CN117815843A - Carbon capture system and control method thereof - Google Patents
Carbon capture system and control method thereof Download PDFInfo
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- CN117815843A CN117815843A CN202311597150.0A CN202311597150A CN117815843A CN 117815843 A CN117815843 A CN 117815843A CN 202311597150 A CN202311597150 A CN 202311597150A CN 117815843 A CN117815843 A CN 117815843A
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 53
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 53
- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000007788 liquid Substances 0.000 claims abstract description 92
- 238000010521 absorption reaction Methods 0.000 claims abstract description 55
- 238000003795 desorption Methods 0.000 claims abstract description 55
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 54
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 27
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 27
- 239000003546 flue gas Substances 0.000 claims description 25
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 24
- 238000010438 heat treatment Methods 0.000 claims description 6
- 238000004064 recycling Methods 0.000 claims description 6
- 239000003507 refrigerant Substances 0.000 claims description 6
- 239000006096 absorbing agent Substances 0.000 claims description 4
- 239000002918 waste heat Substances 0.000 abstract description 7
- 230000008569 process Effects 0.000 description 7
- 230000009467 reduction Effects 0.000 description 6
- 230000009471 action Effects 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 238000011084 recovery Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Abstract
The invention relates to a carbon capture system and a control method thereof, wherein the system comprises a carbon capture device and a first circulating unit, the carbon capture device comprises an absorption tower, a rich liquid pump and a desorption tower which are sequentially connected, and a first conveying pipeline and a second conveying pipeline are arranged on the desorption tower; the first circulation unit comprises a first condenser, a first compressor, a first expansion device and a rich liquid heater, wherein the rich liquid heater is respectively connected with the absorption tower and the desorption tower, the first condenser is connected with a first conveying pipeline, an inlet of the first compressor is connected with a cold end outlet of the first condenser, an outlet of the first compressor is connected with a hot end inlet of the rich liquid heater, an inlet of the first expansion device is connected with a hot end outlet of the rich liquid heater, and an outlet of the first expansion device is connected with a cold end inlet of the first condenser. The method and the device can enable the low-grade waste heat of the first condenser after heat exchange with the carbon dioxide to be reused, reduce resource consumption and improve the economy of the carbon capture system.
Description
Technical Field
The present disclosure relates to the field of carbon capture technology, and in particular, to a carbon capture system and a control method thereof.
Background
The carbon trapping system is mainly used for carrying out pretreatment such as denitration, dust removal, desulfurization and the like on the exhaust gas of the power plant boiler, removing substances harmful to the subsequent process in the exhaust gas, and then reacting the reaction liquid in the absorption tower with carbon dioxide in the exhaust gas to separate the carbon dioxide from the exhaust gas; then decomposing the product in a desorption tower under certain conditions, thereby releasing carbon dioxide, and compressing, purifying and liquefying the carbon dioxide to obtain a high-purity liquid carbon dioxide product.
The existing carbon capture system has the problems of overlarge energy consumption, insufficient utilization of low-grade waste heat and the like, so that the economy of the carbon capture system is too low.
Disclosure of Invention
The invention aims to provide a carbon capture system and a control method thereof, wherein the system can reasonably utilize low-grade waste heat generated in a carbon capture process, and the economy of the carbon capture system is improved.
To achieve the above object, a first aspect of the present disclosure provides a carbon capture system including: the carbon trapping device comprises an absorption tower, a rich liquid pump and a desorption tower which are connected in sequence; the rich liquid pump is used for inputting the rich liquid generated by the absorption tower into the desorption tower to decompose the rich liquid into carbon dioxide and lean liquid, and a first conveying pipeline for recycling the carbon dioxide and a second conveying pipeline for conveying at least part of the lean liquid back into the absorption tower are arranged on the desorption tower; a first circulation unit including a first condenser, a first compressor, a first expansion device, and a rich liquid heater connected between the absorption tower and the desorption tower; the cold end inlet of the rich liquid heater is connected with the absorption tower, and the cold end outlet of the rich liquid heater is connected with the desorption tower; the first condenser is connected to the first conveying pipeline, an inlet of the first compressor is connected to a cold end outlet of the first condenser, an outlet of the first compressor is connected to a hot end inlet of the rich liquid heater, an inlet of the first expansion device is connected to a hot end outlet of the rich liquid heater, and an outlet of the first expansion device is connected to a cold end inlet of the first condenser.
