CN114963218A - Flue gas waste heat recovery device and method coupled with carbon capture - Google Patents
Flue gas waste heat recovery device and method coupled with carbon capture Download PDFInfo
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- CN114963218A CN114963218A CN202210609341.3A CN202210609341A CN114963218A CN 114963218 A CN114963218 A CN 114963218A CN 202210609341 A CN202210609341 A CN 202210609341A CN 114963218 A CN114963218 A CN 114963218A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 78
- 239000003546 flue gas Substances 0.000 title claims abstract description 75
- 239000002918 waste heat Substances 0.000 title claims abstract description 26
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 23
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 23
- 238000011084 recovery Methods 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title claims abstract description 17
- 238000010521 absorption reaction Methods 0.000 claims abstract description 72
- 239000002002 slurry Substances 0.000 claims abstract description 44
- 239000007788 liquid Substances 0.000 claims abstract description 43
- 238000003795 desorption Methods 0.000 claims abstract description 36
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 32
- 238000006477 desulfuration reaction Methods 0.000 claims description 27
- 230000023556 desulfurization Effects 0.000 claims description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 14
- 239000007789 gas Substances 0.000 claims description 10
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 7
- 239000001569 carbon dioxide Substances 0.000 claims description 5
- 230000008878 coupling Effects 0.000 claims description 5
- 238000010168 coupling process Methods 0.000 claims description 5
- 238000005859 coupling reaction Methods 0.000 claims description 5
- 229920006395 saturated elastomer Polymers 0.000 claims description 5
- 238000000746 purification Methods 0.000 claims 1
- 230000008929 regeneration Effects 0.000 abstract description 8
- 238000011069 regeneration method Methods 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 3
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 229920003169 water-soluble polymer Polymers 0.000 description 1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1431—Pretreatment by other processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/343—Heat recovery
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20478—Alkanolamines
- B01D2252/20484—Alkanolamines with one hydroxyl group
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Environmental & Geological Engineering (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a flue gas waste heat recovery device and method coupled with carbon capture, which comprises a desulfurizing tower, a flash tank, an absorption tower and a desorption tower, wherein a flue gas outlet arranged on the desulfurizing tower is connected with a flue gas inlet arranged on the absorption tower; a slurry outlet arranged on the desulfurizing tower is connected with a slurry inlet arranged on the flash tank; a rich liquid outlet arranged on the absorption tower is connected with a rich liquid inlet arranged on the desorption tower; a barren liquor outlet arranged on the desorption tower is connected with a barren liquor inlet arranged on the absorption tower; a slurry outlet arranged on the flash tank is connected with a slurry inlet arranged on the desulfurizing tower; a flue gas outlet is formed in the absorption tower; the invention can effectively reduce the consumption of the steam of the power plant in the MEA regeneration process, thereby reducing the regeneration energy consumption and effectively reducing the temperature of the flue gas discharged by the desulfurizing tower.
Description
Technical Field
The invention belongs to the field of environment, and particularly relates to a flue gas waste heat recovery device and method coupled with carbon capture.
Background
Climate warming has attracted a close global attention, CO 2 Is one of the most prominent greenhouse gases in the atmosphere. As a key industry for carbon dioxide emission, the flue gas tail gas of each thermal power plant in the power industry contains a large amount of carbon dioxide, and is directly discharged to the atmosphere in the current process flow. Along with the establishment of the national carbon emission right trading market, the carbon emission is comprehensively and directly related to the economic benefits of enterprises, and CO is captured 2 The demand of (2) is gradually coming up.
The MEA monoethanolamine method is a common method for capturing CO2, regeneration circulation is realized through absorption and desorption of MEA, but a high-temperature heat source is required in the regeneration process, and a steam extraction of a steam turbine of a power plant is generally adopted, so that the overall energy consumption of the technology is high. Meanwhile, the flue gas temperature at the outlet of the wet desulphurization tower of the coal-fired power plantHigher than the requirement of MEA process on the flue gas temperature, CO 2 The absorption rate is low.
