon dioxide from combustion exhaust gas.

In recent years, the greenhouse effect of carbon dioxide in combustion exhaust gas generated upon combustion of fossil fuels has been one of the major causes of global warming. Countries may address reductions of greenhouse gas emissions based on the Kyoto Protocol to the United Nations Frameworks Convention on Climate Change to solve the problem.

Under such a circumstance, the study has been in progress on a carbon dioxide capture system that prevents the release into the air of carbon dioxide contained in combustion exhaust gas generated upon the combustion of a fossil fuel at thermal plants or other facilities where a large amount of the fossil fuel is consumed. Such a carbon dioxide capture system, after bringing the combustion exhaust gas into contact with an amine absorbing liquid, separates the carbon dioxide from the combustion exhaust gas and captures the separated carbon dioxide.

Specifically, the carbon dioxide capture system includes an absorber and a stripper. The absorber causes the carbon dioxide contained in the combustion exhaust gas to be absorbed in the amine absorbing liquid as Japanese Patent Laid-open Publication No. 2004-323339 discloses. The stripper heats the absorbing liquid (rich liquid) containing the absorbed carbon dioxide and supplied from the absorber, causes the carbon dioxide to be released from the rich liquid, and regenerates the absorbing liquid. The stripper is coupled to a reboiler configured to supply a heating source, and the rich liquid is heated within the stripper. The absorbing liquid (lean liquid) regenerated in the stripper is supplied to the absorber. The absorbing liquid circulates within the system.

As explained above, the stripper heats the absorbing liquid (rich liquid) to release the carbon dioxide. Generally, the higher the temperature that the stripper heats the rich liquid, the more carbon dioxide is released. However, raising the temperature of the rich liquid may need much more heat at the reboiler, which results in an increase in the total recovery energy required to regenerate the rich liquid. Especially, in a larger type of carbon dioxide capture system, an increase in required recovery energy may be increased.

Accordingly, present embodiments provide a carbon dioxide capture system and a method of operating a carbon dioxide capture system that captures carbon dioxide from combustion exhaust gas efficiently.

In accordance with a presently disclosed aspect, a carbon dioxide capture system includes a first capture system and a second capture system. The first capture system causes carbon dioxide contained in a combustion exhaust gas to be absorbed in a first absorbing liquid. The second capture system causes carbon dioxide contained in a combustion exhaust gas to be absorbed in a second absorbing liquid. The second rich liquid releases carbon dioxide at a lower temperature than the first rich liquid.

It is to be understood that both the foregoing general description and the following detailed description are exemplary and explanatory only and are not restrictive of the embodiments, as claimed.

The accompanying drawings, which are incorporated in and constitute a part of the specification, illustrate an embodiment of the embodiments and together with the description, serve to explain the principles of the embodiments.

FIG. 1 is a schematic drawing of a first embodiment of a carbon dioxide capture system.

FIG. 2 is a schematic drawing of an alternative implementation of the first embodiment of a carbon dioxide capture system.

FIG. 3 is a schematic drawing of a second embodiment of a carbon dioxide capture system.

FIG. 4 is a schematic drawing of a third embodiment of a carbon dioxide capture system.

FIG. 5 is a schematic drawing of a fourth embodiment of a carbon dioxide capture system.

FIG. 6 is a schematic drawing of a fifth embodiment of a carbon dioxide capture system.

FIG. 7 is a schematic drawing of a sixth embodiment of a carbon dioxide capture system.

Reference will now be made in detail to the present embodiment, an example of which is illustrated in the accompanying drawing. Wherever possible, the same reference numbers will be used throughout the drawing to refer to the same or like parts.

First Embodiment

FIG. 1 shows a schematic diagram of a carbon dioxide capture system 1 that includes a first capture system 1 a and a second capture system 1 b.

The first capture system 1 a separates the carbon dioxide from the combustion exhaust gas 2 (process gas) and captures the separated carbon dioxide by using a first absorbing liquid explained below. The second capture system 1 b separates the carbon dioxide from the combustion exhaust gas 2 and captures the separated carbon dioxide by using a second absorbing liquid explained below. At first, the first capture system 1 a is explained.

As illustrated in FIG. 1 , the first capture system 1 includes a first absorber 20 a and a first stripper 30 a . The first absorber 20 a causes carbon dioxide contained in combustion exhaust gas 2 to be absorbed in the first absorbing liquid. The first absorbing liquid containing the absorbed carbon dioxide (a first rich liquid 4 a ) is supplied to the first stripper 30 a . The first stripper 30 a causes the carbon dioxide to be released from the first rich liquid and regenerates the first absorbing liquid. The combustion exhaust gas 2 from which the carbon dioxide is absorbed in the absorbing liquid in the first absorber 20 a is discharged as decarbonated combustion exhaust gas 3 from the absorber 20 a via a chimney 42 as shown in FIG. 2 . In addition, the carbon dioxide is discharged as carbon dioxide-containing gas 8 (carbon dioxide-containing steam or superheated steam) together with steam from the first stripper 30 a . For the purposes of this disclosure, the term steam is used to mean one or more of steam and superheated steam. The combustion exhaust gas 2 supplied to the first absorber 20 a is not limited to but may be combustion exhaust gas discharged from a boiler (not illustrated) of a thermal plant or process exhaust gas. It may be supplied to the first absorber 20 a after being subjected to a cooling process as appropriate.

The first absorber 20 a includes a carbon dioxide capturer 21 a (packed bed). The carbon dioxide capturer 21 a causes carbon dioxide contained in the combustion exhaust gas 2 to be absorbed in the first absorbing liquid to produce the first rich liquid 4 a . The carbon dioxide capturer 20 a is configured as a countercurrent gas-liquid contact device, made using trays or a packed bed in which gas and liquid contact each other, causing the liquid to flow down and the gas to flow up.

