CN114788992A - Carbon capture system and power plant boiler steam turbine system coupled with carbon capture system - Google Patents
Carbon capture system and power plant boiler steam turbine system coupled with carbon capture system Download PDFInfo
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- CN114788992A CN114788992A CN202210225630.3A CN202210225630A CN114788992A CN 114788992 A CN114788992 A CN 114788992A CN 202210225630 A CN202210225630 A CN 202210225630A CN 114788992 A CN114788992 A CN 114788992A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/343—Heat recovery
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
Abstract
The invention provides a carbon capture system and a power plant boiler steam turbine system coupled with the carbon capture system, wherein the carbon capture system comprises an absorption tower, a regeneration tower, a reboiler, a first heat exchanger, a second heat exchanger and a waste heat utilization heat exchanger, hot barren solution flowing out of the regeneration tower enters the hot side of the first heat exchanger, at least part of the hot barren solution after heat exchange enters the hot side of the second heat exchanger, at least part of rich solution flowing out of the absorption tower enters the cold side of the second heat exchanger to exchange heat with the hot barren solution and raise the temperature, then enters the cold side of the first heat exchanger to exchange heat with the hot barren solution and raise the temperature, and then enters the regeneration tower to carry out desorption; and part of the hot barren solution after heat exchange in the first heat exchanger can enter the hot side of the waste heat utilization heat exchanger, and the waste heat utilization heat exchanger is used for waste heat utilization of the part of the hot barren solution. The carbon capture system of the invention realizes the reduction of the heat consumption of the carbon capture system and the reduction of the cooling water consumption.
Description
Technical Field
The invention relates to the technical field of carbon capture, in particular to a carbon capture system and a power plant boiler steam turbine system coupled with the carbon capture system.
Background
China is the biggest global carbon emission subject at present, and the emission reduction pressure of the thermal power industry is higher under the background of 'carbon peak reaching and carbon neutralization' in China. While the energy structure mainly based on coal in China can be maintained for a long time, under the background, the carbon capture, utilization and sequestration technology is an important guarantee for the sustainable utilization of coal-based energy in the future, so that the research on the carbon capture technology of flue gases of advanced low-energy-consumption coal-fired power plants, steel plants, cement plants and the like is very important for realizing the aim of 'carbon neutralization' in the future.
At present, the carbon capture technology suitable for flue gas of coal-fired power plant smoke and the like mainly comprises a chemical absorption method, a chemical adsorption method, a physical adsorption method, a membrane separation method and the like, and the chemical absorption method is the mainstream technology of carbon capture of the coal-fired power plant at present. But because the operation energy consumption is too high, wherein the regeneration heat consumption of the absorbent accounts for about 70 percent of the energy consumption of the whole system, the commercial large-scale popularization and application of the process still have obvious limitation.
Disclosure of Invention
The present invention is based on the discovery and recognition by the inventors of the following facts and problems:
in the related art, desorption and regeneration of the rich solution require that the rich solution is raised to a certain temperature in a regeneration tower, a reboiler is generally adopted in the process, the rich solution is indirectly heated by using steam, and a large amount of heat energy is consumed in the process. The absorption and desorption system is a circulation process, the heated rich solution is desorbed and then becomes the hot barren solution, in order to ensure the absorption effect, the hot barren solution needs to be cooled to a certain temperature and then can enter the absorption tower to circularly absorb the flue gas, the cooling process generally adopts circulating cooling water for cooling, but not only can consume a large amount of water resources, but also can cause a large amount of heat loss due to poor economy in water-deficient areas.
The present invention is directed to solving, at least to some extent, one of the technical problems in the related art. Therefore, the embodiment of the invention provides a carbon capture system capable of recycling waste heat comprehensively, so that the heat consumption is reduced, and the cooling water consumption is reduced. Embodiments of the present invention also provide a power plant boiler steam turbine system coupled with a carbon capture system.