For a cogeneration unit, recovering the waste heat in the system is one of the best ways to increase the heating capacity without enlarging the unit size. At present, the flue gas is generally discharged after being cooled to 50-60 ℃ by adopting a water spraying method in a power plant, and the heat in the flue gas is not recovered, so that the energy waste is caused.
CN 109454620A discloses a carbon capture and waste heat recovery coupling device, which utilizes an absorption tower and a desorption tower to realize CO in high-temperature flue gas discharged by industry 2 The collection and storage of the waste heat and the recovery of a certain waste heat are carried out. However, in the scheme, the utilization of the waste heat of the flue gas is rough, the flue gas temperature of the absorption tower is high, and CO is generated 2 The absorption rate is low.
Disclosure of Invention
The invention aims to provide a flue gas waste heat recovery device and method coupled with carbon capture, which solve the problems that the prior art can achieve a certain purpose of waste heat recovery, but the heat recovery rate is low, and simultaneously, the flue gas temperature at the inlet of an absorption tower is high and CO is generated in the prior art 2 Low absorption rate.
In order to achieve the purpose, the invention adopts the technical scheme that:
the invention provides a flue gas waste heat recovery device coupled with carbon capture, which comprises a desulfurizing tower, a flash tank, an absorption tower and a desorption tower, wherein a flue gas outlet arranged on the desulfurizing tower is connected with a flue gas inlet arranged on the absorption tower; a slurry outlet arranged on the desulfurizing tower is connected with a slurry inlet arranged on the flash tank;
a rich liquid outlet arranged on the absorption tower is connected with a rich liquid inlet arranged on the desorption tower;
a barren liquor outlet arranged on the desorption tower is connected with a barren liquor inlet arranged on the absorption tower;
a slurry outlet arranged on the flash tank is connected with a slurry inlet arranged on the desulfurizing tower;
and a flue gas outlet is formed in the absorption tower.
Preferably, a heat exchange unit is arranged between the absorption tower and the desorption tower.
Preferably, a steam outlet arranged on the flash tank is connected with a steam inlet arranged on the heat exchange unit.
Preferably, the connection unit comprises a lean-rich liquid heat exchanger and an absorption heat pump, wherein a rich liquid outlet on the absorption tower is connected with a rich liquid inlet on the desorption tower through the lean-rich liquid heat exchanger and the absorption heat pump in sequence.
Preferably, the connection unit further comprises a lean liquid cooler, wherein the lean liquid outlet on the desorption tower is connected with the lean liquid inlet on the absorption tower through the lean-rich liquid heat exchanger and the lean liquid cooler in sequence.
Preferably, the absorption heat pump is provided with a driving steam inlet and a first condensed water outlet, and the first condensed water outlet is connected with the clean water tank.
Preferably, the absorption heat pump is provided with a second condensate outlet.
Preferably, a carbon dioxide outlet arranged on the desorption tower is connected with a gas inlet on the condenser; the condenser is provided with a gas outlet and a liquid outlet, and the liquid outlet is connected with a liquid inlet arranged on the desorption tower.
A method for recovering flue gas waste heat by coupling carbon capture comprises the following steps:
the flue gas enters a desulfurizing tower to exchange heat with low-temperature desulfurizing slurry sprayed from the top of the tower and is purified, and the flue gas is cooled and humidified;
enabling the high-temperature desulfurization slurry at the bottom of the desulfurization tower to enter a flash tank to generate flash steam and low-temperature desulfurization slurry, and transferring heat from the desulfurization slurry to the flash steam;
the saturated wet flue gas purified from the desulfurizing tower enters an absorption tower to be in countercurrent contact with MEA barren solution sprayed from the top of the tower, CO in the flue gas is absorbed, and the flue gas after the CO is absorbed is discharged from the top of the absorption tower;
the MEA rich solution is discharged from the bottom of the absorption tower and enters a desorption tower to be desorbed; and the desorbed MEA barren solution enters an absorption tower for circulation.