The combustion exhaust gas 2 that contains the carbon dioxide discharged from an external source (such as the aforementioned boiler of a thermal plant) is supplied by a blower (not illustrated) to a lower portion of the first absorber 20 a and ascends toward the carbon dioxide capturer 21 a within the first absorber 20 a . The first lean liquid 5 a is supplied from the stripper 30 to the carbon dioxide capturer 21 a and dropped in the carbon dioxide capturer 21 a . In the carbon dioxide capturer 21 a , the first lean liquid 5 a comes into contact with the combustion exhaust gas 2 and then absorbs the carbon dioxide contained in the combustion exhaust gas 2 , generating the first rich liquid 4 a.

The generated first rich liquid 4 a is temporarily stored in the lower portion of the first absorber 20 a and discharged from the lower portion. The combustion exhaust gas 2 further ascends as the decarbonated combustion exhaust gas 3 from the carbon dioxide capturer 21 a within the first absorber 20 a.

An amine recovery device (not shown) could be provided. The amine recovery device washes the decarbonated combustion exhaust gas 3 by water and recovers the amine in the decarbonated combustion exhaust gas 3 . The amine recovery device could be provided inside or outside of the first absorber 30 a . In the case that the amine recovery device is provided inside of the first absorber 30 a , the amine recovery device provided is provided at upper portion of the carbon dioxide capturer 21 a.

A heat exchanger 32 a is provided between the first absorber 20 a and the first stripper 30 a . A first rich liquid pump 33 a is arranged between the first absorber 20 a and the first heat exchanger 32 a . The first rich liquid 4 a discharged from the first absorber 20 a is supplied by the first rich liquid pump 33 a through the first heat exchanger 31 to the first stripper 30 . The first heat exchanger 31 causes heat transfer between the first rich liquid 4 a supplied to the first stripper 30 a and the first lean liquid 5 a supplied to the first absorber 20 a . The first lean liquid 5 a serves as a heating source to heat the first rich liquid 4 a to a desired temperature. In other words, the first rich liquid 4 a serves as a cooling source to cool the first lean liquid 5 a to a desired temperature.

The first stripper 30 a includes an amine regenerator 31 a (packed bed). The amine regenerator 31 a is configured to cause the carbon dioxide to be released from the first rich liquid 4 a that has been cooled by the first heat exchanger 32 a . The amine regenerator 31 a is configured as a countercurrent gas-liquid contact device.

The first stripper 30 a is coupled to a first reboiler 34 a . The first reboiler 34 a uses a first heating medium 6 a to heat the first lean liquid 5 a supplied from the first stripper 30 a to generate steam 7 . The reboiler 34 a supplies the generated steam 7 to the first stripper 30 a . Specifically, a part of the first lean liquid 5 a discharged from a lower portion of the first stripper 30 a is supplied to the reboiler 34 a , while at the same time high-temperature steam is supplied as the heating medium 6 a from an external source, such as a turbine (not illustrated), to the first reboiler 34 a . The first lean liquid 5 a supplied to the reboiler 34 a exchanges heat with the heating medium 6 a so as to be heated and thus generates the steam 7 from the first lean liquid 5 a . The generated steam 7 is supplied to the lower portion of the first stripper 30 a and heats the first lean liquid 5 a within the first stripper 30 a . The heating medium 6 a is not limited to the high-temperature steam supplied from the turbine but may also use high-temperature steam supplied from other known steam sources. After the first heating medium 6 a passes through the reboiler 34 a it is discharged from the reboiler 34 a as first discharged heating medium 6 b.

The steam 7 is supplied from the first reboiler 34 a to the lower portion of the first stripper 30 a and ascends toward the amine regenerator 31 a within the first stripper 30 a . The first rich liquid 4 a is dropped into the first stripper 30 a at the amine regenerator 31 a . In the amine regenerator 31 a , the rich liquid 4 a comes into contact with the steam 7 to cause the carbon dioxide to be released from the first rich liquid 4 a , and thus generate the first lean liquid 5 a . The first absorbing liquid is regenerated in the first stripper 30 a in this manner.

The generated first lean liquid 5 a is discharged from the lower portion of the first stripper 30 a . The steam 7 that has come into contact with the rich liquid 4 a and contains carbon dioxide is discharged as carbon dioxide-containing gas 8 from an upper portion of the first stripper 30 a . The discharged carbon dioxide-containing gas 8 contains steam.

A first lean liquid pump (not illustrated) is provided between the stripper 30 a and the heat exchanger 32 a . The first lean liquid 5 a discharged from the first stripper 30 a is supplied by the lean liquid pump through the aforementioned heat exchanger 32 a to the first absorber 20 a . The first heat exchanger 32 a causes the heat transfer between the first lean liquid 5 a supplied to the first absorber 20 a and the first rich liquid 4 a supplied to the first stripper 30 a to cool the first lean liquid 5 a , as described above. A first lean liquid cooler 35 a is provided between the heat exchanger 32 a and the first absorber 20 a . A cooling medium such as cooling water is supplied from an external component to the first lean liquid cooler 35 a . The first lean liquid cooler 35 a uses the cooling medium to further cool the first lean liquid 5 a cooled by the first heat exchanger 32 a to a desired temperature.

The first lean liquid 5 a cooled by the first lean liquid cooler 35 a is dropped in the first absorber 20 a , and is supplied to the carbon dioxide capturer 21 a . In the carbon dioxide capturer 21 a , the first lean liquid 5 a comes into contact with the combustion exhaust gas 2 , absorbs the carbon dioxide contained in the combustion exhaust gas 2 , and turns into the first rich liquid 4 a . In this manner, in the first capture system 1 a , the absorbing liquid circulates while repeatedly switching being the first lean liquid 5 a and being the first rich liquid 4 a.