The carbon capture system comprises an absorption tower, a regeneration tower and a reboiler, wherein the barren solution enters the absorption tower and then is converted into rich solution after being captured by carbon, and the rich solution is heated by the reboiler in the regeneration tower and then is desorbed and converted into hot barren solution and regeneration gas; the absorption tower comprises a first heat exchanger and a second heat exchanger, wherein hot barren solution flowing out of the regeneration tower enters the hot side of the first heat exchanger, at least part of the hot barren solution after heat exchange enters the hot side of the second heat exchanger, at least part of rich solution flowing out of the absorption tower enters the cold side of the second heat exchanger to exchange heat with the hot barren solution and raise the temperature, then enters the cold side of the first heat exchanger to exchange heat with the hot barren solution and raise the temperature again, and then enters the regeneration tower to be desorbed; the waste heat utilization heat exchanger is used for utilizing waste heat of the part of the hot barren solution.
The carbon capture system in the embodiment of the invention solves the problems of high regeneration heat consumption and high water consumption of circulating cooling water of the carbon capture system in the related technology, fully recycles the heat by utilizing the multistage heat exchanger, and is combined with the cooling process of the circulating cooling water to realize the reduction of the heat consumption and the reduction of the cooling water consumption of the carbon capture system, thereby having important significance for the development of carbon capture, utilization and sealing technology industry and the realization of the aim of carbon neutralization in China.
Optionally, when waste heat utilization is not needed, the waste heat utilization heat exchanger is closed, and the hot lean solution after heat exchange in the first heat exchanger completely enters the second heat exchanger; when the waste heat is needed to be utilized, the waste heat utilization heat exchanger is opened, one part of the hot barren solution after heat exchange in the first heat exchanger enters the second heat exchanger, and the other part of the hot barren solution enters the waste heat utilization heat exchanger.
Optionally, the carbon capture system further comprises a regeneration gas-rich liquid heat exchanger, a part of the rich liquid flowing out of the absorption tower enters the cold side of the regeneration gas-rich liquid heat exchanger, the regeneration gas discharged from the regeneration tower enters the hot side of the regeneration gas-rich liquid heat exchanger to exchange heat with the rich liquid, and the heated rich liquid enters the regeneration tower.
Optionally, the carbon capture system further comprises a regeneration gas cooler and a gas-liquid separator, the regeneration gas discharged from the hot side of the regeneration gas-rich liquid heat exchanger is cooled by the regeneration gas cooler and enters the gas-liquid separator for gas-liquid separation, so as to separate the regeneration gas into carbon dioxide gas and condensed water, and the condensed water returns to the regeneration tower.
Optionally, the carbon capture system further comprises a lean liquid cooler into which the lean liquid is cooled before entering the absorption tower.
Optionally, the waste heat utilization heat exchanger is used for heating domestic water, or the waste heat utilization heat exchanger is used for heating boiler low-condensed water of a boiler steam turbine system of a power plant.
Optionally, the split ratio of the lean solution or the rich solution distributed into the first heat exchanger, the second heat exchanger and the waste heat utilization heat exchanger is adjustable.
Another aspect embodiment of the present invention provides a power plant boiler steam turbine system coupled with a carbon capture system, comprising: a carbon capture system according to any of the preceding claims; and the boiler steam turbine system comprises a steam turbine, a condenser and a low-pressure heater, wherein steam in the steam turbine is input into the condenser for condensation, condensed water enters the low-pressure heater for heating, the steam required by the reboiler is extracted from the steam turbine, and the condensed water flowing out of the reboiler enters the low-pressure heater.
In some embodiments, the waste heat utilization heat exchanger is used to heat condensate entering the low pressure heater exchanger.
In some embodiments, the condensed water flowing out of the condenser flows into the cold side of the waste heat utilization heat exchanger, is heated by the barren liquor at the hot side, and then enters the low-pressure heat exchanger.
Drawings
FIG. 1 is a schematic diagram of a carbon capture system provided by an embodiment of the invention.
FIG. 2 is a schematic diagram of a power plant boiler steam turbine system coupled to a carbon capture system provided by an embodiment of the present invention.
