CN110152457A - The chemical absorption method carbon dioxide capture system utilized based on Waste Heat Recovery - Google Patents
The chemical absorption method carbon dioxide capture system utilized based on Waste Heat Recovery Download PDFInfo
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- CN110152457A CN110152457A CN201910409729.7A CN201910409729A CN110152457A CN 110152457 A CN110152457 A CN 110152457A CN 201910409729 A CN201910409729 A CN 201910409729A CN 110152457 A CN110152457 A CN 110152457A
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- absorption tower
- desorber
- gas
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 255
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 217
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 115
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 108
- 238000000034 method Methods 0.000 title claims abstract description 50
- 239000002918 waste heat Substances 0.000 title claims abstract description 49
- 239000000126 substance Substances 0.000 title claims abstract description 47
- 238000011084 recovery Methods 0.000 title claims abstract description 36
- 239000007788 liquid Substances 0.000 claims abstract description 251
- 230000002745 absorbent Effects 0.000 claims abstract description 119
- 239000002250 absorbent Substances 0.000 claims abstract description 119
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 107
- 239000003546 flue gas Substances 0.000 claims abstract description 107
- 238000009835 boiling Methods 0.000 claims abstract description 47
- 238000010438 heat treatment Methods 0.000 claims abstract description 27
- 238000003795 desorption Methods 0.000 claims abstract description 21
- 239000007921 spray Substances 0.000 claims abstract description 21
- 230000002411 adverse Effects 0.000 claims abstract description 11
- 238000005406 washing Methods 0.000 claims description 118
- 238000005201 scrubbing Methods 0.000 claims description 83
- 239000007789 gas Substances 0.000 claims description 44
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 42
- 238000001816 cooling Methods 0.000 claims description 25
- 239000003795 chemical substances by application Substances 0.000 claims description 20
- 238000000746 purification Methods 0.000 claims description 18
- 230000008569 process Effects 0.000 claims description 10
- 229920006395 saturated elastomer Polymers 0.000 claims description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- 229910052799 carbon Inorganic materials 0.000 claims description 8
- 230000008859 change Effects 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 7
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical group [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 6
- 241000790917 Dioxys <bee> Species 0.000 claims description 5
- 238000007701 flash-distillation Methods 0.000 claims description 5
- 230000009471 action Effects 0.000 claims description 4
- 235000019504 cigarettes Nutrition 0.000 claims description 4
- 238000004090 dissolution Methods 0.000 claims description 4
- 239000002253 acid Substances 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 230000004044 response Effects 0.000 claims description 3
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 3
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 3
- 125000003277 amino group Chemical group 0.000 claims description 2
- 239000003500 flue dust Substances 0.000 claims description 2
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims description 2
- 238000005086 pumping Methods 0.000 claims description 2
- GCNLQHANGFOQKY-UHFFFAOYSA-N [C+4].[O-2].[O-2].[Ti+4] Chemical compound [C+4].[O-2].[O-2].[Ti+4] GCNLQHANGFOQKY-UHFFFAOYSA-N 0.000 claims 1
- 229960004424 carbon dioxide Drugs 0.000 description 72
- 150000001412 amines Chemical class 0.000 description 16
- 238000005265 energy consumption Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 238000010025 steaming Methods 0.000 description 2
- 235000010215 titanium dioxide Nutrition 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- SOQBVABWOPYFQZ-UHFFFAOYSA-N oxygen(2-);titanium(4+) Chemical class [O-2].[O-2].[Ti+4] SOQBVABWOPYFQZ-UHFFFAOYSA-N 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000004577 thatch Substances 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
Classifications
-
- 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
- B01D53/1456—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
-
- 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
- F25B30/02—Heat pumps of the compression type
-
- 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
- F25B41/00—Fluid-circulation arrangements
- F25B41/30—Expansion means; Dispositions thereof
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
- F28C3/00—Other direct-contact heat-exchange apparatus
- F28C3/06—Other direct-contact heat-exchange apparatus the heat-exchange media being a liquid and a gas or vapour
-
- 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
-
- 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
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The present invention provides a kind of chemical absorption method carbon dioxide capture systems utilized based on Waste Heat Recovery comprising absorption tower, rich solution pump, the first poor rich liquid heat exchanger, rich solution current divider, the second poor rich liquid heat exchanger, heat pump system, desorber, boiling device, lean pump and lean solution cooler.Flue gas enters absorption tower and moves from the bottom up, and absorbent enters in absorption tower and sprays down, and absorbent is contacted with flue gas adverse current, so that absorbent absorbs the carbon dioxide in flue gas and becomes rich solution；Rich solution enters rich solution pump, subsequently into the first poor rich liquid heat exchanger with heating of absorbing heat；The rich solution for completing the first heat exchange enters to be split into two-way in rich solution current divider, and first via rich solution enters heat pump system with heating of absorbing heat, and then first via rich solution enters desorber；Second road rich solution enters the second poor rich liquid heat exchanger with heating of absorbing heat, and then the second road rich solution carries out desorber；First via rich solution and the second road rich solution are heated desorption in desorber and are decomposed into lean solution and carbon dioxide.
