CN219511357U - Waste heat cascade recovery system for flue gas carbon capture regeneration system - Google Patents
Waste heat cascade recovery system for flue gas carbon capture regeneration system Download PDFInfo
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- CN219511357U CN219511357U CN202320191024.4U CN202320191024U CN219511357U CN 219511357 U CN219511357 U CN 219511357U CN 202320191024 U CN202320191024 U CN 202320191024U CN 219511357 U CN219511357 U CN 219511357U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
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- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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Abstract
The utility model designs a waste heat cascade recovery system for a flue gas carbon capture regeneration system; the device comprises a rich liquid pump, a regeneration tower, a lean and rich liquid heat exchanger, a regenerated gas-rich liquid heat exchanger, a flash evaporation steam-rich liquid heat exchanger, a reboiler pump, a reboiler, a lean liquid lift pump, a flash evaporation tank, a flash evaporation steam compressor, a main lean liquid pump, a lean liquid cooler, a regenerated gas first separator, a regenerated gas cooler and a regenerated gas second separator; the regeneration tower is internally provided with a demister, a final-stage spray cooling device, a primary spray cooling device, a liquid collecting redistributor and a filler section. The utility model solves the problems of overhigh cooling load of regenerated gas, insignificant consumption reduction of lean solution flash evaporation, overlow temperature of rich solution entering a regeneration tower and the like in the existing carbon dioxide trapping system, thereby reducing the total energy consumption and the total circulating water consumption of the carbon trapping system.
Description
Technical Field
The utility model relates to the technical field of carbon dioxide trapping, in particular to a waste heat cascade recovery system for a flue gas carbon trapping and regenerating system.
Background
The flue gas carbon dioxide trapping technology is a large-scale greenhouse gas emission reduction technology, and is one of key technologies for realizing carbon neutralization targets in China. The energy of the carbon capture system mainly comes from exogenous steam, and the core equipment of the carbon capture system is an absorption tower and a regeneration tower. The operation temperature of the absorption tower is usually 40-60 ℃, the operation temperature of the regeneration tower is usually 100-120 ℃, and the operation temperature difference of the two towers leads to the requirement that the organic amine absorption liquid which circularly works between the two towers needs to be frequently heated and cooled through heat exchange so as to meet the process requirement. Most of waste heat in the traditional technology is taken away by cooling water at present, so that heat waste which cannot be ignored is caused. For example, the temperature of the regenerated gas at the outlet of the top of the regeneration tower can reach approximately 100 ℃, and a large amount of steam and mist drops are carried, so that a large load is brought to the subsequent regenerated gas cooling and gas-liquid separation unit. In the traditional process, only cooling water is adopted to cool the regenerated gas, so that a large amount of heat cannot be recycled.
In addition, the lean liquid flash evaporation processes disclosed in the patents CN201310599678.1, CN201711181818.8, CN 2015110207. X and the like can recover heat in the hot lean liquid to generate secondary steam to replace reboiling steam through a mechanical vapor recompression technology, so that the load of a reboiler is reduced, and meanwhile, the load of a lean liquid cooler is also reduced. However, excessive temperature of the secondary steam leads to an increase in the degradation rate of the organic amine absorbent, so that the temperature of the secondary steam is generally not higher than the desorption temperature (120 ℃) and the pressure before entering the tower is not lower than the pressure of the regeneration tower. The pressure drop of the flash tank is usually lower and the flash depth is not high, so that the energy consumption reduction effect of the flash evaporation of the lean solution is not obvious.
Disclosure of Invention
In order to solve the technical problems, the utility model designs a waste heat cascade recovery system for a flue gas carbon capture regeneration system; the problems that the cooling load of regenerated gas in the existing carbon dioxide trapping system is too high, the flash evaporation of lean solution is not obvious, consumption reduction is not obvious, the temperature of the rich solution entering the regeneration tower is too low and the like are solved, so that the total energy consumption and the total circulating water consumption of the carbon trapping system are reduced.
