CO2 recovery apparatus and CO2 recovery method

The present invention relates to a CO 2 recovery apparatus and a CO 2 recovery method for reducing concentration of amine compounds remaining in and being emitted from a decarbonated exhaust gas from which CO 2 has been removed by being contacted with an absorbing liquid.

As a cause of global warming, the greenhouse effect due to CO 2 is pointed out, and countermeasures against the same must be quickly taken internationally in saving the global environment. Various fields of human activity burning fossil fuel as generation sources of CO 2 , the demand for suppression of CO 2 emissions is further increasing. Accordingly, for power generation facilities such as thermal power plants and the like using a large amount of fossil fuel, a method that exhaust gas from a boiler is contacted with an amine-based absorbing liquid such as an aqueous solution of amine compound so as to remove CO 2 in the exhaust gas and recover the same is energetically studied.

When recovering CO 2 from exhaust gas using such an absorbing liquid, a decarbonated exhaust gas from which the CO 2 is recovered is accompanied by the absorbing liquid and anime compounds derived from the absorbing liquid. Additionally, in order to prevent air pollution by the amine compounds, it is necessary to reduce the discharge amount of the amine compounds which are emitted together with the decarbonated exhaust gas.

Conventionally, Patent Literature 1 discloses that plural stages of water washing portions which recover an amine compound accompanied by a decarbonated exhaust gas by bringing a washing liquid into contact with the decarbonated exhaust gas from which CO 2 is absorbed and removed by a gas-liquid contact with an absorbing liquid are provided, and a recovery process of an amine compound accompanying a decarbonated exhaust gas is sequentially performed in the plural stages of the water washing portions. For the washing liquid of Patent Literature 1, condensed water obtained by condensing and separating moisture contained in CO 2 in a process where CO 2 is diffused from an amine-based absorbing liquid which has absorbed the CO 2 so as to regenerate the amine-based absorbing liquid is used.

Further, conventionally, Patent Literature 2 discloses that a cooling portion where a decarbonated exhaust gas from which CO 2 is absorbed and removed by a gas-liquid contact with an absorbing liquid is cooled, and a contact portion where condensed water which has been condensed in the cooling portion and the decarbonated exhaust gas are in counterflow contact with each other. Furthermore, Patent Literature 2 discloses that a water washing portion which recovers an amine compound accompanying a decarbonated exhaust gas by bringing a washing liquid into contact with the decarbonated exhaust gas from which CO 2 is absorbed and removed by a gas-liquid contact with an absorbing liquid are provided, and for the washing liquid, condensed water which has been condensed in a cooling tower where exhaust gas before CO 2 is recovered therefrom is used.

Patent Literatures

Patent Literature 1: Japanese Patent Application Laid-open No. 2002-126439

Patent Literature 2: Japanese Patent Application Laid-open No. 8-80421

Technical Problem

However, in recent years, it is desired to further reduce concentration of components of an absorbing liquid remaining in and being emitted from a decarbonated exhaust gas in terms of environmental preservation. Especially, when installing CO 2 recovery apparatuses for exhaust gas from thermal power plants and the like which have a large amount of flow of processing gas anticipated in the future, a large amount of exhaust gas is emitted, and thereby the emission amount of components of an absorbing liquid remaining in and being emitted from a decarbonated exhaust gas tends to increase. Therefore, it is necessary to further reduce the concentration of emitted components of an absorbing liquid.

The present invention is to solve the above-mentioned problem and to provide a CO 2 recovery apparatus and a CO 2 recovery method capable of further reducing concentration of amine compounds remaining in and being emitted from a decarbonated exhaust gas.