Description
Technical field
The present invention relates to field of waste heat recovery more particularly to a kind of chemical absorption method titanium dioxides utilized based on Waste Heat Recovery
Carbon capture system.
Background technique
Due to a large amount of burnings of fossil fuel, CO in atmosphere2Content also constantly rise, a large amount of CO2Discharge lead to greenhouse
Effect is increasingly severe, controls CO2Discharge amount have become various countries' focus of attention.
Organic amine capture CO2Technology is technology most mature at present.Organic amine capture CO2Principle and process are as follows: in flue gas
CO2It is reacted on absorption tower with organic amine and generates carbaminate, and be transported to desorber heat resolve and be reduced to organic amine
And carbon dioxide, Amine Solutions return to absorption tower and are absorbed again.Organic amine carbon capture method traps CO2Process is because of its absorption
Rate is fast, absorption efficiency is high and simple process, technology is more mature and is widely used；But organic amine capture CO2Technology energy
Consume higher, and how the waste heat in lean solution and gas that desorber desorbs is carried out recycling is the main way for reducing energy consumption
Diameter and the main foothold of energy saving technique exploitation.
Summary of the invention
In view of the problems in the background art, the purpose of the present invention is to provide a kind of changes utilized based on Waste Heat Recovery
Absorption process carbon dioxide capture system is learned, the heat for the gas that desorber top row goes out can be efficiently used to heat rich solution, mentioned
The utilization rate of high waste heat reduces heat required when rich solution desorption.
To achieve the goals above, the present invention provides a kind of chemical absorption method carbon dioxide utilized based on Waste Heat Recovery
Trapping system comprising absorption tower, rich solution pump, the first poor rich liquid heat exchanger, rich solution current divider, the second poor rich liquid heat exchanger, heat
Pumping system, desorber, boiling device, lean pump and lean solution cooler.Absorption tower includes: absorption tower first entrance, is located at and absorbs
The lower part of tower enters for flue gas, and flue gas has carbon dioxide；Absorption tower second entrance, positioned at the top on absorption tower, for absorbent
Into；Absorption tower first outlet is flowed out positioned at the bottom on absorption tower for rich solution；Absorption tower second outlet, positioned at the top on absorption tower
Portion.Rich solution pump includes: rich solution pump intake, is connected to absorption tower first outlet；Rich solution pump discharge.First poor rich liquid heat exchanger includes:
First poor rich liquid heat exchanger first entrance is connected to rich solution pump discharge；First poor rich liquid heat exchanger second entrance；First rich or poor liquid changes
Hot device first outlet；First poor rich liquid heat exchanger second outlet.Rich solution current divider includes: rich solution splitter inlet, connection first
Poor rich liquid heat exchanger first outlet；Rich solution current divider first outlet；Rich solution current divider second outlet.Second poor rich liquid heat exchanger packet
Include: the second poor rich liquid heat exchanger first entrance is connected to rich solution current divider second outlet；Second poor rich liquid heat exchanger second entrance；
Second poor rich liquid heat exchanger first outlet；Second poor rich liquid heat exchanger second outlet, connection the first poor rich liquid heat exchanger second enter
Mouthful.Heat pump system includes evaporator, compressor, condenser and throttle valve.Evaporator includes: evaporator first entrance；Evaporation
Device second entrance；Evaporator first outlet；Evaporator second outlet.Compressor includes: suction port of compressor, is connected to evaporator second
Outlet；Compressor outlet.Condenser includes: condenser first entrance, is connected to rich solution current divider first outlet；Condenser second enters
Mouthful, it is connected to compressor outlet；Condenser first outlet；Condenser second outlet.Throttle valve be set to condenser and evaporator it
Between, the controlled connection condenser second outlet in one end, the controlled connection evaporator second entrance of the other end.Desorber includes: desorber
First entrance is located at desorber top, is connected to condenser first outlet；Desorber second entrance, simultaneously positioned at the top of desorber
Lower than desorber first entrance, it is connected to the second poor rich liquid heat exchanger first outlet；Desorber third entrance, in desorber
Portion is simultaneously lower than desorber second entrance；The 4th entrance of desorber, positioned at desorber lower part and be lower than desorber third entrance；Solution
Tower first outlet is inhaled, is located at the top of desorber, evaporator first entrance is connected to；Desorber second outlet is located at desorption tower bottom；
Desorber third outlet, positioned at the lower part of desorber.Boiling device includes: boiling device first entrance, the outlet of connection desorber third；
Boiling device second entrance is flowed into for external saturated vapor；Boiling device first outlet is connected to the 4th entrance of desorber；Boiling device
Second outlet.Lean pump includes: lean solution pump intake, is connected to the first poor rich liquid heat exchanger second outlet；Lean solution pump discharge.Lean solution is cold
But device side is connected to lean solution pump discharge, and the other side is connected to absorption tower second entrance.
