CN218077173U - Coke oven flue gas carbon dioxide capture system - Google Patents
Coke oven flue gas carbon dioxide capture system Download PDFInfo
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- CN218077173U CN218077173U CN202222167366.0U CN202222167366U CN218077173U CN 218077173 U CN218077173 U CN 218077173U CN 202222167366 U CN202222167366 U CN 202222167366U CN 218077173 U CN218077173 U CN 218077173U
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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
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- 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 provides a coke oven flue gas carbon dioxide capture system, which belongs to the technical field of flue gas treatment and comprises an absorption unit and an desorption recovery unit; the absorption unit comprises an absorption tower, the lower part of the absorption tower is provided with a to-be-treated flue gas inlet which is communicated with the heat exchanger, the bottom end of the absorption tower is provided with a rich liquid outlet, the rich liquid outlet is respectively conveyed to the lean rich liquid heat exchanger and the first gas-liquid heat exchanger through a rich liquid pump, and the decarbonized flue gas in the absorption tower is discharged from the top end, enters the first gas-liquid heat exchanger and then is discharged through the heat exchanger; the absorption unit comprises a desorption tower, one side of the desorption tower is provided with a rich liquid inlet pipeline communicated with the lean rich liquid heat exchanger and the first gas-liquid heat exchanger, the top end of the desorption tower is provided with a gas outlet pipeline, the bottom end of the desorption tower is provided with a regenerated lean liquid outlet pipe orifice, and the regenerated lean liquid outlet pipe orifice is communicated with the absorption tower through a lean liquid pump and the lean rich liquid heat exchanger; the utility model realizes the capture of the carbon dioxide in the coke oven flue gas by an absorption method, and utilizes the flue gas and the waste heat of lean and rich liquid to the maximum extent, thereby realizing the energy gradient utilization.
Description
Technical Field
The utility model relates to a flue gas treatment facility technical field, concretely relates to coke oven flue gas carbon dioxide entrapment system.
Background
Carbon capture, utilization and sequestration technologies are widely considered as one of the important technologies for dealing with global climate change and controlling greenhouse gas emissions.
Carbon dioxide capture technology processes typically include pre-combustion capture, post-combustion capture, and oxyfuel combustion capture, among others. The trapping after combustion means that the flue gas is treated by a physical or chemical method, and the carbon dioxide in the flue gas is trapped by waste gas treatment.
In the current carbon dioxide capture system, the energy in the system operation process can not be effectively utilized, the energy utilization rate is low, and the operation cost is high.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model provides a coke oven flue gas carbon dioxide entrapment system realizes coke oven flue gas carbon dioxide's entrapment through the absorption method to the at utmost utilizes flue gas, lean and rich liquid waste heat, realizes the energy cascade utilization.
In order to solve the technical problem, the utility model provides a coke oven flue gas carbon dioxide capture system, which comprises an absorption unit for capturing carbon dioxide in flue gas and a desorption recovery unit communicated with the absorption unit;
the absorption unit comprises an absorption tower, the lower part of the absorption tower is provided with a to-be-treated flue gas inlet which is communicated with a heat exchanger, the bottom end of the absorption tower is provided with a rich liquid outlet, the rich liquid outlet is respectively conveyed to a lean rich liquid heat exchanger and a first gas-liquid heat exchanger through a rich liquid pump, and decarburized flue gas in the absorption tower is discharged from the top end, enters the first gas-liquid heat exchanger and then is discharged through the heat exchanger;
the absorption unit comprises a desorption tower, a rich liquid inlet pipeline communicated with the lean rich liquid heat exchanger and the first gas-liquid heat exchanger is arranged on one side of the upper portion of the desorption tower, an air outlet pipeline is arranged at the top end of the desorption tower, a regenerated lean liquid outlet pipe is arranged at the bottom end of the desorption tower, and the regenerated lean liquid outlet pipe is communicated with one side of the upper portion of the absorption tower through a lean liquid pump and the lean rich liquid heat exchanger.
Furthermore, a cooler for cooling the flue gas to be treated is arranged on a pipeline for communicating the heat exchanger with the absorption tower.
Furthermore, an air outlet pipeline at the top end of the desorption tower is communicated with a condenser, and the outlet end of the condenser is connected with a compressor.
Furthermore, a reboiler is circularly communicated between a regeneration barren solution outlet pipe opening at the bottom end of the desorption tower and one side of the bottom of the desorption tower, and the reboiler adopts steam supplied by a waste heat boiler in a front desulfurization and denitrification process as a heat source.