Optionally, the carbon capture system further comprises a second circulation unit comprising a second compressor, a second condenser, a second expansion device, and a lean liquor cooler connected to the second transfer line; the hot end inlet of the lean solution cooler is connected with the desorption tower, the hot end outlet of the lean solution cooler is connected with the absorption tower, the inlet of the second compressor is connected with the cold end outlet of the lean solution cooler, the outlet of the second compressor is connected with the hot end inlet of the second condenser, the inlet of the second expansion device is connected with the hot end outlet of the second condenser, and the outlet of the second expansion device is connected with the cold end inlet of the lean solution cooler.
Optionally, the carbon capture system further comprises a reboiler for heating at least part of the lean liquid returned into the desorption tower, a hot end outlet of the reboiler is connected to a cold end inlet of the second condenser, and a cold end outlet of the second condenser is connected to a hot end inlet of the reboiler.
Optionally, the carbon capture system further comprises an ejector for inputting steam into the reboiler, and the cold end outlet of the second condenser is connected to the hot end inlet of the reboiler through the ejector.
Optionally, the absorption tower is connected with the desorption tower through a first branch and a second branch, and the rich liquid heater is connected with the first branch and/or the second branch.
Optionally, the split ratio of the first leg and the second leg is one of 1:9, 2:8, or 3:7.
Optionally, the number of trays of the absorption tower is configured to be 15-40, and the number of trays of the desorption tower is configured to be 20-50.
Optionally, the first expansion device and the second expansion device are configured as an expander or a throttle valve.
Optionally, the carbon capture system further comprises an induced draft fan and a flue gas cooler connected with the induced draft fan, wherein the flue gas cooler is connected with the absorption tower.
In a second aspect of the present disclosure, there is provided a control method of a carbon capture system, the method being based on the above carbon capture system, comprising: starting the carbon capture device: starting an absorption tower, a rich liquid pump and a desorption tower; after the lean liquid in the desorption tower and the absorption tower stably runs, introducing flue gas into the absorption tower; starting a first circulation unit: the refrigerant in the first condenser exchanges heat with carbon dioxide, is compressed by the first compressor, enters the rich liquid heater to exchange heat with lean liquid in the rich liquid heater, and enters the first condenser again through the first expansion device after exchanging heat.
Through the technical scheme, the carbon capture system disclosed by the invention has the advantages that the first circulating unit is arranged, so that the refrigerant in the first condenser enters the rich liquid heater to heat the rich liquid through the first compressor after exchanging heat with carbon dioxide, and reenters the first condenser after heating the rich liquid, thereby enabling the low-grade residual heat of the first condenser after exchanging heat with carbon dioxide to be reused, reducing the consumption of resources and improving the economy of the carbon capture system.
Additional features and advantages of the present disclosure will be set forth in the detailed description which follows.
Drawings
The accompanying drawings are included to provide a further understanding of the disclosure, and are incorporated in and constitute a part of this specification, illustrate the disclosure and together with the description serve to explain, but do not limit the disclosure. In the drawings:
FIG. 1 is a schematic diagram of a carbon capture system provided by an embodiment of the present disclosure.
Description of the reference numerals
1-an absorption tower; 2-a rich liquid pump; 3-a desorption tower; 4-a first delivery line; 5-a second delivery line; 6-a first condenser; 7-a first compressor; 8-a first expansion device; 9-a rich liquid heater; 10-a second compressor; 11-a second condenser; 12-a second expansion device; 13-lean liquor cooler; 14-reboiler; 15-an ejector; 16-a first branch; 17-a second leg; 18-induced draft fan; 19-flue gas cooler.
Detailed Description
Specific embodiments of the present disclosure are described in detail below with reference to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating and illustrating the disclosure, are not intended to limit the disclosure.
