CN114797387A - Flue gas deep carbon capture device and method for recovering waste heat - Google Patents
Flue gas deep carbon capture device and method for recovering waste heat Download PDFInfo
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- CN114797387A CN114797387A CN202210612006.9A CN202210612006A CN114797387A CN 114797387 A CN114797387 A CN 114797387A CN 202210612006 A CN202210612006 A CN 202210612006A CN 114797387 A CN114797387 A CN 114797387A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 85
- 239000003546 flue gas Substances 0.000 title claims abstract description 82
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 31
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 31
- 239000002918 waste heat Substances 0.000 title claims abstract description 26
- 238000000034 method Methods 0.000 title claims abstract description 16
- 238000010521 absorption reaction Methods 0.000 claims abstract description 83
- 239000002002 slurry Substances 0.000 claims abstract description 51
- 239000007788 liquid Substances 0.000 claims abstract description 44
- 238000003795 desorption Methods 0.000 claims abstract description 36
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 25
- 239000007789 gas Substances 0.000 claims abstract description 20
- 238000006477 desulfuration reaction Methods 0.000 claims description 29
- 230000023556 desulfurization Effects 0.000 claims description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 18
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 16
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 8
- 239000001569 carbon dioxide Substances 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 5
- 229920006395 saturated elastomer Polymers 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims 6
- 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
- 238000000926 separation method Methods 0.000 description 3
- 238000005507 spraying Methods 0.000 description 2
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 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
- 239000012528 membrane Substances 0.000 description 1
- 230000000630 rising effect Effects 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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- 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
- 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
- B01D53/1412—Controlling the absorption process
-
- 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
- B01D53/1493—Selection of liquid materials for use as 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/343—Heat recovery
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B30/00—Heat pumps
- F25B30/04—Heat pumps of the sorption type
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D21/0001—Recuperative heat exchangers
- F28D21/0014—Recuperative heat exchangers the heat being recuperated from waste air or from vapors
-
- 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
Abstract
The invention provides a flue gas deep carbon capture device and method for recovering waste heat, which comprises a desulfurizing tower, a primary separator, a flash tank, an absorption tower and a desorption tower, wherein the desulfurizing tower is provided with a flue gas inlet and a flue gas outlet, and the flue gas outlet 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 through a primary separator; a gas outlet arranged on the primary separator is connected with a gas inlet arranged on the absorption tower; 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 flue gas outlet is formed in the absorption tower; the invention can improve the overall carbon capture rate of the flue gas, and can effectively reduce the consumption of the steam of a power plant in the MEA regeneration process, thereby reducing the regeneration energy consumption.
Description
Technical Field
The invention belongs to the field of environment, and particularly relates to a flue gas deep carbon capture device and method for recovering waste heat.
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 for (2) is gradually rising.
The MEA (monoethanolamine) method is a common method for capturing CO2, a regeneration cycle is realized through the 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 plant is higher than the requirement of the MEA (membrane electrode assembly) process on the flue gas temperature, and the CO2 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 upsizing the unit. 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. Meanwhile, a large amount of carbon dioxide also exists in the desulfurization slurry generated after spraying, so that the difficulty is increased for further capturing the carbon dioxide.
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 Low absorption rate and CO content in desulfurized slurry 2 Nor was trapping performed.
Disclosure of Invention
The invention aims to provide a flue gas deep carbon capture device and method for recovering waste heat, which solve the problem that the prior art can achieve a certain purpose of recovering the waste heat, but has lower heat recovery rate, and simultaneously, the flue gas temperature at the inlet of an absorption tower is high, and CO is high in the prior art 2 Low absorption rate and no carbon capture of the desulfurization slurry.
In order to achieve the purpose, the invention adopts the technical scheme that:
the invention provides a flue gas deep carbon capture device for recovering waste heat, which comprises a desulfurization tower, a primary separator, a flash tank, an absorption tower and a desorption tower, wherein the desulfurization tower is provided with a flue gas inlet and a flue gas outlet, and the flue gas outlet is connected with a flue gas inlet formed in the absorption tower; a slurry outlet arranged on the desulfurizing tower is connected with a slurry inlet arranged on the flash tank through a primary separator; a slurry outlet arranged on the flash tank is connected with a slurry inlet arranged on the desulfurizing tower;
a gas outlet arranged on the primary separator is connected with a gas inlet arranged on the absorption tower;
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;
and a flue gas outlet is formed in the absorption tower.
Preferably, a heat exchange unit is arranged between a rich liquid outlet arranged on the absorption tower and a rich liquid inlet arranged on the desorption tower.
Preferably, a steam inlet arranged on the heat exchange unit is connected with a steam outlet arranged on the flash tank.