The utility model adopts the following technical scheme:
the waste heat cascade recovery system for the flue gas carbon capture regeneration system comprises a cold rich liquid pipeline and a regeneration tower, wherein the cold rich liquid pipeline is divided into a cold rich liquid main pipeline and a cold rich liquid branch pipeline, the cold rich liquid main pipeline is sequentially communicated with a lean rich liquid heat exchanger, a regenerated gas-rich liquid heat exchanger and a flash steam-rich liquid heat exchanger and is communicated with the middle part of the regeneration tower, the cold rich liquid branch pipeline is communicated into the top part of the regeneration tower, and a final spray cooling device is communicated with the top part of the regeneration tower;
the hot lean liquid at the bottom end of the regeneration tower is communicated with a flash tank, flash steam output by the flash tank is communicated with a flash steam-rich liquid heat exchanger through a flash steam compressor for heat exchange, the flash steam after heat exchange is communicated to the bottom of the regeneration tower, and the flash hot lean liquid output by the flash tank is returned to the absorption unit after heat exchange by a lean-rich liquid heat exchanger through a lean liquid cooler;
the high-temperature wet regenerated gas at the top end of the regeneration tower is communicated into a regenerated gas-rich liquid heat exchanger for heat exchange and then is communicated into a first regenerated gas separator for gas-liquid separation, condensate at the bottom of the first separator after gas-liquid separation is communicated into the regeneration tower and is communicated with a primary spray cooling device arranged below a final spray cooling device of the regeneration tower, the regenerated gas separated by the first regenerated gas separator is communicated into a second regenerated gas separator for gas-liquid separation after passing through a regenerated gas cooler, and condensate at the bottom of the second separator after gas-liquid separation is communicated into the final spray cooling device of the regeneration tower;
the bottom of the regeneration tower is communicated with a reboiler by the hot lean liquid, and reboiling steam generated by the reboiler and amine liquid are communicated into the bottom of the regeneration tower, and filler sections are respectively arranged among the bottom of the regeneration tower, the middle of the regeneration tower and the top of the regeneration tower.
Preferably, a demister is arranged at the top of the regeneration tower.
Preferably, a liquid collecting redistributor is arranged in the middle of the regeneration tower.
Preferably, the front end of the cold rich liquid pipeline is communicated with a cold rich liquid inlet, a rich liquid pump and an electric regulating valve, and the electric regulating valve regulates flow distribution of the cold rich liquid main pipeline and the cold rich liquid branch pipeline.
Preferably, a lean solution lifting pump is communicated between the bottom end of the regeneration tower and the flash tank.
Preferably, a reboiler pump is communicated between the bottom end of the regeneration tower and the reboiler.
Preferably, a main lean liquid pump is communicated between the flash tank and the lean-rich liquid heat exchanger.
Compared with the prior art, the utility model has the beneficial effects that:
(1) According to the waste heat cascade recovery system for the flue gas carbon capture regeneration system, cascade recovery utilization from low-grade waste heat to high-grade waste heat is sequentially realized according to the heat exchange equipment with low-to-high arrangement of hot stream temperature and cold rich liquid, and the rich liquid temperature entering a regeneration tower is further improved, so that the energy consumption of a reboiler is reduced;
(2) The waste heat cascade recovery system for the flue gas carbon capture regeneration system can relieve the double limitation that the outlet steam of the flash evaporation steam compressor needs to meet the maximum allowable temperature of the absorbent for a long time and is higher than the operation pressure of the regeneration tower, and compared with the prior art, the waste heat cascade recovery system can increase the pressure drop of the flash evaporation tank, deepen the flash evaporation depth and increase the flash evaporation steam production, thereby reducing the steam demand of a reboiler and the energy consumption of the reboiler. The improvement of the flash steam temperature caused by the increase of the pressure difference between the flash tank and the outlet of the flash steam compressor is solved by heat exchange with cold rich liquid, so that the temperature of the rich liquid entering the tower is improved, the control of the temperature of the flash steam finally entering the regeneration tower is realized, and the heat generated by the flash system can completely enter the regeneration tower without causing energy waste;