Wherein, flue gas enters in absorption tower via absorption tower first entrance and moves from the bottom up, and absorbent is via absorption
Tower second entrance enters in absorption tower and sprays down, and the absorbent sprayed down is contacted with flue gas adverse current, so that absorbent is inhaled
It receives the carbon dioxide in flue gas and becomes rich solution, rich solution settles downwards, and the flue gas for being stripped of carbon dioxide continues up；
Rich solution enters rich solution pump via absorption tower first outlet, rich solution pump intake, then via rich solution pump discharge, first poor
Rich solution heat exchanger first entrance, which enters, carries out the first heat exchange in the first poor rich liquid heat exchanger, with heating of absorbing heat；
The rich solution for completing the first heat exchange enters richness via the first poor rich liquid heat exchanger first outlet, rich solution splitter inlet
In liquid current divider, to be split into two-way,
First via rich solution enters in condenser via rich solution current divider first outlet, condenser first entrance to carry out second
Heat exchange and heating of absorbing heat complete the first via rich solution of the second heat exchange via condenser first outlet, desorber first entrance
Into in desorber；
Second road rich solution is rich or poor into second via rich solution current divider second outlet, the second poor rich liquid heat exchanger first entrance
Third heat exchange and heating of absorbing heat are carried out in liquid heat exchanger, the second road rich solution for completing third heat exchange is changed via the second rich or poor liquid
Hot device first outlet, desorber second entrance carry out in desorber；
First via rich solution and the second road rich solution are heated in desorber to be desorbed and is decomposed into lean solution and carbon dioxide, lean solution
It is settled downwards in desorber, carbon dioxide moves upwards；
The partially liq at desorber bottom is exported via desorber third, boiling device first entrance enters in boiling device, and with
The 4th heat exchange is carried out via the saturated vapor that boiling device second entrance flows into, the partially liq absorbs heat heating in boiling device
And be partially vaporized and entered in desorber by boiling device first outlet, the 4th entrance of desorber, it is the rich solution solution in desorber
It inhales and steam and heat is provided；Saturated vapor heat release cooling in boiling device becomes condensed water, and condensed water goes out via boiling device second
Mouth discharge；
The carbon dioxide moved upwards can carry part lean solution, then enter via desorber first outlet, evaporator first
Mouth enters carries out the 5th heat exchange with the worker quality liquid in evaporator in evaporator, worker quality liquid heat absorption heating becomes working medium and steams
Vapour, working substance steam enter in compressor via evaporator second outlet, suction port of compressor, and compressor presses working substance steam
Contracting, becomes superheated steam via compressed working substance steam increasing temperature and pressure, superheated steam is via compressor outlet, condenser second
Entrance enters in condenser, and carries out aforementioned second heat exchange with the first via rich solution flowed into via condenser first entrance, the
Rich solution heat absorption heating all the way, and superheated steam heat release cooling becomes high-pressure working medium liquid, high-pressure working medium liquid flows into throttle valve simultaneously
Be depressurized and become initial conditions worker quality liquid, worker quality liquid under the action of throttle valve via evaporator second entrance again
Into in evaporator, so that worker quality liquid completes one cycle use process；
The lean solution desorbed in desorber enters the via desorber second outlet, the second poor rich liquid heat exchanger second entrance
In two poor rich liquid heat exchangers, aforementioned third heat is carried out with the second road rich solution entered via the second poor rich liquid heat exchanger first entrance
Exchange, lean solution heat release cooling；
The lean solution of third heat exchange is completed via the second poor rich liquid heat exchanger second outlet, the first poor rich liquid heat exchanger second
Entrance enters in the first poor rich liquid heat exchanger, with the rich solution progress aforementioned the entered via the first poor rich liquid heat exchanger first entrance
One heat exchange, lean solution heat release cooling complete the lean solution of the first heat exchange via the first poor rich liquid heat exchanger second outlet, lean pump
Into being cooled again in lean solution cooler, then be cooled after lean solution via lean solution cooler, absorption tower second entrance into
Enter in absorption tower, is used using the absorbent as absorbing carbon dioxide.