The first capture system 1 a illustrated in FIG. 1 further includes a gas cooler 37 a . The gas cooler 37 a is configured to cool the carbon dioxide-containing gas 8 discharged from the upper portion of the first stripper 30 a by using an externally supplied cooling medium. The cooled carbon dioxide-containing gas 8 is supplied to a compressor 40 explained below.

Next, the second capture system 1 b is explained as follows.

The components of the second capture system 1 b are similar to the components of the first capture system 1 a . As illustrated in FIG. 1 , the second capture system 1 b includes a second absorber 20 b and a second stripper 30 b . The second absorber 20 b causes carbon dioxide contained in combustion exhaust gas 2 to be absorbed in the second absorbing liquid. The second absorbing liquid containing the absorbed carbon dioxide (a second rich liquid 4 b ) is supplied to the second stripper 30 b . The second stripper 30 b causes the carbon dioxide to be released from the first absorbing liquid and regenerates the absorbing liquid.

The second stripper 30 b includes an amine regenerator 31 b (packed bed). The amine regenerator 31 b is configured to cause the carbon dioxide to be released from the second rich liquid 4 b . The amine regenerator 31 b is configured as a countercurrent gas-liquid contact device.

A heat exchanger 32 b is provided between the second absorber 20 b and the second stripper 30 b . A second rich liquid pump 33 b is arranged between the second absorber 30 b and the second heat exchanger 32 b.

The second stripper 30 b is coupled to a second reboiler 34 b . The second reboiler 34 b uses a heating medium 6 b to heat the second lean liquid 5 b supplied from the second stripper 30 b to generate steam 7 . The reboiler 34 b supplies the generated steam 7 to the second stripper 30 b.

A second lean liquid cooler 35 b is provided between the heat exchanger 32 b and the second absorber 20 b . A cooling medium such as cooling water is supplied from an external source (not shown) to the lean liquid cooler 35 b . The second lean liquid cooler 35 b uses the cooling medium to cool the second lean liquid 5 b . As in the first capture system 1 a , the absorbing liquid circulates while cycling between being the second lean liquid 5 b and the second rich liquid 4 b . The second capture system 1 b illustrated further includes a gas cooler 37 b . The gas cooler 37 b is configured to cool the carbon dioxide-containing gas 8 discharged from the upper portion of the second stripper 30 b by using an external cooling medium, such as cooling water that is supplied from a source that is external to the carbon dioxide capture system.

As illustrated in FIG. 1 , the first capture system 1 further includes a compressor 40 that compresses the gas 8 cooled by the gas cooler 37 a , 37 b . In particular, moisture in the carbon dioxide-containing gas 8 is at least partially removed at the gas cooler 37 a , 37 b , and the carbon dioxide-containing gas 8 becomes mostly carbon dioxide. After undergoing the cooling process, the carbon dioxide-containing gas 8 is supplied to the compressor 40 . The carbon dioxide-containing gas 8 is compressed at the compressor 40 and stored in a container (not shown).

Next, the first absorbing liquid used in the first capture system 1 a and the second absorbing liquid used in the second capture system 1 b are explained.

One type of absorbing liquid may have a low releasing temperature, indicating that the absorbing liquid releases carbon dioxide at a low temperature compared to a basic absorbing liquid. In this embodiment, the second absorbing liquid is selected to release carbon dioxide at a lower temperature than the first absorbing liquid. For example, a general absorbing liquid may release carbon dioxide at 120 degrees Celsius, and the second absorbing liquid may be selected to release carbon dioxide at 100 degrees Celsius. Preferably, the first absorbing liquid and the second absorbing liquid each contain amine composites.

Examples of the first absorbing liquid amine composite could be alcoholic hydroxyl group-containing primary amines such as monoethanolamine, 2-amino-2-methyl-1-propanol, etc.; alcoholic hydroxyl group-containing secondary amines such as diethnolamine, 2-methylaminoethanol, etc., alcoholic hydroxyl group-containing tertiary amines such as triethanolamine, N-methyldiethanolamine, etc., polyethylenepolyamines such as ethylenediamine, triethylenediamine, diethylenetriamine, etc.; cyclic amines such as piperazines, piperidines, pyrrolidines, etc.; polyamines such as xylenediamine, etc.; amino acids such as methylaminocarboxylic acid, etc., and their mixtures. These amines are normally used in the form of 10 to 70 wt % aqueous solutions thereof. Besides, to the absorbing liquid, there may be added a carbon dioxide absorption promoting agent or a corrosion inhibitor. Further, methanol, polyethylene glycol, sulfolane, etc. may also be added to the absorbing liquid as other medium. Above mentioned composite could be also applied to the second absorbing liquid with mixing other composites.