Solution to Problem

According to a first aspect of the present invention in order to solve the problem, there is provided a CO 2 recovery apparatus including: a CO 2 absorption tower for bringing a CO 2 -containing exhaust gas containing CO 2 and a CO 2 absorbing liquid into contact with each other so as to remove CO 2 and make a purified exhaust gas; and an absorbing liquid regeneration tower for separating CO 2 from the CO 2 absorbing liquid which has absorbed CO 2 so as to regenerate the CO 2 absorbing liquid, wherein a lean solution from which CO 2 has been removed in the absorbing liquid regeneration tower is reused in the CO 2 absorption tower, and wherein the CO 2 absorption tower comprises: a CO 2 absorption portion for absorbing CO 2 in the CO 2 -containing exhaust gas by the CO 2 absorbing liquid, a water washing portion for cooling a CO 2 -removed exhaust gas by a washing liquid and for recovering the CO 2 absorbing liquid which accompanies the same, the water washing portion being provided on a side of a downstream flow of a gas flow of the CO 2 absorption portion; a washing liquid circulation line for supplying the washing liquid containing the CO 2 absorbing liquid recovered in the water washing portion from a side of a top of the water washing portion so as to circulate and wash the washing liquid; an extraction line for extracting a part of the washing liquid containing the CO 2 absorbing liquid as an extracted liquid from the washing liquid circulation line; a concentration portion for concentrating the CO 2 absorbing liquid while separating a gas component from the extracted liquid; and a concentrated liquid feed line for feeding a concentrated liquid concentrated in the concentration portion to the absorbing liquid regeneration tower.

According to a second aspect of the present invention, there is provided the CO 2 recovery apparatus according to the first aspect including a gas exhaust line for merging the gas component into the purified exhaust gas exhausted from the CO 2 absorption tower.

According to a third aspect of the present invention, there is provided the CO 2 recovery apparatus according to the first aspect wherein a cooling tower for cooling the CO 2 -containing exhaust gas containing CO 2 is provided on a side of an upstream flow of the CO 2 absorption tower so as to set a temperature (T 2 ) of the purified exhaust gas exhausted from the CO 2 absorption tower lower than a temperature (T 1 ) of the CO 2 -containing exhaust gas containing CO 2 cooled in the cooling tower (T 1 >T 2 ).

According to a fourth aspect of the present invention, there is provided the CO 2 recovery apparatus according to the first aspect wherein a water is supplied to the water washing portion from an outside or an inside of a system.

According to a fifth aspect of the present invention, there is provided a CO 2 recovery method for using a CO 2 absorption tower for removing CO 2 by bringing a CO 2 -containing exhaust gas containing CO 2 and a CO 2 absorbing liquid into contact with each other so as to remove CO 2 and an absorbing liquid regeneration tower for regenerating the CO 2 absorbing liquid by separating CO 2 from the CO 2 absorbing liquid absorbing CO 2 so as to reuse a lean solution from which CO 2 has been removed in the absorbing liquid regeneration tower in the CO 2 absorption tower, wherein a CO 2 -removed exhaust gas is cooled by a washing liquid and also part of a water washing portion for recovering the CO 2 absorbing liquid which accompanies the same is extracted as an extracted liquid in a side of a downstream flow of the CO 2 absorption tower, and wherein the CO 2 absorbing liquid in the extracted liquid is concentrated and the concentrated liquid is fed to a side of the absorbing liquid regeneration tower.

Advantageous Effects of Invention

According to the present invention, concentration of amine compounds of an absorbing liquid remaining in and being emitted from a decarbonated exhaust gas can be further reduced, and also recovered absorbing liquid can be concentrated to be reused.

FIG. 1 is a schematic view of a CO 2 recovery apparatus according to a first embodiment.

FIG. 2 is a schematic view of another recovery apparatus according to First embodiment.

FIG. 3 is a schematic view of another recovery apparatus according to First embodiment.

FIG. 4 is a schematic view of a CO 2 recovery apparatus according to a second embodiment.

Hereunder, the present invention will be specifically described referring to the figures. Note that the present invention is not limited by these embodiments, and when there are plural embodiments, they include what are configured by combining each embodiment. Further, components in the embodiments below include what a person skilled in the art can easily conceive or what is substantially identical to the same.

First Embodiment

The CO 2 recovery apparatus according to the present invention will be described referring to the figures. FIG. 1 is a schematic view of the CO 2 recovery apparatus according to a first embodiment. FIG. 2 and FIG. 3 are schematic views of another recovery apparatuses according to the first embodiment.