In this disclosure, unless otherwise indicated, terms of orientation such as "inner and outer" are used to refer to "inner and outer" with respect to the contour of the corresponding component itself. In addition, the terms "first," "second," and the like, as used in this disclosure, are used to distinguish one element from another element without sequence or importance. Furthermore, in the following description, when referring to the drawings, the same reference numerals in different drawings denote the same or similar elements unless otherwise explained. The foregoing definitions are provided for the purpose of illustrating and explaining the present disclosure and should not be construed as limiting the present disclosure.
In a first aspect of the present disclosure, as shown in fig. 1, there is provided a carbon capturing system including a carbon capturing device and a first circulation unit, wherein the carbon capturing device includes an absorption tower 1, a rich liquid pump 2, and a desorption tower 3 connected in this order; the rich liquid pump 2 is used for inputting the rich liquid generated by the absorption tower 1 into the desorption tower 3 to decompose the rich liquid into carbon dioxide and lean liquid, and a first conveying pipeline 4 for recycling the carbon dioxide and a second conveying pipeline 5 for conveying at least part of the lean liquid back into the absorption tower 1 are arranged on the desorption tower 3; the first circulation unit comprises a first condenser 6, a first compressor 7, a first expansion device 8 and a rich liquid heater 9, wherein the rich liquid heater 9 is connected between the absorption tower 1 and the desorption tower 3, the cold end inlet of the rich liquid heater 9 is connected with the absorption tower 1, the cold end outlet of the rich liquid heater 9 is connected with the desorption tower 3, the first condenser 6 is connected with the first conveying pipeline 4, the inlet of the first compressor 7 is connected with the cold end outlet of the first condenser 6, the outlet of the first compressor 7 is connected with the hot end inlet of the rich liquid heater 9, the inlet of the first expansion device 8 is connected with the hot end outlet of the rich liquid heater 9, and the outlet of the first expansion device 8 is connected with the cold end inlet of the first condenser 6. After the desulfurized flue gas enters the absorption tower 1, the flue gas reacts with lean liquid in the absorption tower 1, the purified flue gas is directly discharged from the top end of the absorption tower 1, the lean liquid separates and absorbs carbon dioxide in the flue gas from the flue gas to form rich liquid, rich liquid is discharged from the bottom end of the absorption tower 1 and enters the desorption tower 3 under the action of the rich liquid pump 2, the rich liquid is heated by the rich liquid heater 9 in the process that the rich liquid enters the desorption tower 3 from the absorption tower 1, so that the rich liquid is subjected to subsequent desorption operation, the desorption tower 3 is subjected to the re-decomposition of the rich liquid into carbon dioxide and lean liquid, part of lean liquid generated by the desorption flows back to the absorption tower 1 through the second conveying pipeline 5 for recycling, the carbon dioxide generated by the desorption is discharged from the first conveying pipeline 4 at the top of the desorption tower 3 and is cooled under the action of the first condenser 6, so that the subsequent recovery operation is facilitated, the refrigerant in the first condenser 6 is heated and pressurized by the first compressor 7 and enters the rich liquid heater 9 after the rich liquid is subjected to the heat exchange with the carbon dioxide, the rich liquid is subjected to the heat exchange with the first condenser 6, the heat energy can be recovered in the first heat exchanger and the heat exchanger is recycled, the heat energy can be reduced, the heat energy can be recovered in the first heat exchanger is reduced, the heat exchanger is saved, the heat energy can be recovered by the heat recovery system is reduced, and the heat energy can be recovered by the heat recovery device is reduced, and the heat energy is recovered by the heat is reduced, and the heat is recycled by the heat is used.