Reference numerals are as follows:
the system comprises an absorption tower 1, a regeneration tower 2, a reboiler 3, a first heat exchanger 4, a second heat exchanger 5, a waste heat utilization heat exchanger 6, a regenerated gas-rich liquid heat exchanger 7, a regenerated gas cooler 8, a gas-liquid separator 9, a lean liquid cooler 10, an induced draft fan 11, a boiler 12, a high pressure turbine 13, a medium pressure turbine 14, a low pressure turbine 15, a generator 16, a condenser 17, a low pressure heat exchanger 18, a deaerator 19 and a high pressure heat exchanger 20.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings. The embodiments described below with reference to the accompanying drawings are illustrative and intended to explain the present invention and should not be construed as limiting the present invention.
The basic structure of a carbon capture system provided by an embodiment of the present invention is described below with reference to fig. 1. The carbon capture system comprises an absorption tower 1, a regeneration tower 2, a reboiler 3, a first heat exchanger 4, a second heat exchanger 5 and a waste heat utilization heat exchanger 6.
The barren solution enters the absorption tower 1 to complete carbon capture and convert into rich solution, and the rich solution is heated by a reboiler 3 in the regeneration tower 2 and then desorbed to convert into hot barren solution and regeneration gas. The hot lean liquid flows out of the regeneration tower 2 into the hot side of the first heat exchanger 4. At least part of the heat-exchanged hot lean liquor enters the hot side of the second heat exchanger 5. At least part of the rich solution flowing out of the absorption tower 1 enters the cold side of the second heat exchanger 5 to exchange heat with the hot lean solution and raise the temperature, then enters the cold side of the first heat exchanger 4 to exchange heat with the hot lean solution and raise the temperature again, and then enters the regeneration tower 2 to desorb, part of the hot lean solution after heat exchange in the first heat exchanger 4 can enter the hot side of the waste heat utilization heat exchanger 6, and the waste heat utilization heat exchanger 6 is used for waste heat utilization of the part of the hot lean solution.
The hot lean solution flowing out of the regeneration tower 2 is subjected to heat exchange with the rich solution on the cold side in the first heat exchanger 4, and transfers heat to the rich solution on the cold side, so that the rich solution on the cold side is heated, and the temperature of the hot lean solution is reduced to some extent. The hot lean solution flowing out of the hot side of the first heat exchanger 4 can completely enter the second heat exchanger 4, or partially enter the second heat exchanger 4, and the other part enters the waste heat utilization heat exchanger 6. The hot lean solution entering the hot side of the second heat exchanger 4 exchanges heat with the rich solution at the cold side, and transfers heat to the rich solution at the cold side, so that the rich solution at the cold side is heated, and the temperature of the hot lean solution is further reduced. The hot barren solution entering the hot side of the waste heat utilization heat exchanger 6 exchanges heat with the heat exchange agent on the cold side, the hot barren solution transfers heat to the heat exchange agent on the cold side, the temperature of the heat exchange agent is increased, the temperature of the hot barren solution is reduced, and the heated heat exchange agent can be applied to other heat using terminals to realize waste heat utilization of the hot barren solution. The barren solution after heat recovery can be reduced to the required temperature by adopting a circulating cooling water process, and enters the absorption tower 1 for carbon capture.
The temperature of the rich solution flowing out of the absorption tower 1 is low, and after part or all of the rich solution enters the cold side of the second heat exchanger 5 to exchange heat with the hot lean solution and raise the temperature, the rich solution enters the cold side of the first heat exchanger 4 to exchange heat with the hot lean solution and raise the temperature again, and then the rich solution enters the regeneration tower 2 to be desorbed. In this process, the heat of the hot lean solution is sufficiently recovered and used, and the heat consumption required for the reboiler 3 to heat the rich solution is reduced.
The carbon capture system in the embodiment of the invention solves the problems of high regeneration heat consumption and high water consumption of circulating cooling water of the carbon capture system in the related technology, fully recycles the heat by utilizing the multistage heat exchanger, and is combined with the cooling process of the circulating cooling water to realize the reduction of the heat consumption and the reduction of the cooling water consumption of the carbon capture system, thereby having important significance for the development of carbon capture, utilization and sealing technology industry and the realization of the aim of carbon neutralization in China.
A carbon capture system in one embodiment of the invention is described below with reference to fig. 1.