And examples of the second absorbing liquid amine composite are such as N-(2-butyl-)-N-methylamino ethanol, N-(2-pentyl)-N-methylamino ethanol, N-(2-hexyl)-N-methylamino ethanol, N-(3-pentyl)-N-methylamino ethanol, N-(3-hexyl)-N-methylamino ethanol, N-(3-heptyl)-N-methylamino ethanol, N-(4-hextyl)-N-methylamino ethanol, N-(4-octyl)-N-methylamino ethanol, N-(5)-N-methylamino ethanol, N-(2-butyl-)-N-ethylamino ethanol, N-(2-pentyl)-N-ethylamino ethanol, N-(2-hexyl)-N-ethylamino ethanol, N-(3-pentyl-N-ethylamino ethanol, N-(3-hexyl)-N-ethylamino ethanol, N-(3-heptyl)-N-ethylamino ethanol, N-(4-heptyl)-N-ethylamino ethanol, N-(4-octyl)-N-ethylamino ethanol, N-(5-nonyl)-N-ethylamino ethanol, N-(2-butyl-)-N-methylamino propanol, N-(2-pentyl)-N-methylamino propanol, N-(2-hexyl)-N-methylamino propanol, N-(3-pentyl)-N-methylamino-propanol, N-(3-hexyl)-N-methyl-amino-propanol, N-(3-heptyl)-N-methylamino propanol, N-(4-heptyl)-N-methylamino propanol, N-(4-octyl)-N-methylamino propanol, N-(5-nonyl)-N-methyl-amino-propanol, N-(2-butyl)-N-ethylamino propanol, N-(2-pentyl)-N-ethylamino propanol, N-(2-hexyl)-N-ethylamino propanol, N-(3-pentyl)-N-ethylamino propanol, N-(3-hexyl)-N-ethylamino propanol, N-(3-heptyl)-N-ethylamino propanol, N-(4-heptyl)-N-ethylamino propanol, N-(4-octyl)-N-ethylamino propanol, N-(5-nonyl)-N-ethylamino propanol, N-(2-butyl-)-N-methylamino butanol, N-(2-pentyl)-N-methylamino butanol, N-(2-hexyl)-N-methylamino butanol, N-(3-pentyl)-N-methylamino butanol, N-(3-hexyl)-N-methylamino butanol, N-(3-heptyl)-N-methylamino butanol, N-(4-heptyl)-N-methylamino butanol, N-(4-octyl)-N-methylamino butanol, N-(5-nonyl)-N-methylamino butanol, N-(2-butyl)-N-ethylamino-butanol, N-(2-pentyl)-N-ethylamino butanol, N-(2-hexyl)-N-ethylamino butanol, N-(3-pentyl)-N-ethylamino butanol, N-(3-hexyl)-N-ethylamino butanol, N-(3-heptyl)-N-ethylamino butanol, N-(4-heptyl)-N-ethylamino butanol, N-(4-octyl)-N-ethylamino-butanol, N-(5-nonyl)-N-ethylamino butanol.

Other example of the second absorbing liquid amine composite are such as N-cyclopropyl-N-methyl amino ethanol, N-cyclobutyl-N-methyl amino ethanol, N-cyclopentyl-N-methyl amino ethanol, N-cyclohexyl-N-methyl amino ethanol, N-cycloheptyl-N-methyl amino ethanol, N-cyclooctyl-N-methyl amino ethanol.

As shown in FIG. 1 , the first discharged heating medium 6 b discharged from the first reboiler 34 a is supplied to the second reboiler 34 b as the second heating medium 6 b . Specially, an outlet of the first reboiler 34 a and an inlet of the second reboiler 34 b are connected by a first heating liquid supply line 41 , and the first discharged heating medium 6 b discharged from the first reboiler 34 a is used as the second heating medium 6 b.

During operation of the carbon dioxide capture system 1 , the combustion exhaust gas 2 discharged from a boiler (not shown) is separately introduced into the first capture system 1 a and the second capture system 1 b.

At the first capture system 1 a and the second capture system 1 b , the carbon dioxide in the combustion exhaust gas 2 is at least partially removed. The combustion exhaust gas 2 from which the carbon dioxide is at least partially removed is discharged as the decarbonated combustion exhaust gas 3 from the first absorber 20 a and the second absorber 20 b . In addition, the carbon dioxide is discharged as the carbon dioxide-containing gas 8 from the first stripper 30 a and the second stripper 30 b , and the carbon dioxide-containing gas 8 is supplied to the compressor 40 via the gas cooler 37 a,b . The carbon dioxide-containing gas 8 compressed by the compressor 40 is stored in a container (not shown).

During operation, high-temperature steam is supplied as the first heating medium 6 a from an external source, such as a turbine (not illustrated), to the first reboiler 34 a . The first lean liquid 5 a supplied to the first reboiler 34 a exchanges heat with the first heating medium 6 a so as to be heated and thus generates the steam 7 from the first lean liquid 5 a . The generated steam 7 is supplied to the lower portion of the first stripper 30 a and heats the first rich liquid 4 a within the first stripper 30 a , and the carbon dioxide is released from the first rich liquid 4 a.

For example, the heat amount of the first heating medium 6 a supplied to the first reboiler 34 a is adjusted so that the temperature of the first rich liquid 4 a is maintained at or above a temperature at which the first absorbing liquid releases carbon dioxide, for example at or above 120 degrees Celsius. By this process, the carbon dioxide is released from the first rich liquid 4 a efficiently.

As shown in FIG. 1 , the first discharged heating medium 6 b discharged from the first reboiler 34 a is supplied to the second reboiler 34 b as the second heating medium 6 b , which heats the second lean liquid 5 b.

In this embodiment, the carbon dioxide releasing temperature of the second rich liquid 4 b in the second stripper 30 b is lower than the carbon dioxide releasing temperature of the first rich liquid 4 a in the first stripper 30 a . Therefore, the first discharged heating medium 6 b has enough heat to sufficiently raise the temperature of the second lean liquid 5 b to create steam 7 that heats the second rich liquid 4 b sufficiently to release the carbon dioxide. And since the second lean liquid 5 b is heated by the first discharged heating medium 6 b , an additional, externally supplied heating medium other than the first discharged heating medium 6 b may advantageously be omitted.