(3) According to the waste heat cascade recovery system for the flue gas carbon capture regeneration system, provided by the utility model, the deep flash evaporation with high flash tank pressure drop is adopted, and the heat of the hot lean solution is further recovered, so that the temperature of the hot lean solution entering a lean-rich solution heat exchanger is further reduced, the temperature of the lean solution after heat exchange is lower, and compared with the prior art, the load of a lean solution cooler before entering an absorption unit can be reduced;
(4) The waste heat step recovery system for the flue gas carbon capture regeneration system provided by the utility model adopts the cold rich liquid to recover the heat of the regenerated gas leaving the regeneration tower, so that the temperature of the high-temperature wet regenerated gas is reduced; meanwhile, condensate is separated through the first separator of the regenerated gas, so that the flow of the high-temperature wet regenerated gas is reduced, and the volume and the load of a regenerated gas cooler in a subsequent process are reduced;
(5) According to the waste heat cascade recovery system for the flue gas carbon capture regeneration system, the condensate liquid separated by the first regenerated gas separator is used as cooling liquid for primary spray cooling at the top of the regeneration tower, the condensate liquid separated by the cold rich liquid branch and the second regenerated gas separator is used as cooling liquid for final spray cooling at the top of the regeneration tower, and the two-stage spray cooling can reduce the temperature of the regenerated gas leaving the absorption tower, so that the load of a regenerated gas cooler is reduced; the two-stage cooling spraying is beneficial to intercepting large liquid drops carried by regenerated gas, promoting the growth of small liquid drops and enhancing the effect of the tower top demister.
Drawings
FIG. 1 is a schematic view of a construction of the present utility model;
in the figure: 1. the device comprises a rich liquid pump, 2, a regeneration tower, 3, a lean-rich liquid heat exchanger, 4, a regenerated gas-rich liquid heat exchanger, 5, a flash evaporation steam-rich liquid heat exchanger, 6, a reboiler pump, 7, a reboiler, 8, a lean liquid lifting pump, 9, a flash evaporation tank, 10, a flash evaporation steam compressor, 11, a main lean liquid pump, 12, a lean liquid cooler, 13, a regenerated gas first separator, 14, a regenerated gas cooler, 15, a regenerated gas second separator, 201, a demister, 202, a final spray cooling device, 203, a primary spray cooling device, 204, a liquid collecting redistributor, 205 and a filler section;
i, cold rich liquid, II, cold rich liquid branch, III, cold rich liquid main, IV, reboiling front hot lean liquid, V, reboiling steam and amine liquid, VI, hot lean liquid, VII, flash steam, VIII, flash back hot lean liquid, IX, high-temperature wet regenerated gas, X, condensate at the bottom of the first separator, XI, condensate at the bottom of the second separator and crude regenerated gas.
Description of the embodiments
The technical scheme of the utility model is further specifically described by the following specific embodiments with reference to the accompanying drawings:
examples: as shown in fig. 1, the waste heat cascade recovery system for the flue gas carbon capture regeneration system comprises a rich liquid pump 1, a regeneration tower 2, a lean and rich liquid heat exchanger 3, a regenerated gas-rich liquid heat exchanger 4, a flash steam-rich liquid heat exchanger 5, a reboiler pump 6, a reboiler 7, a lean liquid lift pump 8, a flash tank 9, a flash steam compressor 10, a main lean liquid pump 11, a lean liquid cooler 12, a regenerated gas first separator 13, a regenerated gas cooler 14 and a regenerated gas second separator 15; a demister 201, a final spray cooling device 202, a primary spray cooling device 203, a liquid collecting redistributor 204 and a filler section 205 are arranged in the regeneration tower.