Furthermore, a second gas-liquid heat exchanger is communicated between the bottom end of the desorption tower and the absorption tower, a liquid outlet end of the second gas-liquid heat exchanger is connected with a barren liquor pump, an outlet end of the barren liquor pump is connected with a barren liquor inlet end of the barren liquor-rich liquor heat exchanger, and a barren liquor outlet end of the barren liquor-rich liquor heat exchanger is communicated with one side of the upper portion of the absorption tower through a barren liquor cooler.
Furthermore, the decarbonized flue gas discharged from the first gas-liquid heat exchanger is led to the heat exchanger through a second gas-liquid heat exchanger.
Furthermore, the decarbonization flue gas discharged by the heat exchanger is heated by a heater and then discharged.
The utility model discloses an above-mentioned technical scheme's beneficial effect as follows:
1. the utility model discloses in, carry out the entrapment through the carbon dioxide of absorption method in with the coke oven flue gas to realize the enrichment of carbon dioxide through the desorption, through rich solution reposition of redundant personnel technology, decarbonization flue gas step heat transfer, poor rich solution heat transfer technique, flue gas, poor rich solution waste heat are utilized to the at utmost, realize that the energy step utilizes.
2. In the utility model, the heater is arranged before the decarbonization flue gas is exhausted, so that the temperature of the exhaust gas can be effectively maintained, the hot standby of the coke oven chimney is realized, and the safety production of the coke oven is ensured; the heat source used by the reboiler is steam generated by a waste heat boiler in the preposed desulfurization and denitrification process, so that the secondary energy consumption can be reduced.
Drawings
FIG. 1 is a schematic view of a carbon dioxide capturing system for coke oven flue gas of the present invention.
2. A heat exchanger; 3. a cooler; 4. an absorption tower; 5. a rich liquid pump; 6. a lean liquid cooler; 7. a lean-rich liquid heat exchanger; 8. a first gas-liquid heat exchanger; 9. a barren liquor pump; 10. a second gas-liquid heat exchanger; 11. a desorption tower; 12. a reboiler; 13. a condenser; 14. a compressor; 15. a heater.
Detailed Description
In order to make the purpose, technical solution and advantages of the embodiments of the present invention clearer, the following description will be made in conjunction with the accompanying fig. 1 of the embodiments of the present invention to clearly and completely describe the technical solution of the embodiments of the present invention. It is to be understood that the embodiments described are only some of the embodiments of the present invention, and not all of them. All other embodiments, which can be derived by a person skilled in the art from the described embodiments of the present invention, belong to the protection scope of the present invention.
As shown in fig. 1: a coke oven flue gas carbon dioxide capture system comprises an absorption unit for capturing carbon dioxide in flue gas and a desorption recovery unit communicated with the absorption unit;
the absorption unit comprises an absorption tower 4, the lower part of the absorption tower 4 is provided with a to-be-treated flue gas inlet which is communicated with the heat exchanger 2, the bottom end of the absorption tower 4 is provided with a rich liquid outlet, the rich liquid outlet is respectively conveyed to a lean rich liquid heat exchanger 7 and a first gas-liquid heat exchanger 8 through a rich liquid pump 5, and the decarbonized flue gas in the absorption tower 4 is discharged from the top end, enters the first gas-liquid heat exchanger 8 and then is discharged through the heat exchanger 2;
the absorption unit comprises a desorption tower 11, a rich liquid inlet pipeline communicated with the lean and rich liquid heat exchanger 7 and the first gas-liquid heat exchanger 8 is arranged on one side of the upper portion of the desorption tower 11, a gas outlet pipeline is arranged at the top end of the desorption tower 11, a regenerated lean liquid outlet pipe is arranged at the bottom end of the desorption tower 11, and the regenerated lean liquid outlet pipe is communicated with one side of the upper portion of the absorption tower 4 through a lean liquid pump 9 and the lean and rich liquid heat exchanger 7.
And a cooler 3 for cooling the flue gas to be treated is arranged on a pipeline for communicating the heat exchanger 2 with the absorption tower 4.
An air outlet pipeline at the top end of the desorption tower 11 is externally communicated with a condenser 13, and an outlet end of the condenser 13 is connected with a compressor 14.