In one embodiment, absorption tower further include: absorption tower third entrance, positioned at absorption tower middle part and be located at absorption tower
The lower section of second entrance；The outlet of absorption tower third, the middle part positioned at absorption tower and the top positioned at absorption tower third entrance.It is based on
The chemical absorption method carbon dioxide capture system that Waste Heat Recovery utilizes further includes interstage cooler, and side is connected to absorption tower third
Entrance, the other side are connected to the outlet of absorption tower third.Wherein, the absorbent in absorption tower is flowed into via the outlet of absorption tower third
To cool down in interstage cooler, the absorbent after cooling down via interstage cooler is via absorption tower third inlet return to suction
It receives in tower and sprays downwards, the absorbent sprayed downwards is contacted with the flue gas adverse current entered via absorption tower first entrance, is absorbed
Agent absorbs at least partly carbon dioxide in flue gas and becomes rich solution, and rich solution settles downwards；Removing at least partly carbon dioxide
Flue gas continue up and with via absorption tower second entrance spray and under absorbent counter current contacting and by via suction again
Receive tower second entrance spray and lower absorbent carries out the second secondary response and becomes the flue gas of rich solution and carbon dioxide removal, generation
Rich solution settle downwards, and the flue gas of carbon dioxide removal continues to move upwards, and the carbon dioxide removal moved upwards
Flue gas can carry and partially absorb agent.
In one embodiment, absorption tower further include: the 4th entrance of absorption tower, positioned at absorption tower top and be located at absorption tower
The top of second entrance；Absorption tower the 4th exports, the top positioned at absorption tower and the top positioned at absorption tower second entrance, for inhaling
Receive the washing water outflow being pre-stored in tower.The chemical absorption method carbon dioxide capture system utilized based on Waste Heat Recovery further includes one
Secondary washing pump and once washing cooler.Once washing pump includes: once washing pump intake, is connected to absorption tower the 4th and goes out
Mouthful；Once washing pump discharge.Once washing cooler side is connected to once washing pump discharge, and the other side is connected to absorption tower
Four entrances.Wherein, absorption tower, once washing pump, once washing cooler form once washing circuit, open when once washing pumps
Afterwards, the washing water in absorption tower is flowed into once washing pump via the outlet of absorption tower the 4th, once washing pump intake, is then passed through
It is flowed into once washing cooler and is cooled down by once washing pump discharge, washing water after cooling flows back into absorption tower again
Top and spray and under, carbon dioxide removal and carrying partially absorbs the flue gas of agent and moves upwards and be cooled in absorption tower
Washing water counter current contacting, at least partly absorbent in flue gas is dissolved in washing water, the flue gas after once washing after
Then continuous move upwards is discharged via absorption tower second outlet.
In one embodiment, it is also carried via the flue gas that absorption tower second outlet is discharged and partially absorbs agent.Based on waste heat
The chemical absorption method carbon dioxide capture system of recycling further includes the first gas-liquid separator, scrubbing tower, secondary washing pump, two
Secondary scrubber cooler, lean solution current divider, absorbent reservoir.First gas-liquid separator includes: the first gas-liquid separator entrance, even
Logical absorption tower second outlet；First gas-liquid separator first outlet, positioned at the bottom of the first gas-liquid separator；First gas-liquid separation
Device second outlet, positioned at the top of the first gas-liquid separator.Washing water is stored in scrubbing tower, scrubbing tower includes: scrubbing tower
One entrance, middle part and the first gas-liquid separator second outlet of connection positioned at scrubbing tower；Scrubbing tower second entrance is located at scrubbing tower
Top；Scrubbing tower first outlet, positioned at the top of scrubbing tower；Scrubbing tower second outlet, positioned at the lower part of scrubbing tower；Scrubbing tower
Third outlet, positioned at the bottom of scrubbing tower.Secondary washing pump includes: secondary washing pump intake, is connected to scrubbing tower second outlet；Two
Secondary washing pump discharge.Secondary washing cooler side is connected to secondary washing pump discharge, and the other side is connected to scrubbing tower second and enters
Mouthful.Lean solution current divider includes: lean solution current divider first entrance, is connected to the first gas-liquid separator first outlet；Lean solution current divider
Two entrances, the outlet of connection scrubbing tower third；The outlet of lean solution current divider.Absorbent reservoir includes: absorbent storage reservoir entrance,
It is connected to the outlet of lean solution current divider；The outlet of absorbent reservoir, is connected to the side of lean solution cooler.