Compared with the prior art, the invention has the beneficial effects that:
the flue gas waste heat recovery device and method coupled with carbon capture provided by the invention have the advantages that the temperature of the desulfurization slurry is reduced through flash evaporation of the desulfurization slurry, so that the temperature of flue gas discharged by a desulfurization tower is reduced to about 40 ℃, and the aim that MEA absorbs CO is achieved 2 The optimum temperature of the water-soluble polymer improves the absorption rate; by means of desulfurization slurry flash evaporation, the heat of the flue gas is actually recovered, and the part of heat is upgraded by an absorption heat pump and then is used for heating the MEA rich solution, so that the consumption of the power plant steam in the MEA regeneration process can be effectively reduced, and the regeneration energy consumption is reduced.
Drawings
Fig. 1 is a schematic structural view of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings.
The invention provides a flue gas waste heat recovery device for coupling carbon capture, which comprises a desulfurizing tower 1, a flash tank 4, an absorption tower 2 and a desorption tower 3, wherein a flue gas outlet arranged on the desulfurizing tower 1 is connected with a flue gas inlet arranged on the absorption tower 2; a slurry outlet arranged on the desulfurizing tower 1 is connected with a slurry inlet arranged on the flash tank 4;
a rich liquid outlet arranged on the absorption tower 2 is connected with a rich liquid inlet arranged on the desorption tower 3;
a barren liquor outlet arranged on the desorption tower 3 is connected with a barren liquor inlet arranged on the absorption tower 2;
a slurry outlet arranged on the flash tank 4 is connected with a slurry inlet arranged on the desulfurizing tower 1;
and a flue gas outlet is formed in the absorption tower 2.
The invention provides a flue gas waste heat recovery method coupled with carbon capture, which comprises the following steps:
the flue gas 9 enters the desulfurizing tower 1 to exchange heat with low-temperature desulfurizing slurry 12 sprayed from the top of the tower and is purified, and the flue gas is cooled and humidified;
enabling the high-temperature desulfurization slurry 10 at the bottom of the desulfurization tower 1 to enter a flash tank 4 to generate flash steam 13 and low-temperature desulfurization slurry 12, and transferring heat from the desulfurization slurry to the flash steam;
purified from the desulfurizing tower 1The saturated wet flue gas 11 enters the absorption tower 2 to be in countercurrent contact with MEA lean solution sprayed from the top of the tower, and CO in the flue gas 2 Is absorbed, CO 2 The absorbed flue gas 18 is discharged from the top of the absorption tower;
the MEA rich solution 17 is discharged from the bottom of the absorption tower 2 and enters the desorption tower 3 for desorption; the desorbed MEA lean solution 20 enters the absorption tower 2 to be circulated.
As shown in fig. 1, the flue gas waste heat recovery device with coupled carbon capture provided by the invention comprises a desulfurizing tower 1, an absorption tower 2, a desorption tower 3, a flash tank 4, an absorption heat pump 5, a lean-rich liquid heat exchanger 6, a lean liquid cooler 7, a condenser 8, flue gas 9, high-temperature desulfurization slurry 10, saturated wet flue gas 11, low-temperature desulfurization slurry 12, flash steam 13, condensed water 14, driving steam 15, condensed water 16, MEA rich liquid 17, flue gas 18, high-temperature rich liquid 19, MEA lean liquid 20, rich CO 2 Gas 21 and high purity CO 2 22, wherein the desulfurizing tower 1 is provided with a flue gas inlet and a flue gas outlet, and the flue gas outlet absorption tower 2 is provided with a flue gas inlet; a slurry outlet formed in the desulfurizing tower 1 is connected with a slurry inlet formed in the flash tank 4; and a slurry outlet arranged on the flash tank 4 is connected with a slurry inlet arranged on the desulfurizing tower 1.
And a steam outlet formed in the flash tank 4 is connected with a steam inlet on the absorption heat pump 5.
The absorption heat pump 5 is provided with a driving steam inlet and a first condensate outlet, and the first condensate outlet is connected with a water purifying tank.