The carbon capture system comprises an absorption tower 1, a regeneration tower 2, a reboiler 3, a first heat exchanger 4, a second heat exchanger 5, a waste heat utilization heat exchanger 6, a barren liquor cooler 10 and a regenerated gas treatment system. The relations among the absorption tower 1, the regeneration tower 2, the reboiler 3, the first heat exchanger 4, the second heat exchanger 5, and the waste heat utilization heat exchanger 6 are as described above, and are not described herein again.
As shown in fig. 1, the lean liquid enters the lean liquid cooler 10 for cooling before entering the absorption tower 1. Specifically, the lean solution flowing out of the second heat exchanger 5 and the lean solution flowing out of the waste heat utilization heat exchanger 6 are collected and then flow into the lean solution cooler 10 for cooling, and after being cooled to an appropriate temperature, the lean solution enters the absorption tower 1 and is sprayed downwards to be in reverse contact with the flue gas. Alternatively, the lean liquid cooler 10 cools the lean liquid by circulating cooling water. Since the lean liquid that enters the lean liquid cooler 10 has already undergone heat exchange in the first heat exchanger 4, the second heat exchanger 5, and the waste heat utilization heat exchanger 6, most of the heat has already been recovered, and therefore the amount of cooling water required in the lean liquid cooler 10 is greatly reduced.
It should be noted that the arrangement of the first heat exchanger 4, the second heat exchanger 5, and the waste heat utilization heat exchanger 6 can facilitate the adjustment of the lean solution split flow. The waste heat utilization heat exchanger 6 can be switched on and off, for example, as required for waste heat utilization. When waste heat utilization is not needed, the waste heat utilization heat exchanger 6 is closed, the hot barren solution after heat exchange in the first heat exchanger 4 completely enters the second heat exchanger 5, and the first heat exchanger 4 and the second heat exchanger 5 can be used as two-stage barren and rich solution heat exchangers; when the waste heat utilization is needed, the waste heat utilization heat exchanger 6 is opened, one part of the hot barren solution after heat exchange in the first heat exchanger 4 enters the second heat exchanger 4, the other part of the hot barren solution enters the waste heat utilization heat exchanger 6, and when the temperature of the rich solution is not influenced, one part of the hot barren solution is separated to be subjected to waste heat utilization, so that the waste of heat energy is avoided.
Optionally, the waste heat utilization heat exchanger 6 is used for heating domestic water, or the waste heat utilization heat exchanger 6 is used for heating boiler low condensed water of a boiler steam turbine system of a power plant, so that energy consumption for heating condensed water through steam turbine air extraction is reduced.
As shown in fig. 1, the desorbed regeneration gas escapes from the top of the regeneration tower 2 and enters a regeneration gas treatment system, and the regeneration gas treatment system is used for treating the regeneration gas and performing gas-liquid separation on carbon dioxide gas and condensed water in the regeneration gas. The regeneration gas temperature is higher, and the regeneration gas processing system need cool off it to certain temperature and can realize gas-liquid separation, and the regeneration gas processing system of this embodiment can carry out recycle to a large amount of latent heat of regeneration gas, helps the reduction of carbon capture system regeneration energy consumption, has reduced the cooling water consumption simultaneously.
Specifically, the regeneration gas treatment system includes a regeneration gas-rich liquid heat exchanger 7, a regeneration gas cooler 8, and a gas-liquid separator 9. And a part of the rich solution flowing out of the absorption tower 1 enters the cold side of the regenerated gas-rich solution heat exchanger 7, the regenerated gas discharged from the regeneration tower 2 enters the hot side of the regenerated gas-rich solution heat exchanger 7 to exchange heat with the rich solution, and the heated rich solution enters the regeneration tower 2. The regenerated gas discharged from the hot side of the regenerated gas-rich liquid heat exchanger 7 is cooled by a regenerated gas cooler 8, enters a gas-liquid separator 9 for gas-liquid separation, is separated into gaseous carbon dioxide gas and condensed water, the condensed water returns to the regeneration tower 2 from the upper part of the regeneration tower 2, and the gaseous carbon dioxide enters a subsequent compression drying process.
In the process, after the regenerated gas discharged from the regeneration tower 2 exchanges heat with part of the rich liquid entering the regeneration tower 2, the temperature of the rich liquid is increased, the self waste heat of the regenerated gas is fully utilized, and the heat consumption required by rich liquid desorption is reduced. In addition, as the regenerated gas and the rich solution exchange heat, the temperature of the regenerated gas and the rich solution is reduced, the consumption of the circulating cooling water of the regenerated gas cooler 8 is also reduced, and the circulating water consumption of the system is reduced.