In some embodiments of the present disclosure, in order to be able to utilize the residual heat of the lean liquid separated from the desorber 3, the carbon capture system further comprises a second circulation unit comprising a second compressor 10, a second condenser 11, a second expansion device 12, and a lean liquid cooler 13 connected to the second transfer line 5; the hot end inlet of the lean solution cooler 13 is connected to the desorption tower 3, the hot end outlet of the lean solution cooler 13 is connected to the absorption tower 1, the inlet of the second compressor 10 is connected to the cold end outlet of the lean solution cooler 13, the outlet of the second compressor 10 is connected to the hot end inlet of the second condenser 11, the inlet of the second expansion device 12 is connected to the hot end outlet of the second condenser 11, and the outlet of the second expansion device 12 is connected to the cold end inlet of the lean solution cooler 13. In the process of flowing in the lean solution from the hot end inlet to the hot end outlet of the lean solution cooler 13, the rest heat of the lean solution exchanges heat with a first heat exchange medium entering from the cold end inlet of the lean solution cooler 13, the first heat exchange medium is heated and pressurized by the second compressor 10 to enter the second condenser 11, and exchanges heat with a second heat exchange medium passing through the second condenser 11 to raise the temperature of the second heat exchange medium, and then the first heat exchange medium flows back into the lean solution cooler 13 again after being subjected to temperature and pressure reduction by the second expansion device 12 to exchange heat with the lean solution. The temperature of the lean solution can be reduced on the one hand, so that the lean solution accords with the temperature in the reflux absorption tower 1, on the other hand, the waste heat of the lean solution can be transmitted to the second heat exchange medium through the second circulating unit, the energy source required for heating the second heat exchange medium is saved, and the economy of the carbon capture system is further improved.
Wherein the first heat exchange medium may be low temperature low pressure steam or the like, the second heat exchange medium may be condensed water or the like, and the first expansion device 8 and the second expansion device 12 may be configured as an expander or a throttle valve.
In some embodiments, the carbon capture system further comprises a reboiler 14 for heating at least part of the lean liquid returned into the desorber 3, the warm end outlet of the reboiler 14 being connected to the cold end inlet of the second condenser 11, the cold end outlet of the second condenser 11 being connected to the warm end inlet of the reboiler 14. The hot steam generated after the lean solution exchanges heat with the reboiler 14 heats the rich solution, so that desorption of carbon dioxide is accelerated, the steam in the reboiler 14 is condensed into condensed water, the hot steam regenerated after the condensed water exchanges heat with the second condenser 11 returns to the reboiler 14 for recycling, and the recycled hot steam is mixed with new hot steam from the outside and then heats the rich solution, so that part of the hot steam introduced from the outside can be reduced, and consumption of resources is reduced.
To reduce the pressure of the steam entering the reboiler 14 and to ensure safety and stability of the overall carbon capture system, the carbon capture system further comprises an ejector 15 for feeding steam into the reboiler 14, the cold end outlet of the second condenser 11 being connected to the hot end inlet of the reboiler 14 by the ejector 15.
In some embodiments of the present disclosure, the absorption column 1 and the desorption column 3 are connected by a first branch 16 and a second branch 17, and the rich liquid heater 9 is connected to the first branch 16 and/or the second branch 17. The pipeline of the absorption tower 1 entering the desorption tower 3 is divided into two, so that the rich liquid is split into the desorption tower 3, the work load of the desorption tower 3 can be reduced to a certain extent, the temperature and the pressure in the desorption tower 3 are ensured, and the desorption efficiency is ensured. The split ratio of the first branch 16 to the second branch 17 may be one of 1:9, 2:8 or 3:7, and since the flow of the first branch 16 is smaller and the flow of the second branch 17 is larger, the rich liquid heater 9 may be disposed on the second branch 17 to ensure the subsequent desorption effect.
In some embodiments, the number of trays of absorber 1 is configured to be 15-40 and the number of trays of desorber 3 is configured to be 20-50. A sufficient number of trays may allow sufficient contact and reaction of the gas or liquid located therein to enhance the effectiveness of absorption and desorption.
In addition, in order to ensure that the desulfurization flue gas can smoothly enter the absorption tower 1, the carbon capture system of the present disclosure further comprises an induced draft fan 18 and a flue gas cooler 19 connected with the induced draft fan 18, wherein the flue gas cooler 19 is connected with the absorption tower 1. After the induced draft fan 18 introduces the flue gas, the flue gas is cooled by the flue gas cooler 19 to ensure that the temperature of the flue gas meets the requirement of entering the absorption tower 1, thereby ensuring the normal operation of the absorption tower 1.