Steam 7 is generated from the second lean liquid 5 b heated by the first discharged heating medium 6 b , and the steam 7 is supplied to the lower portion in the second stripper 30 b . In the second stripper 30 b , the second rich liquid 4 b is heated by the steam 7 , and the carbon dioxide is released from the second rich liquid 4 b.

The temperature of the second rich liquid 4 b is adjusted to be at or above a carbon dioxide releasing temperature of the second rich liquid 4 b , for example, at or above 100 degrees Celsius. The second rich liquid 4 b is selected to release carbon dioxide at a lower temperature than the first rich liquid 4 a . Therefore, at the second stripper 30 b , the second rich liquid 4 b releases the carbon dioxide by the heat of the steam 7 generated by the first discharged heating medium 6 b.

By above process, the first heating medium 6 a becomes the first discharged heating medium 6 b , which is used for heating the second lean liquid 5 b . Thus, the excess heat of the first heating medium 6 a , after it is discharged as the first discharged heating medium 6 b , is used efficiently at the second reboiler 34 b.

The carbon dioxide capture system 1 could be operated so that the efficiency of carbon dioxide captured at the first capture system 1 a and the second capture system 1 b are almost the same. However, in order to minimize the heat amount supplied from the first discharged heating medium 6 b , the percentages of captured carbon dioxide at the first capture system 1 a and the second capture system 1 b could be adjusted to be different values. For example, the percentage of captured carbon dioxide at the first capture system 1 a could be larger than the percentage of captured carbon dioxide at the second capture system 1 b . In this case, so that the percentage of captured carbon dioxide as a whole system becomes 90%, the percentage of captured carbon dioxide at the first capture system 1 a is adjusted to be 95%, and the percentage of captured carbon dioxide at the second capture system 1 b is adjusted to be 85%. Alternatively, the percentage of captured carbon dioxide at the first capture system 1 a could be less than the percentage of captured carbon dioxide at the second capture system 1 b.

In this embodiment, the temperature of the second rich liquid 4 b at the second stripper 30 b is generally lower than the temperature of the first rich liquid 4 a at the first stripper 30 a . Furthermore, the first heating medium 6 a discharged from the first reboiler 34 a is supplied to the second reboiler 34 b as the second heating medium 6 b . Thus, the second lean liquid 5 b is heated by the first heating medium 6 a . As a result, an externally supplied heating medium other than the first heating medium 61 could be omitted. The heat amount of the first discharged heating medium 6 b discharged from the first reboiler 34 a is used at the second reboiler 34 b efficiently. And total energy consumed at the carbon dioxide capture system 1 as a whole is advantageously reduced.

In addition, different types of absorbing liquid may be used as the first absorbing liquid and second absorbing liquid. As a result, low cost absorbing liquid could be applied to at least one of the first absorbing liquid and second absorbing liquid, and the cost of absorbing liquid for the entire system as a whole could be reduced. In addition, in the case the first absorbing liquid and second absorbing liquid have different deterioration characteristics, the timing of exchanging old for new absorbing liquid in the system due to deterioration of each absorbing liquid 4 a , 5 a could be different, which could be another benefit for system operation.

The case that the first capture system 1 a and the second capture system 1 b are provided in parallel was explained above. However, as shown FIG. 2 , plural of the first capture systems 1 a could be provided in parallel to a second capture system 1 b . In this case, the first discharged heating medium 6 b discharged from one or more of the parallel first reboiler 34 a is supplied to the second reboiler 34 b in the second capture system 1 b . This case also reduces the amount of energy of the carbon dioxide capture system 1 as a whole. Furthermore, multiple of the second capture system 1 b could be provided in parallel. And more than 3 types of the capture system could be provided and connected in order by using more than 3 types of absorbing liquid which have different carbon dioxide release temperature with respect to each other.

Second Embodiment

FIG. 3 shows a schematic diagram of a second embodiment of the carbon capture system. The carbon dioxide capture system 1 further includes a flashing device 50 . The flashing device 50 is provided at the first heating medium supply line 41 , and flashes the first heating medium 6 a by pressure reduction. The pressure of inside of the flashing device 50 is maintained lower than the pressure of an inside of the first heating medium supply line 41 . And, the first heating medium 6 a may include high temperature and high pressure drain water. When the first heating medium 6 a is introduced in the flashing device 50 , a portion of the first heating medium 6 a evaporates by pressure reduction.

The first heating medium 6 a has a relatively high temperature when it is supplied from the turbine (not shown) to the first reboiler 34 a . However, the temperature of the first heating medium 6 a is decreased by heating the first lean liquid 5 a at the first reboiler 34 a , and a portion of the first discharged heating medium 6 b could condense and liquefy. Therefore, by flashing the first discharged heating medium 6 b by the flashing device 50 , the first discharged heating medium 6 b is at least partially vaporized, and efficiency of heat exchanging between the first discharged heating medium 6 b and the second lean liquid 5 b at the second reboiler 34 b is improved.

As shown in FIG. 3 , the third reboiler 51 could be provided to heat the second lean liquid 5 b . Even if the heat amount of the first discharged heating medium 6 b , after being flashed, is too low for heating the second lean liquid 5 b , the third reboiler 51 adds sufficient heat to the first discharged heating medium 6 b to heat the second lean liquid 5 b.

As with the first heating medium 6 a in the first embodiment, high temperature steam supplied from an external source, such as a low pressure turbine source (not shown) could be used as the heating medium 9 b supplied to the third reboiler 51 . The third reboiler 51 also could be provided in other embodiments.

The pressure in the first stripper 30 a could be higher than the pressure in the second stripper 30 b . In this case, a maintenance bulb 52 could be provided. By adjusting the opening of the maintenance bulb 52 , the pressure in the first stripper 30 a is controlled. Reducing the size of an opening of the maintenance bulb 52 may cause the pressure in the first stripper 30 a to increase, and may also cause the temperature of the first rich liquid 4 a to increase in the first stripper 30 a.

