CN216935390U - A high temperature hot-blast furnace flue gas carbon dioxide entrapment system for waste heat recovery - Google Patents
A high temperature hot-blast furnace flue gas carbon dioxide entrapment system for waste heat recovery Download PDFInfo
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Abstract
The utility model relates to a high-temperature hot blast furnace flue gas carbon dioxide capturing system for waste heat recovery.A reboiler inlet is connected with a high-temperature hot blast furnace flue gas inlet, an outlet is connected with the gas inlet of an absorption tower through a high-temperature flue gas cooling heat exchanger, a washing liquid storage tank and the absorption tower form a passage, an inlet of a lean-rich liquid heat exchanger is connected with an absorption liquid storage tank, and an outlet is connected with a lean liquid inlet of the absorption tower; the rich liquid outlet of the absorption tower is connected to a first inlet of a rich liquid reheater sequentially through the high-temperature flue gas cooling heat exchanger and the lean and rich liquid heat exchanger, a first outlet of the rich liquid reheater is connected to a rich liquid inlet of the desorption tower, the desorption tower and the reboiler form a passage, a lean liquid outlet of the desorption tower is communicated with an inlet of the lean and rich liquid heat exchanger, an exhaust port of the desorption tower is communicated with a second inlet of the rich liquid reheater, a second outlet of the rich liquid reheater is communicated with a regenerated carbon dioxide gas cooler, an outlet of the regenerated carbon dioxide gas cooler is communicated with a regenerated separator, and the regenerated separator is provided with an exhaust port.
Description
Technical Field
The utility model belongs to the technical field of waste heat recovery, and particularly relates to a high-temperature hot blast stove flue gas carbon dioxide capture system for waste heat recovery.
Background
The excessive emission of greenhouse gases such as carbon dioxide and the like causes global climate change and seriously threatens the safety of human life and property, so the emission reduction of the carbon dioxide is not slow at all.
The carbon capture, utilization and sequestration (CCUS for short) technology is a promising approach for realizing the remarkable emission reduction of carbon dioxide in a short time. The chemical absorption method represented by an alcohol amine absorbent is the most mature method which can be applied to the high-temperature hot blast stove flue gas carbon dioxide capture at present.
However, the chemical absorption method based on the alcohol amine absorbent has over high energy consumption in large-scale application, and the energy consumption is as high as 4.0-6.0 MJ/kg CO2And a large amount of heat is required to regenerate the alcohol amine absorbent.
SUMMERY OF THE UTILITY MODEL
Based on the problems existing in the background technology, the utility model provides a high-temperature hot blast stove flue gas carbon dioxide capture system for waste heat recovery, which can effectively utilize the heat of high-temperature flue gas of a hot blast stove and gas exhausted from the top end of a desorption tower to heat rich liquid, reduce the heat required by rich liquid desorption, effectively utilize the high-temperature flue gas of the hot blast stove to provide heat for the desorption tower to desorb carbon dioxide through the stripping effect, and improve the utilization rate of energy in the system.
In order to achieve the purpose, the utility model adopts the technical scheme that:
a high-temperature hot blast stove flue gas carbon dioxide capture system for waste heat recovery comprises a washing liquid storage tank, an absorption tower, a high-temperature flue gas cooling heat exchanger, a lean and rich liquid heat exchanger, a rich liquid reheater, a desorption tower and a reboiler;
an inlet of the reboiler is connected with a flue gas inlet of the high-temperature hot blast stove, an outlet of the reboiler is connected with a gas inlet of the absorption tower through a high-temperature flue gas cooling heat exchanger, a washing liquid storage tank and a liquid inlet and a liquid outlet of the absorption tower form a passage, an inlet of the lean and rich liquid heat exchanger is connected with an absorption liquid storage tank, an outlet of the lean and rich liquid heat exchanger is connected with a lean liquid inlet of the absorption tower, and the absorption tower is provided with an exhaust port;
the absorption tower is characterized in that a rich liquid outlet of the absorption tower is connected to a first inlet of a rich liquid reheater sequentially through a high-temperature flue gas cooling heat exchanger and a lean and rich liquid heat exchanger, a first outlet of the rich liquid reheater is connected to a rich liquid inlet of a desorption tower, the desorption tower and a reboiler form a passage, a lean liquid outlet of the desorption tower is communicated with an inlet of the lean and rich liquid heat exchanger, an exhaust port of the desorption tower is communicated with a second inlet of the rich liquid reheater, a second outlet of the rich liquid reheater is communicated with a regenerated carbon dioxide gas cooler, an outlet of the regenerated carbon dioxide gas cooler is communicated with a regeneration separator, and the regeneration separator is provided with an exhaust port.