Furthermore, the flow dividing ratio of the barren solution or the rich solution which is distributed to enter the first heat exchanger 4, the second heat exchanger 5, the waste heat utilization heat exchanger 6 and the regeneration gas-rich solution heat exchanger 7 is adjustable, namely the flow dividing ratio of the rich solution, the flow dividing ratio of the barren solution and the arrangement of each heat exchanger can flexibly adjust the flow dividing ratio and the temperature of each level of heat exchanger, and the flow dividing ratio and the temperature of each level of heat exchanger are optimally configured according to different waste heat utilization requirements of the power plant.
The specific operation principle of the carbon capture system provided in the present embodiment will be described below with reference to fig. 1.
The flue gas after pretreatment such as dust removal, desulfurization and primary cooling enters the absorption tower 1 through the induced draft fan 11, and contacts and reacts with lean solution sprayed from top to bottom, carbon dioxide in the flue gas is absorbed by the lean solution, and the flue gas without carbon dioxide is discharged from the top of the absorption tower 1.
The lean liquid is sprayed downwards from the upper part of the absorption tower 1, and becomes rich liquid after absorbing carbon dioxide, and the rich liquid is discharged from the lower part of the absorption tower 1 by a pump. The rich solution discharged from the absorption tower 1 is divided into two parts, one part of the rich solution enters the regeneration gas-rich solution heat exchanger 7 to exchange heat with the regeneration gas, part of heat in the regeneration gas is recovered, the temperature of the rich solution after heat recovery is increased and then enters the regeneration tower 2, the sensible heat required for further increasing the temperature of the rich solution to the desorption temperature is reduced, and therefore the regeneration heat consumption of the system is reduced. And the other part of the rich solution enters the second heat exchanger 5 to exchange heat with the lean solution, then enters the first heat exchanger 4 to exchange heat with all the lean solution again, and the heat of the hot lean solution flowing out of the regeneration tower 2 is recovered by using the low temperature of the rich solution in the first heat exchanger 4 and the second heat exchanger 5. The rich liquor flowing out of the regeneration gas-rich liquor heat exchanger 7 and the rich liquor flowing out of the first heat exchanger 4 are mixed and then enter from the upper part of the regeneration tower 2, or enter at certain intervals according to the tower height, the rich liquor after heat exchange with the regeneration gas is arranged above, and the rich liquor after heat exchange with the barren liquor is arranged below.
The rich solution enters a regeneration tower 2 and is heated by a reboiler 3 to be desorbed into a lean solution, and the lean solution needs to be cooled and then enters an absorption tower 1 for circulating absorption. As shown in figure 1, the lean solution is pumped out from the bottom of the regeneration tower 2, and after heat exchange with the rich solution is carried out through the first heat exchanger 4, the temperature is still high, and waste heat utilization can be carried out. The lean solution is divided into two parts, wherein one part of the lean solution enters a second heat exchanger 5 to exchange heat with the rich solution, and the other part of the lean solution enters a waste heat utilization heat exchanger 6 to utilize waste heat. The lean solution after the waste heat utilization and the lean solution after the heat exchange with the rich solution are mixed, cooled to a certain temperature by a lean solution cooler 10, and then enter from the upper part of the absorption tower 1 to circularly absorb the carbon dioxide.
The lean solution can be shunted by arranging the waste heat utilization heat exchanger 6, the heat of the lean solution can be fully recycled by shunting the lean solution, the circulating cooling water consumption of the lean solution cooler 10 is reduced, partial heat in the lean solution can be used for heating other heat consumption ends, and the waste of heat energy is avoided.