And a second condensate water outlet is arranged on the absorption heat pump 5.
An MEA rich liquid outlet arranged on the absorption tower 2 is connected with an MEA rich liquid inlet on the desorption tower 3 through a lean-rich liquid heat exchanger 6 and an absorption heat pump 5 in sequence.
An MEA lean solution outlet on the desorption tower 3 is connected with an MEA lean solution inlet arranged on the absorption tower 2 through a lean-rich solution heat exchanger 6 and a lean solution cooler 7 in sequence.
And a flue gas outlet is formed in the absorption tower 2.
And a carbon dioxide outlet arranged on the desorption tower 3 is connected with a gas inlet arranged on a condenser 8.
And a liquid outlet arranged on the condenser 8 is connected with a liquid inlet arranged on the desorption tower 3.
And a gas outlet is arranged on the condenser 8.
The working principle of the invention is as follows:
the flue gas 9 enters the desulfurizing tower 1 to exchange heat with the low-temperature desulfurizing slurry 12 sprayed from the top of the tower and is purified, and the temperature of the flue gas is reduced and the flue gas is humidified. The high-temperature desulfurization slurry 10 at the bottom of the desulfurization tower enters a flash tank 4 and is flashed in a vacuum environment to generate flash steam 13 and low-temperature desulfurization slurry 12, and heat is transferred from the desulfurization slurry to the flash steam.
The flash steam 13 enters an absorption heat pump 5, and is upgraded by using driving steam 15, and the MEA rich solution is heated.
The driving steam is condensed in the heat pump to form condensed water 16 which returns to the clean water tank, and the flash steam 13 is condensed to form condensed water 14 which is used as the desulfurization water supplement.
The purified saturated wet flue gas 11 enters an absorption tower 2 to be in countercurrent contact with MEA barren solution sprayed from the top of the tower, and CO in the flue gas 2 Is absorbed, CO 2 The absorbed flue gas 18 is discharged from the top of the absorption tower.
The MEA rich solution 17 is discharged from the bottom of the absorption tower, is heated by the lean-rich solution heat exchanger 6, enters the heat pump 5, is further heated to high-temperature rich solution 19, and enters the desorption tower 3 for desorption.
The desorbed MEA lean solution 20 enters the absorption tower for circulation after being cooled by the lean-rich solution heat exchanger and the lean solution cooler 7. Desorbed CO-rich gas 2 The gas 21 is discharged from the top of the tower, enters a condenser for gas-liquid separation and is further compressed to obtain high-purity CO 2 22。
The invention reduces the temperature of the desulfurization slurry through flash evaporation of the desulfurization slurry, thereby reducing the temperature of the flue gas discharged by the desulfurization tower to about 40 ℃, achieving the optimal temperature for absorbing CO2 by MEA, and improving the absorption rate. By means of desulfurization slurry flash evaporation, the heat of the flue gas is actually recovered, and the part of heat is upgraded by an absorption heat pump and then is used for heating the MEA rich solution, so that the consumption of the power plant steam in the MEA regeneration process can be effectively reduced, and the regeneration energy consumption is reduced.
Claims (9)
1. The flue gas waste heat recovery device for coupling carbon capture is characterized by comprising a desulfurizing tower (1), a flash tank (4), an absorption tower (2) and a desorption tower (3), wherein a flue gas outlet arranged on the desulfurizing tower (1) is connected with a flue gas inlet arranged on the absorption tower (2); a slurry outlet arranged on the desulfurizing tower (1) is connected with a slurry inlet arranged on the flash tank (4);
a rich liquid outlet arranged on the absorption tower (2) is connected with a rich liquid inlet arranged on the desorption tower (3);
a barren liquor outlet arranged on the desorption tower (3) is connected with a barren liquor inlet arranged on the absorption tower (2);
a slurry outlet arranged on the flash tank (4) is connected with a slurry inlet arranged on the desulfurizing tower (1);
and a flue gas outlet is formed in the absorption tower (2).