In a second aspect of the present disclosure, there is provided a control method of a carbon capture system, the method being based on the above carbon capture system, comprising:
starting the carbon capture device: starting the absorption tower 1, the rich liquid pump 2 and the desorption tower 3, wherein lean liquid in the absorption tower 1 can circularly flow between the absorption tower 1 and the desorption tower 3; after the lean liquid in the desorption tower 3 and the absorption tower 1 stably runs, flue gas is introduced into the absorption tower 1, and after entering the absorption tower 1, the flue gas reacts with the lean liquid in the absorption tower 1 to produce rich liquid, and the rich liquid enters the desorption tower 3 under the action of the rich liquid pump 2 to be decomposed into carbon dioxide and the lean liquid.
Starting a first circulation unit: the refrigerant in the first condenser 6 exchanges heat with carbon dioxide, is compressed by the first compressor 7, enters the rich liquid heater 9 to exchange heat with lean liquid in the rich liquid heater 9, and enters the first condenser 6 again for circulation after exchanging heat by the first expansion device 8.
Starting a second circulation unit: the lean solution cooler 13 transfers the waste heat of the lean solution passing through the lean solution cooler to the first heat exchange medium, the first heat exchange medium is heated and pressurized by the second compressor 10 to enter the second condenser 11, and exchanges heat with the second heat exchange medium passing through the second condenser 11 to raise the temperature of the second heat exchange medium, and then the first heat exchange medium is subjected to temperature and pressure reduction by the second expansion device 12 and then flows back to the lean solution cooler 13 again for cyclic heating.
In summary, the working principle of the present disclosure is: the induced draft fan 18 firstly conveys the desulfurized flue gas into the flue gas cooler 19 for cooling, then the cooled desulfurized flue gas enters the absorption tower 1 and reacts with lean liquor in the absorption tower 1 to generate rich liquor, the rich liquor is shunted into the desorption tower 3 through the first branch 16 and the second branch 17 under the action of the rich liquor pump 2 to be decomposed into carbon dioxide and lean liquor, the rich liquor heater 9 heats the rich liquor of the first branch 16 and/or the second branch 17 in the process that the rich liquor flows into the desorption tower 3 so as to facilitate the subsequent desorption operation, carbon dioxide after the rich liquor decomposition is discharged from the first conveying pipeline 4 at the top of the desorption tower 3 and is cooled under the action of the first condenser 6 so as to facilitate the subsequent recovery operation, and the refrigerant in the first condenser 6 is heated and pressurized by the first compressor 7 after heat exchange with the carbon dioxide and then enters the rich liquor heater 9 to heat the rich liquor, and is subjected to temperature reduction and pressure reduction by the first expansion device 8 after heat exchange with the rich liquor, and finally returns to the first condenser 6; part of lean solution decomposed by the rich solution flows back to the absorption tower 1 through the lean solution cooler 13 to react with new flue gas, in the process that the part of lean solution passes through the lean solution cooler 13, waste heat of the lean solution is transferred to a first heat exchange medium, the first heat exchange medium is heated and pressurized by the second compressor 10 to enter the second condenser 11, and heat exchange is carried out on the first heat exchange medium and the second heat exchange medium passing through the second condenser 11 so as to raise the temperature of the second heat exchange medium, and then the first heat exchange medium flows back to the lean solution cooler 13 again after being subjected to temperature reduction and pressure reduction through the second expansion device 12 to carry out heat exchange; the other part of lean solution decomposed from the rich solution can generate hot steam to heat the rich solution after exchanging heat with the reboiler 14 so as to accelerate desorption of carbon dioxide, the steam in the reboiler 14 can be condensed into condensed water (namely a second heat exchange medium), the hot steam regenerated after exchanging heat with the second condenser 11 can be returned to the reboiler 14 for recycling, and the recycled hot steam can be mixed with new hot steam from the outside to heat the rich solution, so that part of hot steam led from the outside can be reduced, and consumption of resources is reduced. Based on the method, the low-grade waste heat in the carbon capturing process can be reasonably utilized, so that the consumption of resources is reduced, and the economy of a carbon capturing system is improved.
The preferred embodiments of the present disclosure have been described in detail above with reference to the accompanying drawings, but the present disclosure is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solutions of the present disclosure within the scope of the technical concept of the present disclosure, and all the simple modifications belong to the protection scope of the present disclosure.