Wherein, the carrying of absorption tower second outlet discharge partially absorb the flue gas of agent via the first gas-liquid separator entrance into
Entering in the first gas-liquid separator, the first gas-liquid separator will at least partly absorbent be separated with flue gas,
Flue gas is discharged via the first gas-liquid separator second outlet, and the flue gas of discharge still contains at least partly absorbent, contains
There is the flue gas of at least partly absorbent to enter in scrubbing tower and move upwards via scrubbing tower first entrance, the washing in scrubbing tower
Water enters in secondary washing pump via scrubbing tower second outlet, secondary washing pump intake, then via secondary washing pump discharge
It is flowed into secondary washing cooler and is cooled down, cooled washing water enters in scrubbing tower simultaneously via scrubbing tower second entrance
Spray and under, spray and lower washing water is contacted with the flue gas adverse current of carrying at least partly absorbent, the absorbent quilt in flue gas
Washing water dissolution, the flue gas for being stripped of absorbent is discharged via scrubbing tower first outlet, and the washing water dissolved with absorbent passes through
It is flowed into lean solution current divider by the outlet of scrubbing tower third, lean solution current divider second entrance；
The absorbent gone out via the first gas-liquid separator separates is via the first gas-liquid separator first outlet, lean solution current divider
First entrance is flowed into lean solution current divider；
Lean solution current divider mixes two-way absorbent, and mixed absorbent is exported via lean solution current divider, absorbed
Agent reservoir entrance enters in absorbent reservoir, then flows into absorption tower via the outlet of absorbent reservoir, lean solution cooler
In be re-circulated use.
It in one embodiment, further include flash distillation based on the chemical absorption method carbon dioxide capture system that Waste Heat Recovery utilizes
Tank, roots blower, steam condenser.Flash tank includes: flash tank entrance, is connected to desorber second outlet；Flash tank first goes out
Mouthful；Flash tank second outlet is connected to the second poor rich liquid heat exchanger second entrance.Roots blower includes: roots blower entrance, connection
Flash tank first outlet；Roots blower outlet.Steam condenser side is connected to roots blower outlet, and the other side is connected to desorption
Tower third entrance.
Directly enter in flash tank via flash tank entrance via the lean solution that desorber second outlet flows out, lean solution is flashing
The steam flashed off to flash off some vapor is flashed in tank to enter via flash tank first outlet, roots blower entrance
Roots blower, steam are pressurized heating in roots blower, then via roots blower outlet, into carrying out in steam condenser
Cooling, steam after cooling enters in desorber via desorber third entrance, auxiliary to provide for the rich solution desorption in desorber
The heat helped；Lean solution after flash distillation process enters second via flash tank second outlet, the second poor rich liquid heat exchanger second entrance
In poor rich liquid heat exchanger, aforementioned third heat is carried out with the second road rich solution entered via the second poor rich liquid heat exchanger first entrance and is handed over
It changes, lean solution heat release cooling.
It in one embodiment, further include purification based on the chemical absorption method carbon dioxide capture system that Waste Heat Recovery utilizes
Tower, self-fractionating pump, purification cooler.Cleanser is stored in purifying column, purifying column includes: purifying column first entrance, is located at purification
The lower part of tower enters for external flue gas；Purifying column second entrance, positioned at the top of purifying column；Purifying column first outlet is located at net
Change the top of tower, is connected to absorption tower first entrance；Purifying column second outlet, positioned at purifying column lower part and be located at purifying column first
The lower section of entrance.Self-fractionating pump includes: purification pump intake, is connected to purifying column second outlet；Purify pump discharge.Purify cooler side
Connection purification pump discharge, the other side is connected to purifying column second entrance.
Wherein, purifying column, self-fractionating pump, purification cooler form external gas cleaning circulation loop, after self-fractionating pump is opened,
Cleanser in purifying column be pumped into via the discharge of purifying column second outlet, via self-fractionating pump purification cooler cooled down, it
By by purifying column second entrance, back to spraying in purifying column and downwards, external flue gas enters only via purifying column first entrance
Change tower in and move upwards, the external flue gas moved upwards with via purifying column second entrance spray and under cleanser countercurrently connect
Touching, cleanser absorbs the acid impurities gas and flue dust in external flue gas, and the carbon dioxide in external flue gas is not cleaned
Agent absorbs, and flue gas moves upwards and enter in absorption tower via purifying column first outlet, absorption tower first entrance, with to absorption tower
Supply.
In one embodiment, cleanser is sodium bicarbonate solution.
In one embodiment, part lean solution is also carried from the carbon dioxide that desorber first outlet is discharged.Based on waste heat
The chemical absorption method carbon dioxide capture system of recycling further includes desorption gas condenser, the second gas-liquid separator.Stripping gas
Condenser includes: stripping gas condenser inlet, is connected to evaporator first outlet；Desorption device condensator outlet.Second gas-liquid separation
Device includes: the second gas-liquid separator entrance, is connected to stripping gas condensator outlet；Second gas-liquid separator first outlet is located at the
The top of two gas-liquid separators；Second gas-liquid separator second outlet, positioned at the bottom of the second gas-liquid separator.