As shown in figure 1, the waste heat cascade recovery system of the 2.5 ten thousand tons/year flue gas carbon capture regeneration system is characterized in that after cold rich liquid I at the temperature of 46 ℃ from an absorption system enters the system, the lift is firstly increased by a rich liquid pump 1 and then divided into a cold rich liquid main path III and a cold rich liquid branch path II which are connected in parallel, and the flow distribution of the main path and the branch path is regulated by an electric regulating valve of the main path, so that the flow of the branch path accounts for 15% of the total flow; the cold rich liquid branch II is directly conveyed to the top of the regeneration tower 2, is sprayed by a final spray cooling device 202, and carries out final cooling on high-temperature regenerated gas carrying a large amount of water vapor in the tower, and finally reduces the temperature of high-temperature wet regenerated gas IX to 85.5 ℃; the cold rich liquid main path III is conveyed to a lean rich liquid heat exchanger 3 to be used as cold flow, exchanges heat with hot lean liquid VIII from a flash evaporation system, and the temperature is raised to 72.5 ℃; after heat exchange, the cold rich liquid is conveyed to a regenerated gas-rich liquid heat exchanger 4 to be used as cold flow, exchanges heat with high-temperature wet regenerated gas IX at the outlet of the top of the regeneration tower, and the temperature is further increased to 76.6 ℃; the cold rich liquid after heat exchange is conveyed to a flash steam-rich liquid heat exchanger 5 to be used as a cold flow, and exchanges heat with superheated flash steam VII to reduce the superheat degree; the temperature of the rich liquid after heat exchange finally reaches 80.8 ℃, the rich liquid is conveyed to the middle part of the regeneration tower 2, enters the tower at Leng Fuye branch II and the lower part of the condensate XI inlet at the bottom of the secondary separator of the regenerated gas, is uniformly distributed in the tower through a liquid collecting redistributor 204, and performs heat and mass transfer with the upward secondary steam from the reboiler at the lower packing section 205 to complete the removal of carbon dioxide and the regeneration of the absorbent.
The regenerated hot lean solution part is conveyed to a reboiler 7 through a reboiler pump 6, and reboiled steam and amine solution V at 111.4 ℃ are generated after indirect heat exchange by external steam at 144 ℃ and 0.4MPa, and energy is supplied to the regeneration process of the absorbent after the reboiled steam and amine solution V return to the regeneration tower 2; the hot lean liquid VI leaves the regeneration tower 2 and reaches 111.5 ℃, is conveyed to a flash tank 9 with the operating pressure of 40kPa for flash evaporation through a lean liquid lifting pump 8, flash evaporation steam VII with the temperature of 78.2 ℃ and 2.4t/h is generated, the pressure is lifted to 142kPa through a flash evaporation steam compressor 10, and the temperature of the flash evaporation steam VII is then lifted to 236.0 ℃. The compressed superheated steam VII is subjected to heat recovery through a flash steam-rich liquid heat exchanger 5, and enters a tower from the bottom of a regeneration tower 2 after the temperature is reduced to 120 ℃ to supply energy for the regeneration process of the absorbent; the temperature of the rest hot lean solution VIII in the flash evaporation process is reduced to 78.2 ℃, the rest hot lean solution VIII is conveyed to a lean-rich solution heat exchanger 3 through a main lean solution pump 11, heat is supplied to cold rich solution from an absorption tower, the temperature is further reduced to 56.5 ℃, and finally the lean solution passes through a lean solution cooler 12, and the temperature is reduced to 40 ℃ through circulating cooling water and then returns to an absorption unit;
when the high-temperature wet regenerated gas IX leaves the top of the regeneration tower 2, the temperature reaches 85.4 ℃ and the water content reaches 20.0%. After part of heat is recovered by the regenerated gas-rich liquid heat exchanger 4, the temperature is reduced to 75.8 ℃, the water content is reduced to 14.2%, and the cooled high-temperature wet regenerated gas IX is conveyed to the first regenerated gas separator 13 for gas-liquid separation. The flow X of condensate at the bottom of the first separator reaches 0.21t/h, the condensate is conveyed to the lower part of the inlet of the cold rich liquid branch II and enters the regeneration tower, and the primary cooling spray device 203 is used for carrying out primary cooling on the regenerated gas leaving the filler section; the regenerated gas leaving the first regenerated gas separator 13 enters a regenerated gas cooler 14, is cooled to 30 ℃ by carrying heat through circulating cooling water, and then enters a second regenerated gas separator 15 for gas-liquid separation. The flow rate of condensate XI at the bottom of the second separator reaches 0.38t/h, and the condensate XI and the cold rich liquid branch III are jointly subjected to final spray cooling on regenerated gas in the tower through a final cooling spray device 202; leave fromCO in the crude regeneration gas XII of the regeneration gas second separator 15 2 The purity is 98.7 percent, and the water content is reduced to 1.3 percent.