The regenerated gas after desorption escapes from the top of the regeneration tower 2, exchanges heat with the rich solution in the regenerated gas-rich solution heat exchanger 7, improves the temperature of the rich solution, fully utilizes the self waste heat, and reduces the heat consumption required by rich solution desorption. And the regenerated gas after heat exchange with the rich liquid enters a regenerated gas cooler 8, is cooled to a certain temperature and then enters a gas-liquid separator 9, after gas-liquid separation, gaseous carbon dioxide enters a subsequent compression drying process, and liquid condensate water enters the regeneration tower 2 again from the upper part of the regeneration tower 2. Because the regenerated gas and the rich solution exchange heat and part of heat is transferred to the rich solution, the consumption of the circulating cooling water of the regenerated gas cooler 8 is reduced, and the circulating water consumption of the system is reduced.
A schematic diagram of a power plant boiler-steam engine system coupled to a carbon capture system provided by an embodiment of the present invention is described below with respect to fig. 2.
As shown in fig. 2, the carbon capture system is the carbon capture system in the above embodiment. The power plant boiler turbine system coupled to the carbon capture system includes a boiler 12, a high pressure turbine 13, an intermediate pressure turbine 14, a low pressure turbine 15, a generator 16, a condenser 17, a low pressure heat exchanger 18, a deaerator 19, and a high pressure heat exchanger 20. As shown in fig. 2, a boiler 12, a high pressure turbine 13, an intermediate pressure turbine 14, a low pressure turbine 15, a condenser 17, a low pressure heat exchanger 18, a deaerator 19, and a high pressure heat exchanger 20 form a loop, and steam of the low pressure turbine 15 is used for driving a generator 16. Steam of the low-pressure turbine 15 enters a condenser 17 to be condensed, condensed water enters a low-pressure heat exchanger 18 to be heated, the condensed water is deaerated by a deaerator 19 and then enters a high-pressure heat exchanger 20 to be reheated, and the high-pressure heat exchanger 20 is used for supplying water to the boiler 12.
The steam of the reboiler 3 in the carbon capture system comes from the extraction steam of the medium pressure turbine 14, the steam is heated in the reboiler 3 to desorb the rich solution and then is condensed, and the condensate liquid flows back to the inlet of the low pressure heater 18.
The temperature of the condensed water in the condenser 17 is mostly 30-40 ℃, and the temperature of the barren solution entering the waste heat utilization heat exchanger 6 is about 80-90 ℃ in the waste heat utilization process, so that the condensed water entering the low-pressure heat exchanger 18 can be effectively heated by the waste heat utilization heat exchanger 6, and the heating consumption of the low-pressure heat exchanger 18 is reduced. Specifically, as shown in fig. 2, the condensed water flowing out of the condenser 17 flows into the cold side of the waste heat utilization heat exchanger 6, is heated by the lean solution at the hot side, and then flows back into the low heat exchanger 18.
Since the heating steam of the reboiler 3 comes from the extraction steam of the medium pressure turbine 14 and the heating steam of the low pressure heat exchanger 18 also comes from the extraction steam of the turbine, the consumption of the heating steam of the low pressure heat exchanger 18 can be reduced by heating the low pressure condensed water by using the waste heat of the barren liquor, and a part of heat can be considered to be also supplied to the turbine by the barren liquor, so that the regeneration heat consumption of the carbon capture system is reduced as a whole.
Through simulation test research, the coupling processes of barren liquor diversion recovery barren liquor waste heat, rich liquor diversion recovery regeneration gas waste heat and the like can reduce the regeneration heat consumption of the carbon capture system by 20-30% and the circulating water consumption by 5-10%.
In the description of the present invention, it is to be understood that the terms "central," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," "circumferential," and the like are used in the orientations and positional relationships indicated in the drawings for convenience in describing the invention and to simplify the description, and are not intended to indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and are therefore not to be considered limiting of the invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or to implicitly indicate the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless explicitly specified otherwise.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally formed; may be mechanically coupled, may be electrically coupled or may be in communication with each other; they may be directly connected or indirectly connected through intervening media, or they may be interconnected within two elements or in a relationship where two elements interact with each other unless otherwise specifically limited. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
In the present invention, unless otherwise expressly stated or limited, the first feature "on" or "under" the second feature may be directly contacting the first and second features or indirectly contacting the first and second features through an intermediate. Also, a first feature "on," "above," and "over" a second feature may be directly on or obliquely above the second feature, or simply mean that the first feature is at a higher level than the second feature. A first feature "under," "beneath," and "under" a second feature may be directly under or obliquely under the second feature, or may simply mean that the first feature is at a lesser elevation than the second feature.