A reboiler 12 is circularly communicated between a regeneration barren solution outlet pipe opening at the bottom end of the desorption tower 11 and one side of the bottom of the desorption tower 11, and the reboiler 12 adopts steam supplied by a waste heat boiler in a front desulfurization and denitrification process as a heat source.
A second gas-liquid heat exchanger 10 is communicated between the bottom end of the desorption tower 11 and the absorption tower 4, a liquid outlet end of the second gas-liquid heat exchanger 10 is connected with a lean liquid pump 9, an outlet end of the lean liquid pump 9 is connected with a lean liquid inlet end of the lean-rich liquid heat exchanger 7, and a lean liquid outlet end of the lean-rich liquid heat exchanger 7 is communicated with one side of the upper portion of the absorption tower 4 through a lean liquid cooler 6.
The decarbonized flue gas discharged from the first gas-liquid heat exchanger 8 is led to the heat exchanger 2 through the second gas-liquid heat exchanger 10.
Wherein, the decarbonization flue gas discharged by the heat exchanger 2 is heated by a heater 15 and then discharged.
The utility model discloses a working method: specifically, the purified coke oven flue gas from the desulfurization and denitrification device enters the heat exchanger 2 through a pipeline and exchanges heat with the decarbonized flue gas from the second gas-liquid heat exchanger 10. The coke oven flue gas after heat exchange enters a cooler 3, is cooled to 40-50 ℃ and then enters an absorption tower 4. In the absorption tower 4, the coke oven flue gas reversely contacts with the lean solution sprayed from the top of the tower from bottom to top, the carbon dioxide in the flue gas is absorbed by the lean solution under the pushing of mass transfer force, and the rich solution absorbing the carbon dioxide flows out from the bottom end of the absorption tower 4 and is divided into two parts by a rich solution pump 5 to be respectively conveyed to a lean and rich solution heat exchanger 7 and a first gas-liquid heat exchanger 8.
The rich liquid entering the lean-rich liquid heat exchanger 7 exchanges heat with the lean liquid from the lean liquid pump 9, enters the desorption tower 11 through a pipeline, is regenerated into the lean liquid by one stage in the desorption tower 11, enters the desorption tower 11 after exchanging heat with the decarbonized flue gas at the top of the absorption tower 4, and is regenerated into the lean liquid by one stage in the desorption tower 11.
The desorbed carbon dioxide is discharged from the top end of the desorption tower 11 and enters a condenser 13, and then enters a product refining process after passing through a compressor 14.
A reboiler 12 is circularly communicated between a regenerated lean solution outlet pipe opening at the bottom end of the desorption tower 11 and one side of the bottom of the desorption tower 11, part of the regenerated lean solution at the bottom end of the desorption tower 11 is heated by the reboiler 12 and then returns to the bottom of the desorption tower 11 to provide mass transfer power for desorption, wherein the reboiler 12 adopts steam supplied by a waste heat boiler in a front desulfurization and denitrification process as a heat source, so that the secondary energy consumption can be reduced; and other regenerated barren solution exchanges heat with the decarbonized flue gas of the second gas-liquid heat exchanger 10, is primarily cooled, enters the barren and rich solution heat exchanger 7 through a barren solution pump 9, is secondarily cooled with rich solution from the bottom end of the absorption tower 4, is further cooled through a barren solution cooler 6, and is sent to the top of the absorption tower 4.
The decarbonized flue gas discharged from the top of the absorption tower 4 sequentially enters a first gas-liquid heat exchanger 8, a second gas-liquid heat exchanger 10 and a heat exchanger 2, namely the flue gas is subjected to heat exchange with rich liquid at the bottom of the absorption tower 4, regenerated barren liquid at the bottom of a desorption tower 11 and clean coke oven flue gas after desulfurization and denitrification, and then is heated to the exhaust temperature and then is discharged, namely the flue gas is subjected to rich liquid shunting process, decarbonized flue gas step heat exchange and barren and rich liquid heat exchange technologies, flue gas and barren and rich liquid waste heat are utilized to the maximum extent, energy step utilization is realized, and the heater 15 is arranged before the decarbonized flue gas is exhausted, so that the exhaust temperature can be effectively maintained, the heat of a coke oven chimney is reserved, and the safe production of the coke oven is ensured.
In the present invention, unless otherwise explicitly specified or limited, for example, it may be fixedly connected, detachably connected, or integrated; can be mechanically or electrically connected; they may be directly connected or indirectly connected through an intermediate medium, and may be connected through the inside of two elements or in an interaction relationship between two elements, unless otherwise specifically defined, and the specific meaning of the above terms in the present invention will be understood by those skilled in the art according to specific situations.