Preferably, the flue gas cooling heat exchanger further comprises an induced draft fan, an outlet of the reboiler is connected to an inlet of the induced draft fan, and an outlet of the induced draft fan is connected to an inlet of the high-temperature flue gas cooling heat exchanger.
Preferably, the outlet of the washing liquid storage tank is connected with the inlet of a washing pump, and the outlet of the washing pump is connected with the liquid inlet of the absorption tower.
Preferably, a rich liquid pump is arranged between the high-temperature flue gas cooling heat exchanger and the lean-rich liquid heat exchanger.
Preferably, a barren liquor pump is installed between the absorption liquid storage tank and the barren and rich liquor heat exchanger, and an inlet of the barren liquor pump is communicated with a barren liquor outlet of the desorption tower.
Preferably, a lean liquid cooler is arranged between the outlet of the lean-rich liquid heat exchanger and the lean liquid inlet of the absorption tower.
Preferably, the first outlet of the regenerative separator is connected with an underground tank.
Preferably, the second outlet of the regeneration separator is respectively connected with the liquid inlet of the desorption tower and the inlet of the washing liquid storage tank.
Furthermore, a backflow liquid supplementing pump is installed at a second outlet of the regeneration separator, and an outlet of the backflow liquid supplementing pump is respectively connected to a liquid inlet of the desorption tower and an inlet of the washing liquid storage tank.
Preferably, a foam removing device is arranged below the exhaust port of the regeneration separator, and a volume metering device is arranged outside the exhaust port of the regeneration separator.
Compared with the prior art, the utility model has the following beneficial technical effects:
the utility model relates to a high-temperature hot blast stove flue gas carbon dioxide capture system for waste heat recovery.A reboiler outlet is connected with an air inlet of an absorption tower through a high-temperature flue gas cooling heat exchanger, so that the reboiler can absorb the heat of the flue gas of the high-temperature hot blast stove and provide heat for desorbing carbon dioxide by a desorption tower through a stripping effect, the high-temperature flue gas can exchange heat with rich liquid in a rich liquid pipeline, the temperature is reduced to a reaction temperature, and the temperature of the rich liquid is increased to complete primary heat recovery; because the outlet of the lean-rich liquid heat exchanger is connected with the lean liquid inlet of the absorption tower, the cooled flue gas enters the absorption tower, the absorption liquid in the absorption tower can capture carbon dioxide, the washing liquid in the washing liquid storage tank can be recovered and used for purifying the absorbent in the high-temperature flue gas, the lean liquid absorbs the carbon dioxide in the high-temperature flue gas to form rich liquid, the heat in the high-temperature flue gas is firstly absorbed by the high-temperature flue gas cooling heat exchanger, then the heat in the lean liquid is absorbed in the lean-rich liquid heat exchanger, the lean liquid is heated again by the rich liquid reheater and enters the desorption tower, the rich liquid is heated in the reboiler and returns to the desorption tower, the carbon dioxide is desorbed from the rich liquid, and the rich liquid becomes the lean liquid after the carbon dioxide is desorbed. The lean solution enters a lean solution pipeline through a lean solution outlet of the desorption tower, an exhaust port of the desorption tower is communicated with an inlet of a rich solution reheater, an outlet of the rich solution reheater is communicated with a regenerated carbon dioxide gas cooler, an outlet of the regenerated carbon dioxide gas cooler is communicated with a regenerated separator, the desorbed carbon dioxide gas releases heat and then enters the regenerated carbon dioxide gas cooler to be cooled to form condensate, and the carbon dioxide gas is separated in the regenerated separator. According to the utility model, the high-temperature flue gas cooling heat exchanger and the rich liquid reheater are arranged, so that multi-stage heat recovery is realized, the heat of the high-temperature flue gas and the carbon dioxide gas exhausted by the desorption tower is efficiently transferred to the rich liquid, the temperature of the rich liquid in the rich liquid pipeline is increased, the heated rich liquid enters the desorption tower to be desorbed, the energy consumption is reduced, and the utilization rate of waste heat is improved; the flue gas of the high-temperature hot blast stove is directly introduced into a reboiler connected with the desorption tower to provide heat for the desorption tower to desorb the carbon dioxide through the steam stripping effect, so that the energy consumption required by system operation and amine solvent regeneration can be compensated.