In the present disclosure, the terms "one embodiment," "some embodiments," "an example," "a specific example," or "some examples" and the like mean that a specific feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present disclosure. In this specification, the schematic representations of the terms used above are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.
Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art within the scope of the present invention.
Claims (10)
1. A carbon capture system, comprising:
the absorption tower, the regeneration tower and the reboiler, the barren liquor finishes carbon capture and is converted into rich liquor after entering the absorption tower, and the rich liquor is heated by the reboiler in the regeneration tower and then is desorbed and is converted into hot barren liquor and regeneration gas;
the absorption tower comprises a first heat exchanger and a second heat exchanger, wherein hot barren solution flowing out of the regeneration tower enters the hot side of the first heat exchanger, at least part of the hot barren solution after heat exchange enters the hot side of the second heat exchanger, at least part of rich solution flowing out of the absorption tower enters the cold side of the second heat exchanger to exchange heat with the hot barren solution and raise the temperature, then enters the cold side of the first heat exchanger to exchange heat with the hot barren solution and raise the temperature again, and then enters the regeneration tower to be desorbed;
the waste heat utilization heat exchanger is used for utilizing waste heat of the part of the hot barren solution.
2. The carbon capture system of claim 1,
when waste heat utilization is not needed, the waste heat utilization heat exchanger is closed, and the hot barren solution after heat exchange in the first heat exchanger completely enters the second heat exchanger;
when the waste heat is needed to be utilized, the waste heat utilization heat exchanger is opened, one part of the hot barren solution after heat exchange in the first heat exchanger enters the second heat exchanger, and the other part of the hot barren solution enters the waste heat utilization heat exchanger.
3. The carbon capture system of claim 1, further comprising a regeneration gas-rich liquid heat exchanger, wherein a part of the rich liquid flowing out of the absorption tower enters a cold side of the regeneration gas-rich liquid heat exchanger, the regeneration gas discharged from the regeneration tower enters a hot side of the regeneration gas-rich liquid heat exchanger to exchange heat with the rich liquid, and the heated rich liquid enters the regeneration tower.
4. The carbon capture system of claim 3, further comprising a regeneration gas cooler and a gas-liquid separator, wherein the regeneration gas discharged from the hot side of the regeneration gas-rich liquid heat exchanger is cooled by the regeneration gas cooler and enters the gas-liquid separator for gas-liquid separation into carbon dioxide gas and condensed water, and the condensed water returns to the regeneration tower.
5. The carbon capture system of claim 1, further comprising a lean liquid cooler into which lean liquid is cooled prior to entering the absorption tower.
6. The carbon capture system of any one of claims 1-5, wherein the waste heat recovery heat exchanger is configured to heat domestic water or the boiler low-plus-condensate water of a power plant boiler steam turbine system.
7. The carbon capture system of any of claims 1-5, wherein a split ratio of the lean or rich liquid distributed into the first heat exchanger, the second heat exchanger, and the waste heat utilization heat exchanger is adjustable.
8. A power plant boiler steam turbine system coupled with a carbon capture system, comprising:
a carbon capture system according to any one of claims 1-7;
the boiler-steam engine system comprises a steam turbine, a condenser and a low pressure heater, wherein steam in the steam turbine is input into the condenser for condensation, condensed water enters the low pressure heater for heating, steam required by the reboiler is extracted from the steam turbine, and the condensed water flowing out of the reboiler enters the low pressure heater.
9. The power plant boiler steam turbine system coupled with the carbon capture system of claim 8, wherein the waste heat utilization heat exchanger is configured to heat condensate entering a low-plus heat exchanger.
10. A power plant boiler steam turbine system coupled to a carbon capture system in accordance with claim 9, wherein the condensed water from the condenser flows into the cold side of the waste heat utilization heat exchanger, is heated by the lean solution at the hot side, and then flows back into the low-pressure heat exchanger.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202210225630.3A CN114788992A (en) | 2022-03-09 | 2022-03-09 | Carbon capture system and power plant boiler steam turbine system coupled with carbon capture system |
Applications Claiming Priority (1)
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