Wherein, the carbon dioxide with part lean solution enters cold via evaporator first outlet, stripping gas condenser inlet
It is cooled down in condenser, enters second via the second gas-liquid separator entrance through the overcooled carbon dioxide with part lean solution
In gas-liquid separator, the carbon dioxide with part lean solution carries out gas-liquid separation via the second gas-liquid separator and is separated into dioxy
Change carbon products gas and lean solution, carbon dioxide product gas are discharged via the second gas-liquid separator first outlet, to carry out in next step
Operation；
The lean solution isolated is then refluxed in absorbent reservoir via the discharge of the second gas-liquid separator second outlet.
In one embodiment, absorbent is Amine Solutions.
Beneficial effects of the present invention are as follows: in the chemical absorption method titanium dioxide according to the present invention utilized based on Waste Heat Recovery
In carbon capture system, the heat transfer of the gas for being arranged effective by desorber top row out of heat pump system is to rich solution, so that rich
Liquid heat absorption heating reduces rich solution heat needed for desorber desorption, reduces energy consumption, improve the utilization rate of waste heat.
Detailed description of the invention
Fig. 1 is the signal of the chemical absorption method carbon dioxide capture system according to the present invention utilized based on Waste Heat Recovery
Figure.
Wherein, the reference numerals are as follows:
11 absorption tower 18B1 boiling device first outlets
The absorption tower 11A1 first entrance 18B2 boiling device second outlet
19 lean pump of the absorption tower 11A2 second entrance
The absorption tower 11A3 third entrance 19A lean solution pump intake
The 4th entrance 19B lean solution pump intake of the absorption tower 11A4
20 lean solution cooler of the absorption tower 11B1 first outlet
21 interstage cooler of the absorption tower 11B2 second outlet
The absorption tower 11B3 third exports 22 once washings pump
The absorption tower 11B4 the 4th exports 22A once washing pump intake
12 rich solution pump 22B once washing pump discharges
23 once washing cooler of 12A rich solution pump intake
24 first gas-liquid separator of 12B rich solution pump discharge
13 first poor rich liquid heat exchanger 24A the first gas-liquid separator entrances
The first the first gas-liquid separator of 2,4B1 first of the first poor rich liquid heat exchanger of 13A1 goes out
Entrance mouth
The 2nd the first gas-liquid separator of 2,4B2 second of the first poor rich liquid heat exchanger of 13A2 goes out
Entrance mouth
The one 25 scrubbing tower of the first poor rich liquid heat exchanger of 13B1
Export 25A1 scrubbing tower first entrance
The 2nd 25A2 scrubbing tower second entrance of the first poor rich liquid heat exchanger of 13B2
Export 25B1 scrubbing tower first outlet
14 rich solution current divider 25B2 scrubbing tower second outlets
The outlet of 14A rich solution splitter inlet 25B3 scrubbing tower third
26 secondary washing of 14B1 rich solution current divider first outlet pump
14B2 rich solution current divider second outlet 26A secondary washing pump intake
15 second poor rich liquid heat exchanger 26B secondary washing pump discharges
The one 27 secondary washing cooler of the second poor rich liquid heat exchanger of 15A1
28 lean solution current divider of entrance
The 2nd 28A1 lean solution current divider first entrance of the second poor rich liquid heat exchanger of 15A2
Entrance 28A2 lean solution current divider second entrance
The outlet of the first 28B lean solution current divider of the second poor rich liquid heat exchanger of 15B1
Export 29 absorbent reservoirs
The 2nd 29A absorbent of the second poor rich liquid heat exchanger of 15B2 stores up reservoir entrance
Export the outlet of 29B absorbent reservoir
16 heat pump system, 30 flash tank
161 evaporator 30A flash tank entrances
161A1 evaporator first entrance 30B1 flash tank first outlet
161A2 evaporator second entrance 30B2 flash tank second outlet
31 roots blower of 161B1 evaporator first outlet
161B2 evaporator second outlet 31A roots blower entrance
The outlet of 162 compressor 31B roots blowers
32 steam condenser of the suction port of compressor 162A
33 purifying column of 162B compressor outlet
163 condenser 33A1 purifying column first entrances
163A1 condenser first entrance 33A2 purifying column second entrance
163A2 condenser second entrance 33B1 purifying column first outlet
163B1 condenser first outlet 33B2 purifying column second outlet
34 self-fractionating pump of 163B2 condenser second outlet
164 throttle valve 34A purify pump intake
17 desorber 34B purify pump discharge
17A1 desorber first entrance 35 purifies cooler
17A2 desorber second entrance 36 desorbs gas condenser
17A3 desorber third entrance 36A stripping gas condenser inlet
The 4th entrance 36B desorption device condensator outlet of 17A4 desorber
37 second gas-liquid separator of 17B1 desorber first outlet
17B2 desorber second outlet 37A the second gas-liquid separator entrance
17B3 desorber third outlet the second gas-liquid separator of 3,7B1 first goes out
18 boiling device mouths
The second gas-liquid separator of 18A1 boiling device first entrance 3,7B2 second goes out
18A2 boiling device second entrance mouth
Specific embodiment
Referring to Fig.1, the chemical absorption method carbon dioxide capture system of the invention utilized based on Waste Heat Recovery includes absorbing
Tower 11, rich solution pump 12, the first poor rich liquid heat exchanger 13, rich solution current divider 14, the second poor rich liquid heat exchanger 15, heat pump system 16,
Desorber 17, boiling device 18, lean pump 19 and lean solution cooler 20.