Drawings
FIG. 1 is a process flow diagram of the high temperature hot blast stove flue gas carbon dioxide capture system of the present invention in use.
In the figure: 1-a washing liquid storage tank, 2-a washing pump, 3-an exhaust pipe, 4-a barren liquor cooler, 5-an absorption tower, 6-a high-temperature flue gas cooling heat exchanger, 7-a draught fan, 8-a pregnant solution pump, 9-a barren pregnant solution heat exchanger, 10-a barren solution pump, 11-a pregnant solution reheater, 12-an absorption liquid storage tank, 13-a desorption tower, 14-a regenerated carbon dioxide gas cooler, 15-a regeneration separator, 16-a reflux liquid supplementing pump, 17-a reboiler and 18-an underground tank.
Detailed Description
The present invention will be described in further detail with reference to the following drawings and specific embodiments, which should be understood as being described in the specification and drawings only for the purpose of illustrating the utility model and not for the purpose of limiting the same.
The utility model discloses a high-temperature hot blast stove flue gas carbon dioxide capture system for efficiently recovering waste heat, which takes a chemical absorption method of an alcohol amine absorbent as a specific process, and mainly comprises a washing liquid storage tank 1, an absorption tower 5, a high-temperature flue gas cooling heat exchanger 6, a barren solution cooler 4, a barren and rich solution heat exchanger 9, an absorption liquid storage tank 12, a rich solution reheater 11, a regenerated carbon dioxide gas cooler 14, a regeneration separator 15, a desorption tower 13 and a reboiler 17, as shown in figure 1. In the chemical absorption method using the alcohol amine absorbent, the absorption liquid discharged from the absorption tower 5 is a rich liquid, and the first absorption liquid or the desorbed rich liquid is a lean liquid. In the process, when high-temperature hot blast stove flue gas is introduced, the absorption liquid in the absorption liquid storage tank 12 runs in the reboiler 17, the desorption tower 13 and the absorption tower 5, a pipeline through which the lean liquid flows is called a lean liquid pipeline, and a pipeline through which the rich liquid flows is called a rich liquid pipeline between the desorption tower 13 and the absorption tower 5.
The specific configuration of the carbon dioxide capture system of the present invention (i.e., the manner in which the components are connected in the figures) and the corresponding operating principle will be described in detail below:
an inlet of the reboiler 17 is connected with an air inlet of the high-temperature hot blast furnace flue gas, an outlet of the reboiler 17 is connected with an inlet of the induced draft fan 7, an outlet of the induced draft fan 7 is connected with an inlet of the high-temperature flue gas cooling heat exchanger 6, and an outlet of the high-temperature flue gas cooling heat exchanger 6 is connected with an air inlet of the absorption tower 5, so that the induced draft fan 7 introduces the high-temperature flue gas passing through the reboiler 17 into an air inlet pipe of the induced draft fan 7, the high-temperature flue gas enters the absorption tower 5 through the air inlet at the lower part of the right side wall of the absorption tower 5 after exchanging heat with rich liquid in a rich liquid pipeline through the high-temperature flue gas cooling heat exchanger 6, and the absorption liquid in the absorption tower 5 can capture carbon dioxide; the upper part of the right side wall of the absorption tower 5 is provided with a barren solution inlet, the inlet of the barren and rich solution heat exchanger 9 is connected with an absorption solution storage tank 12, the outlet of the barren and rich solution heat exchanger 9 is connected with the barren solution inlet of the absorption tower 5, and the high-temperature flue gas entering the absorption tower 5 and the barren solution entering the absorption tower 5 from the barren solution inlet are subjected to absorption reaction to capture carbon dioxide in the high-temperature flue gas.