In addition, the specific features described in the foregoing embodiments may be combined in any suitable manner, and in order to avoid unnecessary repetition, the present disclosure does not further describe various possible combinations.
Moreover, any combination between the various embodiments of the present disclosure is possible as long as it does not depart from the spirit of the present disclosure, which should also be construed as the disclosure of the present disclosure.
Claims (10)
1. A carbon capture system, comprising:
the carbon trapping device comprises an absorption tower, a rich liquid pump and a desorption tower which are connected in sequence; the rich liquid pump is used for inputting the rich liquid generated by the absorption tower into the desorption tower to decompose the rich liquid into carbon dioxide and lean liquid, and a first conveying pipeline for recycling the carbon dioxide and a second conveying pipeline for conveying at least part of the lean liquid back into the absorption tower are arranged on the desorption tower;
a first circulation unit including a first condenser, a first compressor, a first expansion device, and a rich liquid heater connected between the absorption tower and the desorption tower;
the cold end inlet of the rich liquid heater is connected with the absorption tower, and the cold end outlet of the rich liquid heater is connected with the desorption tower; the first condenser is connected to the first conveying pipeline, an inlet of the first compressor is connected to a cold end outlet of the first condenser, an outlet of the first compressor is connected to a hot end inlet of the rich liquid heater, an inlet of the first expansion device is connected to a hot end outlet of the rich liquid heater, and an outlet of the first expansion device is connected to a cold end inlet of the first condenser.
2. The carbon capture system of claim 1, further comprising a second circulation unit comprising a second compressor, a second condenser, a second expansion device, and a lean liquor cooler connected to the second transfer line;
the hot end inlet of the lean solution cooler is connected with the desorption tower, the hot end outlet of the lean solution cooler is connected with the absorption tower, the inlet of the second compressor is connected with the cold end outlet of the lean solution cooler, the outlet of the second compressor is connected with the hot end inlet of the second condenser, the inlet of the second expansion device is connected with the hot end outlet of the second condenser, and the outlet of the second expansion device is connected with the cold end inlet of the lean solution cooler.
3. The carbon capture system of claim 2, further comprising a reboiler for heating at least a portion of the lean liquid back into the desorber, a hot side outlet of the reboiler being connected to a cold side inlet of the second condenser, a cold side outlet of the second condenser being connected to a hot side inlet of the reboiler.
4. A carbon capture system according to claim 3, further comprising an ejector for inputting steam into the reboiler, the cold end outlet of the second condenser being connected to the hot end inlet of the reboiler by the ejector.
5. The carbon capture system of claim 1, wherein the absorber column and the desorber column are connected by a first leg and a second leg, and the rich liquid heater is connected to the first leg and/or the second leg.
6. The carbon capture system of claim 5, wherein a split ratio of the first leg and the second leg is one of 1:9, 2:8, or 3:7.
7. The carbon capture system of claim 1, wherein the number of trays of the absorber is configured to be 15-40 and the number of trays of the desorber is configured to be 20-50.
8. The carbon capture system of claim 2, wherein the first expansion device and the second expansion device are configured as an expander or a throttle valve.
9. The carbon capture system of claim 1, further comprising an induced draft fan and a flue gas cooler coupled to the induced draft fan, the flue gas cooler coupled to the absorber tower.
10. A control method of a carbon trapping system, characterized in that the control method of a carbon trapping system according to any one of claims 1 to 9 comprises:
starting the carbon capture device:
starting an absorption tower, a rich liquid pump and a desorption tower;
after the lean liquid in the desorption tower and the absorption tower stably runs, introducing flue gas into the absorption tower;
starting a first circulation unit:
the refrigerant in the first condenser exchanges heat with carbon dioxide, is compressed by the first compressor, enters the rich liquid heater to exchange heat with lean liquid in the rich liquid heater, and reenters the first condenser for circulation after exchanging heat by the first expansion device.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202311597150.0A CN117815843A (en) | 2023-11-27 | 2023-11-27 | Carbon capture system and control method thereof |
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| CN202311597150.0A CN117815843A (en) | 2023-11-27 | 2023-11-27 | Carbon capture system and control method thereof |
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