The foregoing is a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of improvements and embellishments can be made without departing from the principle of the present invention, and these improvements and embellishments should also be regarded as the protection scope of the present invention.
Claims (7)
1. A coke oven flue gas carbon dioxide capture system is characterized in that: comprises an absorption unit for capturing carbon dioxide in the flue gas and a desorption recovery unit communicated with the absorption unit;
the absorption unit comprises an absorption tower (4), a to-be-treated flue gas inlet communicated with the heat exchanger (2) is formed in the lower portion of the absorption tower (4), a rich liquid outlet is formed in the bottom end of the absorption tower (4), the rich liquid outlet is respectively conveyed to a lean rich liquid heat exchanger (7) and a first gas-liquid heat exchanger (8) through a rich liquid pump (5), and decarburized flue gas in the absorption tower (4) is discharged from the top end, enters the first gas-liquid heat exchanger (8) and then is discharged through the heat exchanger (2);
the absorption unit comprises a desorption tower (11), wherein a rich liquid inlet pipeline communicated with the lean-rich liquid heat exchanger (7) and the first gas-liquid heat exchanger (8) is arranged on one side of the upper part of the desorption tower (11), a gas outlet pipeline is arranged at the top end of the desorption tower (11), a regenerated lean liquid outlet pipe orifice is arranged at the bottom end of the desorption tower (11), and the regenerated lean liquid outlet pipe orifice is communicated with one side of the upper part of the absorption tower (4) through a lean liquid pump (9) and the lean-rich liquid heat exchanger (7).
2. The coke oven flue gas carbon dioxide capture system of claim 1, wherein: and a cooler (3) for cooling the flue gas to be treated is arranged on a pipeline for communicating the heat exchanger (2) with the absorption tower (4).
3. The coke oven flue gas carbon dioxide capture system of claim 1, wherein: an air outlet pipeline at the top end of the desorption tower (11) is communicated with a condenser (13) outwards, and the outlet end of the condenser (13) is connected with a compressor (14).
4. The coke oven flue gas carbon dioxide capture system of claim 1, wherein: a reboiler (12) is circularly communicated between a regeneration barren solution outlet pipe opening at the bottom end of the desorption tower (11) and one side of the bottom of the desorption tower (11), and the reboiler (12) adopts steam supplied by a waste heat boiler in a front desulfurization and denitrification process as a heat source.
5. The coke oven flue gas carbon dioxide capture system of claim 1, wherein: a second gas-liquid heat exchanger (10) is communicated between the bottom end of the desorption tower (11) and the absorption tower (4), the liquid outlet end of the second gas-liquid heat exchanger (10) is connected with a barren liquid pump (9), the outlet end of the barren liquid pump (9) is connected with the barren liquid inlet end of the barren and rich liquid heat exchanger (7), and the barren liquid outlet end of the barren and rich liquid heat exchanger (7) is communicated with one side of the upper part of the absorption tower (4) through a barren liquid cooler (6).
6. The coke oven flue gas carbon dioxide capture system of claim 5, wherein: and the decarbonized flue gas discharged from the first gas-liquid heat exchanger (8) is led to the heat exchanger (2) through a second gas-liquid heat exchanger (10).
7. The coke oven flue gas carbon dioxide capture system of claim 6, wherein: and the decarbonization flue gas discharged by the heat exchanger (2) is heated by a heater (15) and then discharged.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222167366.0U CN218077173U (en) | 2022-08-17 | 2022-08-17 | Coke oven flue gas carbon dioxide capture system |
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| CN202222167366.0U CN218077173U (en) | 2022-08-17 | 2022-08-17 | Coke oven flue gas carbon dioxide capture system |
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| CN218077173U true CN218077173U (en) | 2022-12-20 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116078116A (en) * | 2023-01-17 | 2023-05-09 | 武汉理工大学 | Container-type modularized ship tail gas carbon capture system |
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2022
- 2022-08-17 CN CN202222167366.0U patent/CN218077173U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116078116A (en) * | 2023-01-17 | 2023-05-09 | 武汉理工大学 | Container-type modularized ship tail gas carbon capture system |
| CN116078116B (en) * | 2023-01-17 | 2024-04-26 | 武汉理工大学 | Container-type modularized ship tail gas carbon capture system |
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