The high temperature flue gas of separation carbon dioxide can be difficult to avoid containing some absorbent, need retrieve, purify the absorbent in the high temperature flue gas, the left side wall upper portion of absorption tower 5 is equipped with washing liquid entry and washing liquid export, washing liquid storage tank 1 forms the route with the inlet and the liquid outlet of absorption tower 5, 1 exit linkage in washing liquid storage tank is at the entry of washing pump 2, the exit linkage of washing pump 2 is at the inlet of absorption tower 5, washing pump 2 introduces absorption tower 5 through the washing liquid entry with washing liquid from washing liquid storage tank 1, the high temperature flue gas that the purification separation contains carbon dioxide, the flue gas after the purification is discharged through setting up 3 blast pipes at absorption tower 5 tops, washing liquid flows back to washing liquid storage tank 1 through the washing liquid export.
The lean solution absorbs carbon dioxide in the high-temperature flue gas to form rich solution, a rich solution outlet of the absorption tower 5 is connected to a first inlet of a rich solution reheater 11 sequentially through a high-temperature flue gas cooling heat exchanger 6 and a lean and rich solution heat exchanger 9, a rich solution pump 8 is installed between the high-temperature flue gas cooling heat exchanger 6 and the lean and rich solution heat exchanger 9, a first outlet of the rich solution reheater 11 is connected to a rich solution inlet of a desorption tower 13, and the desorption tower 13 and a reboiler 17 form a passage. The rich solution enters a rich solution pipeline through a rich solution outlet arranged at the lower part of the right side wall of the absorption tower 5, the rich solution absorbs heat in high-temperature flue gas through a high-temperature flue gas cooling heat exchanger 6, the rich solution runs to a lean rich solution heat exchanger 9 under the action of a rich solution pump 8, the lean rich solution heat exchanger 9 absorbs heat in lean solution, the lean rich solution heat exchanger is reheated through a rich solution reheater 11, and the rich solution enters a desorption tower 13 through a rich solution inlet arranged at the upper part of the left side wall of the desorption tower 13 connected with the rich solution pipeline. The reboiler 17 is connected to the right side of the lower part of the desorption tower 13, and the rich liquid is heated in the reboiler 17 and returned to the desorption tower 13, so that the carbon dioxide is desorbed from the rich liquid, and the rich liquid becomes a lean liquid after the carbon dioxide is desorbed. A barren solution outlet of the desorption tower 13 is communicated with an inlet of the barren and rich solution heat exchanger 9, a barren solution pump 10 is installed between the absorption solution storage tank 12 and the barren and rich solution heat exchanger 9, an inlet of the barren solution pump 10 is communicated with a barren solution outlet of the desorption tower 13, barren solution enters a barren solution pipeline through a barren solution outlet arranged at the lower part of the left side wall of the desorption tower 13, a barren solution cooler 4 is installed between an outlet of the barren and rich solution heat exchanger 9 and a barren solution inlet of the absorption tower 5, and the barren solution cooler 4 is connected in the barren solution pipeline and used for adjusting the temperature of the barren solution entering the absorption tower 5. The barren solution passes through a barren solution pump 10, a barren and rich solution heat exchanger 9 and a barren solution cooler 4 in sequence and enters the absorption tower 5 through a barren solution inlet at the upper part of the right side wall of the absorption tower 5 connected with a barren solution pipeline.