Absorption tower 11 includes: absorption tower first entrance 11A1, positioned at the lower part on absorption tower 11, is entered for flue gas, flue gas band
There is carbon dioxide；Absorption tower second entrance 11A2 enters positioned at the top on absorption tower 11 for absorbent；Absorption tower first outlet
11B1 is flowed out positioned at the bottom on absorption tower 11 for rich solution；Absorption tower second outlet 11B2, positioned at the top on absorption tower 11.
Rich solution pump 12 includes: rich solution pump intake 12A, is connected to absorption tower first outlet 11B1；Rich solution pump discharge 12B.
First poor rich liquid heat exchanger 13 includes: the first poor rich liquid heat exchanger first entrance 13A1, is connected to rich solution pump discharge
12B；First poor rich liquid heat exchanger second entrance 13A2；First poor rich liquid heat exchanger first outlet 13B1；First rich or poor liquid heat exchange
Device second outlet 13B2.
Rich solution current divider 14 includes: rich solution splitter inlet 14A, is connected to the first poor rich liquid heat exchanger first outlet 13B1；
Rich solution current divider first outlet 14B1；Rich solution current divider second outlet 14B2.
Second poor rich liquid heat exchanger 15 includes: the second poor rich liquid heat exchanger first entrance 15A1, connection rich solution current divider the
Two outlet 14B2；Second poor rich liquid heat exchanger second entrance 15A2；Second poor rich liquid heat exchanger first outlet 15B1；Second is rich or poor
Liquid heat exchanger second outlet 15B2 is connected to the first poor rich liquid heat exchanger second entrance 13A2.
Heat pump system 16 includes evaporator 161, compressor 162, condenser 163 and throttle valve 164.
Evaporator 161 includes: evaporator first entrance 161A1；Evaporator second entrance 161A2；Evaporator first outlet
161B1；Evaporator second outlet 161B2.
Compressor 162 includes: suction port of compressor 162A, is connected to evaporator second outlet 161B2；Compressor outlet 162B.
Condenser 163 includes: condenser first entrance 163A1, is connected to rich solution current divider first outlet 14B1；Condenser
Two entrance 163A2 are connected to compressor outlet 162B；Condenser first outlet 163B1；Condenser second outlet 163B2.
Throttle valve 164 is set between condenser 163 and evaporator 161, the controlled connection condenser second outlet in one end
163B2, the controlled connection evaporator second entrance 161A2 of the other end.
Desorber 17 includes: desorber first entrance 17A1, is located at 17 top of desorber, is connected to condenser first outlet
163B1；Desorber second entrance 17A2, positioned at desorber 17 top and be lower than (preferably, the position desorber first entrance 17A1
In the middle and upper part of desorber 17), it is connected to the second poor rich liquid heat exchanger first outlet 15B1；Desorber third entrance 17A3, is located at
The middle part of desorber 17 is simultaneously lower than desorber second entrance 17A2 (middle and lower part for being preferably located at desorber 17)；Desorber
Four entrance 17A4, positioned at desorber 17 lower part and be lower than desorber third entrance 17A3；Desorber first outlet 17B1, is located at
17 top of desorber, is connected to evaporator first entrance 161A1；Desorber second outlet 17B2 is located at 17 bottom of desorber；Desorption
Tower third exports 17B3, positioned at the lower part of desorber 17.
Boiling device 18 includes: boiling device first entrance 18A1, and connection desorber third exports 17B3；Boiling device second entrance
18A2 is flowed into for external saturated vapor；Boiling device first outlet 18B1 is connected to the 4th entrance 17A4 of desorber；Boiling device
Two outlet 18B2.