As illustrated in FIG. 1 , a CO 2 recovery apparatus 10 A according to this embodiment includes a CO 2 absorption tower (hereunder, also referred to as “absorption tower”) 13 where a CO 2 -containing exhaust gas 11 A which contains CO 2 and a CO 2 absorbing liquid (a lean solution 12 B) are contacted with each other so as to remove CO 2 , thereby obtaining a purified exhaust gas 11 B, an absorbing liquid regeneration tower 14 where a CO 2 absorbing liquid which has absorbed CO 2 (a rich solution 12 A) is regenerated, a CO 2 absorption portion 13 A which is a CO 2 recovery apparatus reusing the lean solution B from which CO 2 has been removed in the absorbing liquid regeneration tower (hereunder, also referred to as “regeneration tower”) 14 , and in which the CO 2 absorption tower 13 absorbs CO 2 in the CO 2 -containing exhaust gas 11 A with a CO 2 absorbing liquid 12 (the lean solution 12 B), a water washing portion 13 B which is composed of a first water washing portion 13 B 1 and a second water washing portion 13 B 2 provided on the upper (the downstream flow of the gas flow) side of the CO 2 absorption portion 13 A for cooling CO 2 -removed exhaust gas as well as recovering the accompanying CO 2 absorbing liquid 12 , a washing liquid circulation line L 1 where a washing liquid 20 containing the CO 2 absorbing liquid 12 which has been recovered at the second water washing portion 13 B 2 on the tower top portion side is directly circulated from the top side of the water washing portion 13 B, an extraction line L 2 where part of the washing liquid 20 containing the CO 2 absorbing liquid 12 is extracted as an extracted liquid 21 from the washing liquid circulation line L 1 , a concentration portion 22 where a gas component (water vapor) 24 is separated from the extracted liquid 21 while the CO 2 absorbing liquid is concentrated, a concentrated liquid feed line L 3 where the concentrated liquid 23 which has been concentrated in the concentration portion 22 is fed to the absorbing liquid regeneration tower 14 side, and a gas exhaust line L 4 where the separated gas component (water vapor) 24 is merged into the purified exhaust gas 11 B exhausted from the absorption tower 13 .

Note that the washing liquid 20 is circulated in the first water washing portion 13 B 1 as well in combination with the washing liquid circulation line L 1 .

Also note that, although not illustrated, the extracted liquid 21 from the first water washing portion 13 B 1 is merged into the CO 2 absorbing liquid 12 .

In the absorption tower 13 , the CO 2 -containing exhaust gas 11 A is brought into counterflow contact with the alkanolamine-based CO 2 absorbing liquid 12 in the CO 2 absorption portion 13 A provided on the lower side of the CO 2 absorption tower 13 , and CO 2 in the CO 2 -containing exhaust gas 11 A is absorbed by the CO 2 absorbing liquid 12 by a chemical reaction (R—NH 2 +H 2 O+CO 2 →R—NH 3 HCO 3 ).

Then, the CO 2 -removed exhaust gas after CO 2 is removed rises to the water washing portion 13 B side via a chimney tray 16 and is brought into gas-liquid contact with the washing liquid 20 supplied from the top side of the water washing portion 13 B so as to recover the CO 2 absorbing liquid 12 accompanying the CO 2 -removed exhaust gas.

After that, the purified exhaust gas 11 B from which the CO 2 absorbing liquid 12 has been removed is exhausted outside from a tower top portion 13 C of the CO 2 absorption tower 13 . Note that a sign 73 indicates a mist eliminator which captures mist in gas.

The rich solution 12 A having absorbed CO 2 is boosted by a rich solvent pomp 51 interposed in a rich solution supply tube 50 , heated by the lean solution 12 B regenerated in the absorbing liquid regeneration tower 14 in a rich/lean solution heat exchanger 52 , and supplied to the top side of the absorbing liquid regeneration tower 14 .

The rich solution 12 A emitted from the top side of the regeneration tower 14 to the inside of the tower emits most of CO 2 by heating by means of water vapor from the tower bottom. The CO 2 absorbing liquid 12 emitting part or most of CO 2 in the regeneration tower 14 is called “semi-lean solution”. The semi-lean solution, not illustrated, becomes the lean solution 12 B from which almost all CO 2 has been removed when it flows down to the bottom of the regeneration tower 14 . The lean solution 12 B is heated by saturated water vapor 62 in a regeneration heater 61 interposed in a circulation line L 20 . The saturated water vapor 62 after heating becomes water-vapor-condensed water 63 .

On the other hand, a CO 2 gas 41 accompanied by water vapor dissipated from the rich solution 12 A and the semi-lean solution, not illustrated, in the tower is emitted from a tower top portion 14 A of the regeneration tower 14 .