The desorbed carbon dioxide gas is discharged from a carbon dioxide gas outlet provided at the top end of the desorption tower 13, and the carbon dioxide gas outlet is communicated with the second inlet of the rich liquid reheater 11. The gas-liquid separation and recovery system for the regenerated carbon dioxide comprises a regenerated carbon dioxide gas cooler 14 and a regenerated separator 15, wherein a second outlet of the rich liquid reheater 11 is communicated with the regenerated carbon dioxide gas cooler 14, an outlet of the regenerated carbon dioxide gas cooler 14 is communicated with the regenerated separator 15, heat is released by the rich liquid reheater 11 and then enters the regenerated carbon dioxide gas cooler 14, a part of water vapor and amine vapor are contained in the desorbed carbon dioxide gas, a condensate liquid is formed after cooling, and the cooled regenerated carbon dioxide and the cooled condensate liquid enter the regenerated separator 15. Since the first outlet of the regenerative separator 15 is connected to the underground tank 18, the condensate thus separated is partially collected into the underground tank 18, and the condensate in the underground tank 18 is treated as a waste liquid. In order to recover the amine vapor and maintain the water balance of the system of the present invention, a reflux liquid replenishing pump 16 is installed at the second outlet of the regeneration separator 15, the outlet of the reflux liquid replenishing pump 16 is respectively connected to the liquid inlet of the desorption tower 13 and the inlet of the washing liquid storage tank 1, when it is detected that the carbon dioxide in the condensate flowing into the reflux liquid replenishing pump 16 is higher, the condensate is totally refluxed to the desorption tower 13 through the reflux liquid replenishing pump 16 by only opening the valve on the pipeline connected to the liquid inlet of the desorption tower 13, and if it is detected that the carbon dioxide in the condensate flowing into the reflux liquid replenishing pump 16 is in a reasonable range, the condensate is refluxed to the desorption tower 13 and the washing liquid storage tank 1 respectively by simultaneously opening the valves on the two pipelines. The condensate which flows back into the washing liquid storage tank 1 does not influence the function of the washing liquid in the washing liquid storage tank 1, and the washing liquid in the washing liquid storage tank 1 can be replaced only when the washing liquid basically loses the function of the purification absorbent. The washing liquid reservoir 1 and the washing pump 2 are also referred to as washing system.
When the system is started, namely the preparation work before the high-temperature hot blast stove flue gas is introduced, the barren solution pump 10 leads the absorption solution in the absorption solution storage tank 12 into the absorption tower 5 through a barren solution pipeline, namely the barren solution pump 10, the barren and rich solution heat exchanger 9 and the barren solution cooler 4 in sequence, and the absorption tower is used for absorbing the carbon dioxide in the flue gas. The absorption liquid enters the desorption tower 13 from the rich liquid outlet of the absorption tower 5 through the high-temperature flue gas cooling heat exchanger 6, the rich liquid pump 8, the lean and rich liquid heat exchanger 9 and the rich liquid reheater 11 in sequence, is heated in the reboiler 17, returns to the desorption tower 13, enters the lean liquid pipeline from the lean liquid outlet of the desorption tower 13, and finally enters the absorption tower 5 to finish the preparation work. Because the smoke of the high-temperature hot blast stove is always introduced, the smoke of the high-temperature hot blast stove introduced before can form rich liquid in the system, thereby forming the technical process. In addition, the absorption liquid storage tank 12 is used for supplementing the loss of the absorption liquid in the system during the operation of the system.
The optimization of the carbon dioxide capturing system in the process flow is embodied in that the flue gas of the high-temperature hot blast stove is directly introduced into the reboiler 17 connected with the desorption tower 13, the desorption tower 13 desorbs the carbon dioxide through the steam stripping effect, and the reboiler 17 provides heat for the desorption process, so that the heat recovery is realized, and the consumption of extra heat is avoided. And then the high-temperature flue gas passing through the reboiler 17 is introduced into the high-temperature flue gas cooling heat exchanger 6 through the draught fan 7 to exchange heat with the rich liquid flowing out of the rich liquid outlet of the absorption tower 5, so that the temperature of the rich liquid is increased, and the high-efficiency utilization of the heat of the flue gas of the hot blast stove is realized. The high-temperature carbon dioxide gas desorbed and released by the desorption tower 13 passes through the rich liquid reheater 11 to exchange heat with the rich liquid entering the desorption tower 13, so that the heat of the high-temperature carbon dioxide gas is efficiently recovered.