Preferably, the heat exchange unit comprises a lean-rich liquid heat exchanger and an absorption heat pump, wherein a rich liquid outlet arranged on the absorption tower is connected with a rich liquid inlet arranged on the desorption tower through the lean-rich liquid heat exchanger and the absorption heat pump in sequence;
and a barren liquor outlet arranged on the desorption tower is connected with a barren liquor inlet arranged on the absorption tower through a barren-rich liquor heat exchanger.
Preferably, a steam outlet arranged on the flash tank is connected with a steam inlet arranged on the absorption heat pump.
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 outlet 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 on the desorption tower.
A deep carbon capture method for flue gas by recovering waste heat 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;
the high-temperature desulfurization slurry at the bottom of the desulfurization tower enters a primary gas-liquid separator to remove CO 2 Release of CO 2 Carrying a small amount of water to enter an absorption tower;
CO removal 2 The desulfurization slurry enters a flash tank to generate flash steam and low-temperature desulfurization slurry, and heat is transferred 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, and CO in the flue gas 2 Is absorbed, CO 2 The absorbed flue gas 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:
according to the flue gas deep carbon capture device for recovering waste heat, 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 MEA rich solution, so that the consumption of power plant steam in the MEA regeneration process can be effectively reduced, and the regeneration energy consumption is reduced; by flashing the desulphurised slurry in two stages, the predominant CO is separated in the first stage primary gas-liquid separation stage 2 And releasing the carbon, realizing the capture of carbon in the desulfurization slurry and improving the overall carbon capture rate of the flue gas.
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 deep carbon capture device for recovering waste heat, which comprises a desulfurizing tower 1, a primary separator 4, a flash tank 5, an absorption tower 2 and a desorption tower 3, wherein the desulfurizing tower 1 is provided with a flue gas inlet and a flue gas outlet, and the flue gas outlet 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 5 through a primary separator 4; a slurry outlet arranged on the flash tank 5 is connected with a slurry inlet arranged on the desulfurizing tower 1;
a gas outlet arranged on the primary separator 4 is connected with a gas inlet arranged on the absorption tower 2;
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;
and a flue gas outlet is formed in the absorption tower 2.
The invention provides a flue gas deep carbon capture method for recovering waste heat, 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;
the high-temperature desulfurization slurry 10 at the bottom of the desulfurization tower 1 enters a primary gas-liquid separator 4 to separate CO 2 Release of CO 2 Carrying a small amount of water to enter an absorption tower 2;
CO removal 2 The desulfurized slurry enters a flash tank 5 to generate flash steam 13 and low-temperature desulfurized slurry 12, and heat is transferred from the desulfurized 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 and enters the desorption tower 3 for desorption; the desorbed MEA lean solution 20 enters the absorption tower 2 for circulation.
As shown in fig. 1, the flue gas deep carbon capture device for recovering waste heat provided by the invention comprises a desulfurization tower 1, an absorption tower 2, a desorption tower 3, a primary gas-liquid separator 4, a flash tank 5, an absorption heat pump 6, a lean-rich liquid heat exchanger 7 and a condenser 8, wherein a flue gas inlet and a flue gas outlet are formed in the desulfurization tower 1, and the flue gas outlet is connected with a flue gas inlet formed in the absorption tower 2.
And a slurry outlet formed in the desulfurizing tower 1 is connected with a slurry inlet formed in the primary gas-liquid separator 4.
And a gas outlet formed in the primary gas-liquid separator 4 is connected with a gas inlet formed in the absorption tower 2.
And a slurry outlet arranged on the primary gas-liquid separator 4 is connected with a slurry inlet on the flash tank 5.
And a steam outlet formed in the flash tank 5 is connected with a steam inlet formed in the absorption heat pump 6.
The absorption heat pump 6 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 6.
The rich liquid outlet arranged on the absorption tower 2 is connected with the rich liquid inlet arranged on the desorption tower 3 through a lean-rich liquid heat exchanger 7 and an absorption heat pump 6 in sequence.
A barren liquor outlet arranged on the desorption tower 3 is connected with a barren liquor inlet arranged on the absorption tower 2 through a barren-rich liquor heat exchanger 7.
And a gas outlet formed in the desorption tower 3 is connected with a gas inlet formed in the 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.
And a flue gas outlet is formed in the absorption tower 2.
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 primary gas-liquid separator 4, and CO in the desulfurization slurry is subjected to vacuum of about 20kPa absolute pressure 2 Released and carries a small amount of water into the absorption tower 2.
CO removal 2 Enters the flash tank 5 and is flashed in a vacuum environment at a lower pressure to produce flash steam 13 and low temperature desulphurised slurry 12, heat being transferred from the desulphurised 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. Driving the steam to condense in the heat pump to form condensed water 16 which returns to the water purifying tank; the flash steam 13 is condensed into condensed water 14 which is used as the water for desulfurization.