Then, the CO 2 gas 41 accompanied by water vapor is guided out by a gas exhaust line L 21 , the water vapor is concentrated by a condenser 42 interposed in the gas exhaust line L 21 , a condensed water 44 is separated in a separation drum 43 , and a CO 2 gas 45 is emitted out of the system and separately subjected to post-processing such as compression recovery.

The condensed water 44 which has been separated in the separation drum 43 is supplied to the upper portion of the absorbing liquid regeneration tower 14 by a condensed water circulation pump 46 interposed in a condensed water line L 22 .

Note that, although not illustrated, part of the condensed water 44 is supplied to the top of the water washing portion 13 B as the washing liquid 20 of the CO 2 absorbing liquid and used for absorbing the CO 2 absorbing liquid 12 accompanying the CO 2 -removed exhaust gas.

The regenerated CO 2 absorbing liquid (lean solution 12 B) is sent to the CO 2 absorption tower 13 side by a lean solution pump 54 via a lean solution supply tube 53 , and circulatedly used as the CO 2 absorbing liquid 12 .

Accordingly, the CO 2 absorbing liquid 12 forms a closed passage circulating through the CO 2 absorption tower 13 and the absorbing liquid regeneration tower 14 , and is reused in the CO 2 absorption portion 13 A of the CO 2 absorption tower 13 . Note that the CO 2 absorbing liquid 12 is supplied by a replenishment line which is not illustrated as necessary, and a CO 2 absorbing liquid is regenerated by a reclaimer which is not illustrated as necessary.

Additionally, the CO 2 -containing exhaust gas 11 A supplied to the CO 2 absorption tower 13 is cooled by cooling water 71 in a cooling tower 70 provided to its front stage side, and then introduced into the CO 2 absorption tower 13 . Note that a sign 72 indicates a circulation pump, a sign 74 indicates a cooling apparatus, L 10 indicates a cooling water circulation line, L 11 indicates a CO 2 -containing exhaust gas supply line, and L 12 indicates a purified exhaust gas exhaust line, respectively.

Thus, the CO 2 absorbing liquid 12 which is circulatedly used through the CO 2 absorption tower 13 and the absorbing liquid regeneration tower 14 brings a CO 2 -removed exhaust gas from which CO 2 has been removed and the washing liquid 20 into counterflow contact with each other and the CO 2 absorbing liquid 12 accompanying the CO 2 -removed exhaust gas is absorbed and removed by the washing liquid 20 in the water washing portion 13 B so as to prevent diffusion to the outside of the absorption tower 13 .

In order to reuse the CO 2 absorbing liquid 12 absorbed and removed by the washing liquid 20 , in this embodiment, a concentration portion 22 is provided and the CO 2 absorbing liquid 12 is fed to the absorbing liquid regeneration tower 14 side via a concentrated liquid feed line L 3 which feeds a concentrated liquid 23 which is concentrated in the concentration portion 22 so as to concentrate and use the CO 2 absorbing liquid 12 .

In this embodiment, part of the washing liquid 20 circulating in the water washing portion 13 B is extracted and concentrated in the concentration portion 22 to make the concentrated liquid 23 which is fed to the separation drum 43 separating CO 2 in the absorbing liquid regeneration tower 14 .

The separation drum 43 separates the CO 2 gas 45 from the CO 2 gas 41 accompanied by water vapor so as to obtain the condensed water 44 which is recirculated to the upper portion of the absorbing liquid regeneration tower 14 , thereby being the lean solution 12 B to be reused in the CO 2 absorption tower 13 again.

Note that a supply destination of the concentrated liquid 23 is not limited to the separation drum 43 , and it may be the condensed water line L 22 which returns the condensed water 44 to the upper portion of the regeneration tower 14 as illustrated in FIG. 2 , for example.

Also, the supply destination of the concentrated liquid 23 may be directly introduced to the upper portion of the regeneration tower 14 , as illustrated in FIG. 3 .

Also, part of the condensed water 44 (* 1 ) may be extracted from the condensed water line L 22 and supplied to the washing liquid circulation line L 1 (* 1 ) so as to be used as a washing liquid.