Therefore, in order to describe the above process more completely, the high-temperature hot blast stove flue gas carbon dioxide capture system with high-efficiency waste heat recovery of the utility model comprises the following steps:
s1: cooling the high-temperature flue gas,
sending high-temperature flue gas of the hot blast stove passing through a reboiler 17 into a high-temperature flue gas cooling heat exchanger 6 through an induced draft fan 7, carrying out heat exchange on the high-temperature flue gas and rich liquor in a rich liquor pipeline through the high-temperature flue gas cooling heat exchanger 6, reducing the temperature of the high-temperature flue gas to a reaction temperature which can be generally 40 ℃, increasing the temperature of the rich liquor, and carrying out primary heat recovery; the washing pump 2 introduces the washing liquid into the absorption tower 5 from the washing liquid storage tank 1 through the washing liquid inlet, high-temperature flue gas containing carbon dioxide is purified and separated, the purified flue gas is discharged through the exhaust pipe 3 arranged at the top of the absorption tower 5, and the washing liquid flows back to the washing liquid storage tank 1 through the washing liquid outlet.
S2: the carbon dioxide is absorbed by the carbon dioxide absorption device,
the cooled flue gas is introduced into the absorption tower 5, and is subjected to absorption reaction with the lean solution entering the absorption tower 5 from the lean solution inlet, so that carbon dioxide in the flue gas is captured, and a rich solution is formed. A rich liquid outlet of the rich liquid self-absorption tower 5 is pumped out by a rich liquid pump 8, and the pressurized rich liquid enters a lean rich liquid heat exchanger 9 to exchange heat with lean liquid from a desorption tower 13 for secondary heat recovery;
s3: after the heat exchange of the lean rich solution, the temperature of the rich solution rises, the rich solution enters a rich solution reheater 11, and the rich solution exchanges heat with carbon dioxide gas discharged from a carbon dioxide gas outlet arranged at the top end of a desorption tower 13 and along with a large amount of steam, so that three-level heat recovery is performed;
s4: the heat of the flue gas is recovered,
the rich solution entering the desorption tower 13 flows into the reboiler 17, the rich solution is heated in the reboiler 17 and returns to the desorption tower 13, carbon dioxide is desorbed from the rich solution, the rich solution becomes a lean solution after the carbon dioxide is desorbed, and heat is provided for desorbing the carbon dioxide by using the flue gas of the high-temperature hot blast stove; the lean liquid enters the lean liquid pipeline through a lean liquid outlet arranged at the lower part of the left side wall of the desorption tower 13.
S5: the carbon dioxide is recovered, and the carbon dioxide is recovered,
the regenerated carbon dioxide gas after heat exchange flows out from the rich liquor reheater 11 and enters a gas-liquid separation and recovery system of the regenerated carbon dioxide, firstly, the regenerated carbon dioxide gas exchanges heat with circulating water in the regenerated carbon dioxide gas cooler 14, the regenerated carbon dioxide gas is cooled and then enters the regenerated separator 15, condensate entrained by the gas is separated in the regenerated separator 15, a foam removing device is arranged below an exhaust port of the regenerated separator 15, a volume metering device is arranged outside the exhaust port of the regenerated separator 15, the foam of the separated carbon dioxide is removed at the upper part of the regenerated separator 15, and then the carbon dioxide is sent to the next process for use after the volume of the carbon dioxide is measured. The separated condensate part is collected into an underground tank 18, and in order to recover the amine vapor and maintain the water balance of the system, the condensate is respectively refluxed into the desorption tower 13 and the washing liquid storage tank 1 through a reflux liquid supplementing pump 16 according to the concentration of carbon dioxide in the condensate.
The high-temperature flue gas of the high-temperature hot blast stove is always led into an air inlet pipe of a draught fan 7 through the high-temperature flue gas of a reboiler 17 and is sent into a high-temperature flue gas cooling heat exchanger 6, so that the circulating process is formed.