The first rich liquid 4 a may be a general absorbing liquid that releases carbon dioxide at a selected temperature, for example at 120 degrees Celsius. As the pressure in the first stripper 30 a is increased, the temperature at which the first rich liquid 4 a releases carbon dioxide also increases. For example, at 200 KPa in the first stripper 30 a , the first rich liquid 4 a releases carbon dioxide at 120 degrees Celsius. Or for example, at 100 KPa in the first stripper 30 a , the first rich liquid 4 a releases carbon dioxide at 90 degrees Celsius. The second capture system 1 b uses the second absorbing liquid that releases carbon dioxide at a lower temperature than the first absorbing liquid. Therefore, the pressure in the second stripper 30 b could be set at the same or a lower pressure than the first stripper 30 a . In other embodiment, the pressure in the first stripper 30 a could be set higher than the pressure of the second stripper 30 b.

In this embodiment, the flashing device 50 flashes the first discharged heating medium 6 b by reduction of pressure. The pressure of an inside of the flashing device 50 is maintained lower than the pressure of an inside of the first heating medium supply line 41 . Thus, even in the condition that the portion of the first discharged heating medium 6 b is condensed and liquefied, the first discharged heating medium 6 b is evaporated by flashing in the flashing device 50 , and the efficiency of the heat exchange between the second lean liquid 5 b and the first discharged heating medium 6 b is improved.

Third Embodiment

FIG. 4 shows a schematic diagram of the carbon dioxide capture system according to a third embodiment. In this embodiment, as shown in FIG. 4 , the second capture system 1 b further includes a fourth boiler 53 as compared to the first embodiment. The fourth boiler 53 heats the second lean liquid 5 b by the carbon dioxide-containing gas 10 b discharged from the first stripper 30 a . The fourth boiler 53 is provided upstream of the second reboiler 34 b . Thus, the second lean liquid 5 b is heated by the fourth reboiler 53 , the second reboiler 34 b , and the third reboiler 51 , in that order.

The top portion of the first stripper 30 a and the inlet of the fourth reboiler 53 are connected by a carbon dioxide-containing gas supply line 54 . And the outlet of the fourth reboiler 53 and the first gas cooler 37 a are connected by the carbon dioxide-containing gas discharge line 55 . By this components, the carbon dioxide-containing gas 10 b discharged from the first stripper 30 a is supplied to the fourth reboiler 53 via the carbon dioxide-containing gas supply line 54 .

In this embodiment, the carbon dioxide releasing temperature of the second rich liquid 4 b in the second stripper 30 b may be lower than the carbon dioxide releasing temperature of the first rich liquid 4 a in the first stripper 30 a . Therefore, the carbon dioxide-containing gas 10 b discharged from the first stripper 30 a has an amount of heat that is capable of heating the second lean liquid 5 b at the fourth reboiler 53 . The second lean liquid 5 b is heated by heat exchanging with the carbon dioxide-containing gas 10 b . After heating, the carbon dioxide-containing gas 10 b is discharged from the fourth reboiler 53 and supplied to the first gas cooler 37 a via the carbon dioxide-containing gas discharge line 55 .

In this embodiment, the second lean liquid 5 b is heated by heat exchanging with the carbon dioxide-containing gas 10 b . By this process, an excess heat amount of the carbon dioxide-containing gas 10 b is used at the fourth reboiler 53 efficiently, and recovery energy of the carbon dioxide capture system 1 as a whole is reduced.

Furthermore, the carbon dioxide-containing gas 10 b discharged from the first stripper 30 a is cooled at the fourth reboiler 53 . By this process, the cooling capacity, such as amount of cooling medium, at the first gas cooler 37 may advantageously be reduced.

This embodiment is not limited to the case that the second rich liquid 5 b flows through the fourth reboiler 53 , the second reboiler 34 b , the third reboiler 51 , in that order, as explained above. For example, if the fourth reboiler 53 and the second reboiler 34 b have enough heat to sufficiently heat the second lean liquid 5 b , the third reboiler 51 could be omitted.

Fourth Embodiment

In this embodiment, as shown in FIG. 5 , the second capture system 1 b further includes a fifth boiler 56 as compared to the first embodiment. The fifth boiler 56 heats the second lean liquid 5 b by the first lean liquid 5 a discharged from the first stripper 30 a . After heating the second lean liquid 5 b , the first lean liquid 5 a is supplied to the first absorber 20 a via the first heat exchanger 32 a.

Specially, the bottom portion of the first stripper 30 a and the inlet of the fifth reboiler 56 are connected by the first lean liquid supply line 57 . And the outlet of the fifth reboiler 56 and the first exchanger 32 a is connected by the first lean liquid discharge line 58 . By these components, the first lean liquid 5 a discharged from the first stripper 5 a is supplied to the fifth reboiler 56 .

In this embodiment, the carbon dioxide releasing temperature of the first rich liquid 4 b in the second stripper 30 b is lower than the carbon dioxide releasing temperature of the first rich liquid 4 a in the first stripper 30 a . Therefore, the first rich liquid 4 a discharged from the first stripper 30 a has an amount of heat that is capable of heating the second lean liquid 5 b at the fifth reboiler 56 . The second lean liquid 5 b is heated by heat exchanging with the first rich liquid 4 a . After heating, the first rich liquid 4 a is discharged from the fifth reboiler 56 and supplied to the first heat exchanger 32 a via the first lean liquid discharge line 58 .