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 7, enters the absorption heat pump 6, 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 2 for circulation after being cooled by the lean-rich solution heat exchanger 7.
Desorbed CO-rich gas 2 The gas 21 is discharged from the top of the tower, enters a condenser 8 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 ℃, and achieving the purpose that MEA absorbs CO 2 The optimum temperature of the water-absorbing agent is improved.
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. By flashing the desulphurised slurry in two stages, the predominant CO is separated in the first stage primary gas-liquid separation stage 2 And releasing the carbon, realizing the capture of carbon in the desulfurization slurry and improving the overall carbon capture rate of the flue gas.
Claims (9)
1. The deep carbon capture device for flue gas capable of recycling waste heat is characterized by comprising a desulfurizing tower (1), a primary separator (4), a flash tank (5), an absorption tower (2) and a desorption tower (3), wherein the desulfurizing tower (1) is provided with a flue gas inlet and a flue gas outlet, and the flue gas outlet is connected with the flue gas inlet formed in the absorption tower (2); a slurry outlet arranged on the desulfurizing tower (1) is connected with a slurry inlet arranged on the flash tank (5) through a primary separator (4);
a slurry outlet arranged on the flash tank (5) is connected with a slurry inlet arranged on the desulfurizing tower (1);
a gas outlet arranged on the primary separator (4) is connected with a gas inlet arranged on the absorption tower (2);
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);
and a flue gas outlet is formed in the absorption tower (2).
2. The deep carbon capture device for flue gas recycling waste heat according to claim 1, wherein a heat exchange unit is arranged between a rich liquid outlet arranged on the absorption tower (2) and a rich liquid inlet arranged on the desorption tower (3).
3. The deep carbon capture device for flue gas recycling waste heat according to claim 2, wherein a steam inlet arranged on the heat exchange unit is connected with a steam outlet arranged on the flash tank (5).
4. The deep flue gas carbon capture device for waste heat recovery according to claim 2, wherein the heat exchange unit comprises a lean-rich liquid heat exchanger (7) and an absorption heat pump (6), wherein a rich liquid outlet arranged on the absorption tower (2) is connected with a rich liquid inlet arranged on the desorption tower (3) through the lean-rich liquid heat exchanger (7) and the absorption heat pump (6) in sequence;
a barren liquor outlet arranged on the desorption tower (3) is connected with a barren liquor inlet arranged on the absorption tower (2) through a barren-rich liquor heat exchanger (7).
5. The deep carbon capture device for flue gas recycling waste heat according to claim 4, characterized in that a steam outlet arranged on the flash tank (5) is connected with a steam inlet arranged on the absorption heat pump (6).
6. The deep carbon capture device for flue gas recycling waste heat according to claim 4, characterized in that the absorption heat pump (6) is provided with a driving steam inlet and a first condensed water outlet, and the first condensed water outlet is connected with a clean water tank.
7. The deep carbon capture device for flue gas with waste heat recovery as recited in claim 4, characterized in that the absorption heat pump (6) is provided with a second condensed water outlet.
8. The deep flue gas carbon capture device for recovering waste heat according to claim 4, wherein a carbon dioxide outlet arranged on the desorption tower (3) is connected with a gas outlet on the 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 on the desorption tower (3).
9. The deep carbon capture method for flue gas by recycling waste heat 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;
the high-temperature desulfurization slurry (10) at the bottom of the desulfurization tower (1) enters a primary gas-liquid separator (4) to remove CO 2 Release of CO 2 Carrying a small amount of water into an absorption tower (2);
removal of CO 2 The desulfurized slurry enters a flash tank (5) to generate flash steam (13) and low-temperature desulfurized slurry (12), and heat is transferred from the desulfurized slurry to the flash steam;
the saturated wet flue gas (11) purified from the desulfurizing tower (1) 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 and enters a desorption tower (3) for desorption; and the desorbed MEA lean solution (20) enters the absorption tower (2) for circulation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210612006.9A CN114797387A (en) | 2022-05-31 | 2022-05-31 | Flue gas deep carbon capture device and method for recovering waste heat |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210612006.9A CN114797387A (en) | 2022-05-31 | 2022-05-31 | Flue gas deep carbon capture device and method for recovering waste heat |
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| Publication Number | Publication Date |
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| CN114797387A true CN114797387A (en) | 2022-07-29 |
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| CN202210612006.9A Pending CN114797387A (en) | 2022-05-31 | 2022-05-31 | Flue gas deep carbon capture device and method for recovering waste heat |
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| CN (1) | CN114797387A (en) |
Citations (17)
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