Claims (10)
1. A high-temperature hot blast stove flue gas carbon dioxide capture system for waste heat recovery is characterized by comprising a washing liquid storage tank (1), an absorption tower (5), a high-temperature flue gas cooling heat exchanger (6), a lean and rich liquid heat exchanger (9), a rich liquid reheater (11), a desorption tower (13) and a reboiler (17);
an inlet of the reboiler (17) is connected with a high-temperature hot blast stove flue gas inlet, an outlet of the reboiler (17) is connected with an air inlet of the absorption tower (5) through a high-temperature flue gas cooling heat exchanger (6), a washing liquid storage tank (1) and a liquid inlet and a liquid outlet of the absorption tower (5) form a passage, an inlet of the lean and rich liquid heat exchanger (9) is connected with an absorption liquid storage tank (12), an outlet of the lean and rich liquid heat exchanger (9) is connected with a lean liquid inlet of the absorption tower (5), and the absorption tower (5) is provided with an exhaust port (3);
a rich liquid outlet of the absorption tower (5) is connected with a first inlet of a rich liquid reheater (11) sequentially through a high-temperature flue gas cooling heat exchanger (6) and a lean rich liquid heat exchanger (9), a first outlet of the rich liquid reheater (11) is connected with a rich liquid inlet of a desorption tower (13), the desorption tower (13) and a reboiler (17) form a passage, a lean liquid outlet of the desorption tower (13) is communicated with an inlet of the lean rich liquid heat exchanger (9), an exhaust port of the desorption tower (13) is communicated with a second inlet of the rich liquid reheater (11), a second outlet of the rich liquid reheater (11) is communicated with a regenerated carbon dioxide gas cooler (14), an outlet of the regenerated carbon dioxide gas cooler (14) is communicated with a regenerated separator (15), and the regenerated separator (15) is provided with an exhaust port.
2. The high-temperature hot blast stove flue gas carbon dioxide capture system for waste heat recovery according to claim 1, further comprising an induced draft fan (7), wherein an outlet of the reboiler (17) is connected to an inlet of the induced draft fan (7), and an outlet of the induced draft fan (7) is connected to an inlet of the high-temperature flue gas cooling heat exchanger (6).
3. The high-temperature hot blast stove flue gas carbon dioxide capture system for waste heat recovery according to claim 1, wherein the outlet of the washing liquid storage tank (1) is connected to the inlet of the washing pump (2), and the outlet of the washing pump (2) is connected to the liquid inlet of the absorption tower (5).
4. A high temperature hot blast stove flue gas carbon dioxide capture system for waste heat recovery according to claim 1, characterized in that a rich liquor pump (8) is installed between the high temperature flue gas cooling heat exchanger (6) and the lean rich liquor heat exchanger (9).
5. The high-temperature hot blast stove flue gas carbon dioxide capture system for waste heat recovery according to claim 1, wherein a barren liquor pump (10) is installed between the absorption liquid storage tank (12) and the barren and rich liquor heat exchanger (9), and an inlet of the barren liquor pump (10) is communicated with a barren liquor outlet of the desorption tower (13).
6. A high temperature hot blast stove flue gas carbon dioxide capture system for waste heat recovery according to claim 1, characterized in that a lean liquid cooler (4) is installed between the outlet of the lean rich liquid heat exchanger (9) and the lean liquid inlet of the absorption tower (5).
7. A high temperature hot blast stove flue gas carbon dioxide capture system for waste heat recovery according to claim 1, characterised in that the first outlet of the regeneration separator (15) is connected with an underground tank (18).
8. The high temperature hot blast stove flue gas carbon dioxide capture system for waste heat recovery of claim 1, wherein the second outlet of the regeneration separator (15) is connected to the liquid inlet of the desorption tower (13) and the inlet of the scrubbing liquid storage tank (1), respectively.
9. The high-temperature hot blast stove flue gas carbon dioxide capture system for waste heat recovery according to claim 8, wherein a reflux liquid supplementing pump (16) is installed at the second outlet of the regeneration separator (15), and the outlet of the reflux liquid supplementing pump (16) is respectively connected to the liquid inlet of the desorption tower (13) and the inlet of the washing liquid storage tank (1).
10. The high-temperature hot blast stove flue gas carbon dioxide capture system for waste heat recovery according to claim 1, characterized in that a foam removal device is arranged below the exhaust port of the regeneration separator (15), and a volume metering device is arranged outside the exhaust port of the regeneration separator (15).
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN116036838A (en) * | 2023-01-06 | 2023-05-02 | 江苏科技大学 | Carbon dioxide trapping system and method |
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| CN117085468B (en) * | 2023-10-19 | 2023-12-19 | 中太海碳(上海)环保科技有限公司 | Energy-saving marine carbon capture system |
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