As shown in FIG. 5 , the first rich liquid 4 a supplied to the first stripper 30 a from the first heat exchanger 32 a may preferably be heated. Therefore, a heater 59 could be provided between the first heat exchanger 32 a and the first stripper 30 a . The first rich liquid 4 a is heated by the heater 59 , and supplied to the first stripper 30 a.

The heater 59 heats the first rich liquid 4 a by using the first discharged heating medium 6 b discharged from the first reboiler 34 a . Specially, the outlet of the first reboiler 34 a and the inlet of the heater 59 are connected by the first heating medium supply line 60 . By these components, the first discharged heating medium 6 b discharged from the first reboiler 34 a is supplied to the heater 59 via the first heating medium supply line 60 . After the first heating medium 6 a heats the first lean liquid 5 a at the first reboiler 34 a , the first discharged heating medium 6 b is supplied to the heater 59 to heat the first rich liquid 4 a.

By heat exchange at the fifth reboiler 56 , the temperature of the first lean liquid 5 a could be reduced, which could otherwise cause the temperature of the first rich liquid 4 a supplied to the first stripper 30 a from the first heat exchanger 32 a to be too low. However, by heating the first rich liquid 4 a by the heater 59 , the temperature of the first rich liquid 4 a is sufficiently raised.

An additional heater (not shown) could be provided between the heater 59 and the first stripper 30 a . In this case, the first rich liquid 4 a discharged from the first stripper 30 a is heated by the additional heater. By this process, even in the condition that the first rich liquid 4 a is not heated to a sufficient temperature by the heater 59 , the additional heater heats first rich liquid 4 a to the sufficient temperature. The additional heater could use steam supplied from external components (such as low pressure turbine) as heat medium, or could use another source as a heat medium.

In this embodiment, instead of the heater 59 , the second reboiler 34 b (shown in FIG. 1 ) could be provided at a position downstream of the fifth reboiler 56 . In the case the heat amount supplied to the fifth reboiler from the first lean liquid 5 a is insufficient to adequately heat the second lean liquid 5 b , the second reboiler 34 b could heat the second lean liquid 5 b further.

As in the first embodiment, the first discharged heating medium 6 b discharged from the first reboiler 34 a may preferably be supplied to the second reboiler 34 b as the second heating medium. And the third reboiler 51 and fourth reboiler 53 could be provided at positions downstream of the fifth reboiler 56 . In this case, the heater 59 could heat the first rich liquid 4 a . Here, in case the fourth reboiler 53 has less capacity than the fifth reboiler 56 , the fourth reboiler 53 is preferably provided upstream of the fifth reboiler 56 .

In this embodiment, the second lean liquid 5 b is heated at the fifth boiler 56 by the first lean liquid 5 a discharged from the first stripper 30 a . By this process, the heat amount of the first lean liquid 5 a discharged from the first stripper 30 a is used efficiently at the fifth reboiler 56 . Thus, recovery energy of the carbon dioxide capture system 1 as a whole system is reduced.

Furthermore, the heater 59 heats the first rich liquid 4 a supplied to the first stripper 30 a from the first absorber 20 a . By this process, even in the case that the temperature of the first lean liquid 5 a becomes low temperature by heat exchange, the temperature of the first rich liquid 4 a could be raised. And the heat amount of the first heating medium 6 a is used efficiently. Thus, recovery energy of the carbon dioxide capture system 1 as a whole system could be reduced.

Fifth Embodiment

In this embodiment, as shown in FIG. 6 , the first cooling medium 36 a discharged from the second lean liquid cooler 35 b is supplied to the first lean liquid cooler 35 a as the first cooling medium 36 a . Especially, the outlet of the second lean liquid cooler 35 b and the inlet of the first lean liquid cooler 35 a are connected by the cooling medium supply line 60 . By these components, the first lean liquid 5 a supplied to the first absorber 20 a is cooled by the first cooling medium 36 a at the first lean liquid cooler 35 a.

In this embodiment, the carbon dioxide releasing temperature of the second rich liquid 4 b in the second stripper 30 b is lower than the carbon dioxide releasing temperature of the first rich liquid 4 a in the first stripper 30 a . Therefore, the temperature of the second lean liquid 5 b supplied to the second absorber 20 b tends to be lower than the temperature of the first lean liquid 5 a supplied to the first absorber 20 a . And, the temperature of the first cooling medium 36 a discharged from the second lean liquid cooler 35 b becomes a low temperature capable of cooling the first lean liquid 5 a . As a result an externally supplied cooling medium to cool the first lean liquid 5 a may advantageously be omitted.

An additional cooler (not shown) could be provided between the first lean liquid cooler 35 a and the first absorber 30 a . In this case, the first lean liquid 5 a discharged from the first lean liquid cooler 35 a is cooled by the additional cooler. By this process, even in the condition that the first lean liquid is not cooled sufficiently by the first lean liquid cooler 35 a , the additional cooler cools the first lean liquid 5 a further. For example, the additional cooler could use cooling water supplied from external components as a cooling medium.

In this embodiment, the first cooling medium 36 a is discharged from the second lean liquid cooler 35 b and supplied to the first lean liquid cooler 35 a as the first cooling medium 36 a . By this process, an externally supplied cooling medium as the first cooling medium 36 a is omitted. And amount of cooling medium as a whole system is reduced. Instead of the case of the first discharged heating medium 6 b being supplied to the second reboiler 34 b , external steam such as turbine (not shown) could be supplied to the second reboiler 34 b instead of using the first discharged heating medium 6 b discharged from the first reboiler 34 a.