The main energy consumption indexes of the energy consumption equipment of the flue gas carbon capture regeneration system in the embodiment are compared with those of the original regeneration system adopting the traditional rich liquid classification and lean liquid flash evaporation process, and the main energy consumption indexes are shown in the following table:
therefore, the waste heat cascade recovery system for the flue gas carbon capture regeneration system greatly reduces total energy consumption.
The above-described embodiment is only a preferred embodiment of the present utility model, and is not limited in any way, and other variations and modifications may be made without departing from the technical aspects set forth in the claims.
Claims (7)
1. The waste heat cascade recovery system for the flue gas carbon capture regeneration system comprises a cold rich liquid pipeline and a regeneration tower, and is characterized in that the cold rich liquid pipeline is divided into a cold rich liquid main pipeline and a cold rich liquid branch pipeline, the cold rich liquid main pipeline is sequentially communicated with a lean rich liquid heat exchanger, a regenerated gas-rich liquid heat exchanger and a flash steam-rich liquid heat exchanger and is communicated with the middle part of the regeneration tower, the cold rich liquid branch pipeline is communicated into the top part of the regeneration tower, and a final spray cooling device at the top part of the regeneration tower is communicated;
the hot lean liquid at the bottom end of the regeneration tower is communicated with a flash tank, flash steam output by the flash tank is communicated with a flash steam-rich liquid heat exchanger through a flash steam compressor for heat exchange, the flash steam after heat exchange is communicated to the bottom of the regeneration tower, and the flash hot lean liquid output by the flash tank is returned to the absorption unit after heat exchange by a lean-rich liquid heat exchanger through a lean liquid cooler;
the high-temperature wet regenerated gas at the top end of the regeneration tower is communicated into a regenerated gas-rich liquid heat exchanger for heat exchange and then is communicated into a first regenerated gas separator for gas-liquid separation, condensate at the bottom of the first separator after gas-liquid separation is communicated into the regeneration tower and is communicated with a primary spray cooling device arranged below a final spray cooling device of the regeneration tower, the regenerated gas separated by the first regenerated gas separator is communicated into a second regenerated gas separator for gas-liquid separation after passing through a regenerated gas cooler, and condensate at the bottom of the second separator after gas-liquid separation is communicated into the final spray cooling device of the regeneration tower;
the bottom of the regeneration tower is communicated with a reboiler by the hot lean liquid, and reboiling steam generated by the reboiler and amine liquid are communicated into the bottom of the regeneration tower, and filler sections are respectively arranged among the bottom of the regeneration tower, the middle of the regeneration tower and the top of the regeneration tower.
2. The waste heat cascade recovery system for a flue gas carbon capture regeneration system of claim 1, wherein a demister is provided at the top of the regeneration tower.
3. The waste heat cascade recovery system for a flue gas carbon capture regeneration system according to claim 1, wherein a liquid collection redistributor is provided in the middle of the regeneration tower.
4. The waste heat cascade recovery system for a flue gas carbon capture regeneration system according to claim 1, wherein the front end of the cold rich liquid pipeline is communicated with a cold rich liquid inlet, a rich liquid pump and an electric regulating valve, and the electric regulating valve regulates flow distribution of a cold rich liquid main pipeline and a cold rich liquid branch pipeline.
5. The waste heat cascade recovery system for the flue gas carbon capture regeneration system according to claim 1, wherein a lean solution lift pump is communicated between the bottom end of the regeneration tower and the flash tank.
6. The waste heat cascade recovery system for a flue gas carbon capture regeneration system according to claim 1, wherein a reboiler pump is communicated between the bottom end of the regeneration tower and the reboiler.
7. The waste heat cascade recovery system for a flue gas carbon capture regeneration system of claim 1, wherein a main lean liquid pump is in communication between the flash tank and the lean-rich liquid heat exchanger.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202320191024.4U CN219511357U (en) | 2023-02-13 | 2023-02-13 | Waste heat cascade recovery system for flue gas carbon capture regeneration system |
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| CN202320191024.4U CN219511357U (en) | 2023-02-13 | 2023-02-13 | Waste heat cascade recovery system for flue gas carbon capture regeneration system |
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