Also, part of the cooling water 71 of the cooling tower 70 (* 2 ) may be extracted and supplied to the washing liquid circulation line L 1 (* 2 ) so as to be used as a washing liquid.

Also, other than water inside the system of the CO 2 recovery apparatus, water from the outside of the system (for example, ion exchange water of a process system or the like) may be supplied to the washing liquid circulation line L 1 (* 3 ) so as to be used as a washing liquid.

Thus, in this embodiment, when the washing liquid 20 is circulated in the washing liquid circulation line L 1 , it recovers a CO 2 absorbing liquid and the recovered CO 2 absorbing liquid is made to a concentrated liquid, and thereby the amount of diffusion of a CO 2 absorbing liquid accompanying the purified exhaust gas 11 B and a volatile component derived from the absorbing liquid into the air can be reduced.

Note that, in the concentration portion 22 , an evaporation apparatus and a vapor compressing concentration apparatus or the like, for example, can be used. The evaporation apparatus in which the washing liquid 20 is heated to be evaporated while being stored in an evaporator, the concentrated liquid 23 is supplied to the next evaporator, and also the water vapor 24 can be used as a heating source in the next evaporator, and the evaporators are provided plurally can be exemplified.

Also, the vapor compressing concentration apparatus pressurizes the water vapor 24 generated in the evaporator with a compressor so as to raise the temperature, thereby using the same as a heat source for heating, and can reduce power consumption upon concentration.

Note that, water vapor may be supplied upon concentration.

Additionally, in the gas exhaust line L 4 to which the gas component (water vapor) 24 separated in the concentration portion 22 is guided out, a separation drum is provided to prevent accompaniment of moisture to the outside and also prevent dissipation of moisture to the outside of the system.

Note that, when introducing the gas component 24 to the side of the tower top portion 13 C of the absorption tower 13 , it is emitted to the outside as it is. Therefore, in a case of being accompanied by ammonia, it may be introduced to the downstream flow side (inside of the tower top portion) of the water washing portion 13 B thereof.

Second Embodiment

FIG. 4 is a schematic view of a CO 2 recovery apparatus according to a second embodiment. Note that, configurations identical to the CO 2 recovery apparatus 10 A according to First embodiment illustrated in FIG. 1 are followed by the identical signs to omit overlapping descriptions.

As illustrated in FIG. 4 , in a CO 2 recovery apparatus 10 B of this embodiment, a thermometer 81 and a thermometer 82 are provided to the CO 2 -containing exhaust gas supply line L 11 and the purified exhaust gas exhaust line L 12 respectively to measure gas temperature.

Then, as a result of a measurement, a control apparatus, not illustrated, controls a gas temperature of the purified exhaust gas 11 B at the outlet of the water washing portion 13 B (T 2 ) so as to set the same lower than a gas temperature at the outlet of the cooling tower 70 (T 1 ) (T 1 >T 2 ).

As a result, lowering the gas temperature of the purified exhaust gas 11 B at the outlet of the CO 2 absorption tower 13 (T 2 ) makes it possible to increase the amount of condensed water, and consequently, amine concentration in liquid in the water washing portion 13 B is reduced, amine vapor pressure becomes lower, and the amount of accompanying CO 2 absorbing liquid (amine solution or the like) is reduced, thereby making it possible to reduce emissions thereof to the outside.

When the gas temperature of the purified exhaust gas 11 B (T 2 ) is lowered from 40° C. to 35° C. here, it is confirmed that amine compound concentration ratio in gas of the purified exhaust gas 11 B is decreased to 0.5 at 35° C. with respect to 1 at 40° C.

As described above, according to the present invention, concentration of amine compounds remaining in and being emitted from a decarbonated exhaust gas can be further reduced, and also a concentrated absorbing liquid can be effectively reused.

10 A, 10 B CO 2 RECOVERY APPARATUS

11 A CO 2 -CONTAINING EXHAUST GAS

12 CO 2 ABSORBING LIQUID

12 A RICH SOLUTION

12 B LEAN SOLUTION

13 CO 2 ABSORPTION TOWER (ABSORPTION TOWER)

14 ABSORBING LIQUID REGENERATION TOWER (REGENERATION TOWER)

20 WASHING LIQUID

21 EXTRACTED LIQUID

22 CONCENTRATION PORTION

23 CONCENTRATED LIQUID

24 GAS COMPONENT