2. The flue gas waste heat recovery device coupled with carbon capture as claimed in claim 1, characterized in that a heat exchange unit is arranged between the absorption tower (2) and the desorption tower (3).
3. The flue gas waste heat recovery device coupled with carbon capture as claimed in claim 2, wherein the steam outlet arranged on the flash tank (4) is connected with the steam inlet arranged on the heat exchange unit.
4. The coupled carbon capture flue gas waste heat recovery device is characterized in that the connecting unit comprises a lean-rich liquid heat exchanger (6) and an absorption heat pump (5), wherein a rich liquid outlet on the absorption tower (2) is connected with a rich liquid inlet on the desorption tower (3) through the lean-rich liquid heat exchanger (6) and the absorption heat pump (5) in sequence.
5. The carbon capture-coupled flue gas waste heat recovery device according to claim 4, wherein the connection unit further comprises a lean liquid cooler (7), wherein a lean liquid outlet on the desorption tower (3) is connected with a lean liquid inlet on the absorption tower (2) through the lean-rich liquid heat exchanger (6) and the lean liquid cooler (7) in sequence.
6. The coupled carbon capture flue gas waste heat recovery device according to claim 4, wherein the absorption heat pump (5) is provided with a driving steam inlet and a first condensed water outlet, and the first condensed water outlet is connected with a water purification tank.
7. The coupled carbon capture flue gas waste heat recovery device is characterized in that the absorption heat pump (5) is provided with a second condensate water outlet.
8. The flue gas waste heat recovery device coupled with carbon capture as claimed in claim 4, wherein a carbon dioxide outlet arranged on the desorption tower (3) is connected with a gas inlet on a condenser (8); the condenser (8) is provided with a gas outlet and a liquid outlet, and the liquid outlet is connected with a liquid inlet arranged on the desorption tower (3).
9. A method for recovering flue gas waste heat by coupling carbon capture is characterized by comprising the following steps:
the flue gas (9) enters a desulfurizing tower (1) to exchange heat with low-temperature desulfurizing slurry (12) sprayed from the top of the tower and is purified, and the flue gas is cooled and humidified;
enabling the high-temperature desulfurization slurry (10) at the bottom of the desulfurization tower (1) to enter a flash tank (4) to generate flash steam (13) and low-temperature desulfurization slurry (12), and transferring heat from the desulfurization slurry to the flash steam;
the saturated wet flue gas (11) purified from the desulfurizing tower (1) enters the absorption tower (2) to be in countercurrent contact with MEA barren solution sprayed from the top of the tower, and CO in the flue gas 2 Is absorbed, CO 2 The absorbed flue gas (18) is discharged from the top of the absorption tower;
the MEA rich solution (17) is discharged from the bottom of the absorption tower (2) and enters a desorption tower (3) for desorption; and the desorbed MEA lean solution (20) enters the absorption tower (2) for circulation.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202210609341.3A CN114963218A (en) | 2022-05-31 | 2022-05-31 | Flue gas waste heat recovery device and method coupled with carbon capture |
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| CN202210609341.3A CN114963218A (en) | 2022-05-31 | 2022-05-31 | Flue gas waste heat recovery device and method coupled with carbon capture |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115138181A (en) * | 2022-05-31 | 2022-10-04 | 华能营口热电有限责任公司 | Energy-saving and water-saving carbon capture device and method |
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| CN110425902A (en) * | 2019-08-26 | 2019-11-08 | 华能国际电力股份有限公司 | Flue gas waste heat recycling system and method after wet desulphurization |
| US20200061525A1 (en) * | 2017-04-12 | 2020-02-27 | Anemos Company Ltd. | Apparatus and method for recovering carbon dioxide in combustion exhaust gas |
| CN111729483A (en) * | 2020-07-23 | 2020-10-02 | 中国华电科工集团有限公司 | Carbon dioxide capture system and method |
| CN218544490U (en) * | 2022-05-31 | 2023-02-28 | 华能营口热电有限责任公司 | Flue gas waste heat recovery device of coupling carbon entrapment |
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