Sixth Embodiment

FIG. 7 shows a schematic diagram of a system according to the sixth embodiment in which a flow control device 61 is further provided. The flow control device 61 controls the first flow amount of the combustion exhaust gas 2 supplied to the first absorber 20 a and the second flow amount of the combustion exhaust gas 2 supplied to the second absorber 20 b . As shown in FIG. 7 , the flow control device 61 could be provided at the branching point of the combustion exhaust gas 2 supplied to the first absorber 20 a and the second absorber 20 b . Or the flow control device 61 could be composed by control bulbs provided downstream of the branching point of the combustion exhaust gas 2 .

Furthermore, in his embodiment, an inlet concentration meter 62 may be further provided. The inlet concentration meter 62 measures the carbon dioxide concentration of the combustion exhaust gas 2 supplied to the first absorber 20 a and second absorber 20 b . And a first outlet concentration meter 63 and a second outlet concentration meter 64 may be further provided. The first outlet concentration meter 63 measures the carbon dioxide concentration of the decarbonated combustion exhaust gas 3 discharged from the first absorber 20 a . The second outlet concentration meter 64 measures the carbon dioxide concentration of the decarbonated combustion exhaust gas 3 discharged from the second absorber 20 b . By measuring the carbon dioxide concentration by these concentration meters, a percentage of carbon dioxide captured by the carbon dioxide capture system 1 is calculated at controller 67 (explained below).

A first heat amount calculator 65 and a second heat amount calculator 66 may be further provided. The first heat amount calculator 65 and the second heat amount calculator 66 may include a programmable processor and a memory. The first heat amount calculator 65 calculates the heat amount supplied to the first reboiler 34 a . The second heat amount calculator 66 calculates the heat amount supplied to the second reboiler 34 b . The first heat amount calculator 65 measures the flow amount, the pressure and the temperature of the first heating medium 6 a which is supplied to the first reboiler 34 a . The first heat amount calculator 65 also measures the flow amount, the pressure and the temperature of the first discharged heating medium 6 b after it is discharged from the first reboiler 34 a . As with the first heat amount calculator 65 , the second heat amount calculator 66 measures the flow amount, the pressure and the temperature of the heating medium before and after it is supplied to the second reboiler 34 b.

Furthermore, a controller 67 is provided. The signals of carbon dioxide concentration measured at the inlet concentration meter 62 , the first outlet concentration meter 63 and the second outlet concentration meter 64 are sent to the controller 67 . The signals of the flow amount, the pressure and the temperature measured at the first heat amount calculator 65 and second heat amount calculator 66 are also sent to the controller 67 .

The controller 67 controls the first flow amount of the combustion exhaust gas 2 and second flow amount of the combustion exhaust gas 2 so that the total value of the heat amount supplied to the first reboiler 34 a and the second reboiler 34 a is minimized.

In particular, the controller 67 calculates the first flow amount and the second flow amount so that the total value of the heat amount supplied to the reboiler 34 a,b becomes a minimum value. For example, the relation between the first flow amount, second flow amount and the total heat amount supplied to the reboiler 34 a,b , are measured and memorized at the controller 67 in advance, and the controller 67 seeks the value of the first flow amount and the second flow amount at which the total value of the heat amount supplied to the first reboiler 34 a and the second reboiler 34 b becomes a minimum value.

The heat amount supplied to the first reboiler 34 a is calculated by the difference between the heat amount of the first heating medium 6 a before it is supplied to the first reboiler 6 a and the heat amount of the first discharged heating medium 6 b after it is discharged from the first reboiler 34 a.

Especially, in the case that the first heating medium 61 is saturated vapor, the weight ratio of the first heating medium 6 a is calculated by the flow amount and the pressure of the first heating medium 6 a before it is supplied to the first reboiler 34 a . The weight flow amount is calculated by the weight ratio, and the heat amount of the first heating medium 6 a before it is supplied to the first reboiler 34 a is calculated by the weight flow amount and the temperature. The heat amount of the first discharged heating medium 6 b after it is discharged by the first reboiler 34 a is calculated in the same way. After this process, the heat amount supplied to the first reboiler 34 a is calculated based on the difference between the heat amount of the first heating medium 6 a before it is supplied to the first reboiler 34 a and the heat amount of the first discharged heating medium 6 b after it is discharged from the first reboiler 34 a.

The heat amount supplied to the second reboiler 34 b is calculated by the difference between the heat amount of the first discharged heating medium 6 b before and after it is supplied to the second reboiler 34 b.

In this embodiment, the controller 67 controls the first flow amount of the combustion exhaust gas 2 and second flow amount of the combustion exhaust gas 2 so that the total value of the heat amount supplied to the first reboiler 34 a and the heat amount supplied to the second reboiler 34 a is minimized. By this process, the heat supplied to the carbon capture system 1 as a whole is reduced.

Instead of the case that the first heating medium 6 a is saturated vapor, in the case that the first heating medium 6 a is heated vapor, the weight ratios are calculated by the pressure and the temperature of the heated vapor, and the heat amounts are calculated by the weight ratios of the heated vapor.

The case that the first discharged heating medium 6 b discharged from the first reboiler 34 a is supplied to the second reboiler 34 b as the second heating medium was explained above. However, the disclosed embodiments are not limited to this case. For example, an external heating medium could be supplied as the second heating medium supplied to the second reboiler 34 b . In this case, the controller 67 also controls the first flow amount of the combustion exhaust gas 2 and second flow amount of the combustion exhaust gas 2 so that the total value of the heat amount supplied to the first reboiler 34 a and the heat amount supplied to the second reboiler 34 a becomes a minimum value.

A more complete appreciation of the invention and many of the attendant advantages thereof will be readily obtained as the same becomes better understood by reference to the following detailed description when considered in connection with the accompanying drawings, wherein.