Lean pump 19 includes: lean solution pump intake 19A, is connected to the first poor rich liquid heat exchanger second outlet 13B2；Lean solution pumps out
Mouth 19B.
20 side of lean solution cooler is connected to lean solution pump discharge 19B, and the other side is connected to absorption tower second entrance 11A2.
Wherein, flue gas enters in absorption tower 11 via absorption tower first entrance 11A1 and moves from the bottom up, absorbent warp
Being entered in absorption tower 11 by absorption tower second entrance 11A2 and is sprayed down, the absorbent sprayed down is contacted with flue gas adverse current,
To which absorbent absorbs the carbon dioxide in flue gas and becomes rich solution, rich solution is settled downwards, be stripped of the flue gas of carbon dioxide after
It is continuous to move upwards.In one embodiment, absorbent is Amine Solutions.It is certainly not limited to this, those skilled in the art can select
Select other suitable absorbents.
Rich solution enters rich solution pump 12 via absorption tower first outlet 11B1, rich solution pump intake 12A, then pumps out via rich solution
Mouth 12B, the first poor rich liquid heat exchanger first entrance 13A1, which enter in the first poor rich liquid heat exchanger 13, carries out the first heat exchange, to inhale
Heat heating.
The rich solution of the first heat exchange is completed via the first poor rich liquid heat exchanger first outlet 13B1, rich solution splitter inlet
14A enters in rich solution current divider 14, to be split into two-way.
First via rich solution enters condenser 163 via rich solution current divider first outlet 14B1, condenser first entrance 163A1
In to carry out the second heat exchange and heating of absorbing heat, complete the first via rich solution of the second heat exchange via condenser first outlet
163B1, desorber first entrance 17A1 enter in desorber 17.
Second road rich solution enters via rich solution current divider second outlet 14B2, the second poor rich liquid heat exchanger first entrance 15A1
Carry out third heat exchange and heating of absorbing heat in second poor rich liquid heat exchanger 15, the second road rich solution of completion third heat exchange is via the
Two poor rich liquid heat exchanger first outlet 15B1, desorber second entrance 17A2 are carried out in desorber 17.
First via rich solution and the second road rich solution are heated in desorber 17 to be desorbed and is decomposed into lean solution and carbon dioxide, poor
Liquid settles downwards in desorber 17, and carbon dioxide moves upwards.
The partially liq (can be the thorough lean solution of desorption, be also possible to desorb halfway semi lean solution) at 17 bottom of desorber
Enter in boiling device 18 via desorber third outlet 17B3, boiling device first entrance 18A1, and enter with via boiling device second
The saturated vapor that mouthful 18A2 is flowed into carries out the 4th heat exchange, the partially liq absorb heat in boiling device 18 heat up and by part vapour
Change and entered in desorber 17 by boiling device first outlet 18B1, the 4th entrance 17A4 of desorber, is the rich solution in desorber 17
Desorption provides steam and heat；Saturated vapor heat release cooling in boiling device 18 becomes condensed water, and condensed water is via boiling device the
Two outlet 18B2 discharges.It should be noted that semi lean solution is broken down into when semi lean solution carries out four heat exchanges in boiling device 18
Steam, lean solution and carbon dioxide simultaneously have a large amount of heat, and three is returned to together in desorber 17, the dioxy with heat
Change carbon and steam moves upwards in desorber 17, provides heat to desorb to two-way rich solution.
The carbon dioxide moved upwards can carry part lean solution (presence in the form of amine steam), then via desorber
One outlet 17B1, evaporator first entrance 161A1, which enter in evaporator 161, carries out the 5th with the worker quality liquid in evaporator 161
Heat exchange, worker quality liquid heat absorption heating become working substance steam, and working substance steam enters via evaporator second outlet 161B2, compressor
Mouth 162A enters in compressor 162, and compressor 162 compresses working substance steam, heats up and rises via compressed working substance steam
Buckling is superheated steam, and superheated steam enters in condenser 163 via compressor outlet 162B, condenser second entrance 163A2,
And aforementioned second heat exchange is carried out with the first via rich solution flowed into via condenser first entrance 163A1, the heat absorption of first via rich solution
Heating, and superheated steam heat release cooling becomes high-pressure working medium liquid, high-pressure working medium liquid flows into throttle valve 164 and is depressurized
For the worker quality liquid of initial conditions, worker quality liquid under the action of throttle valve 164 via evaporator second entrance 161A2 again into
Enter in evaporator 161, so that worker quality liquid completes one cycle use process.
The lean solution desorbed in desorber 17 is via desorber second outlet 17B2, the second poor rich liquid heat exchanger second entrance
15A2 enters in the second poor rich liquid heat exchanger 15, with the second tunnel richness entered via the second poor rich liquid heat exchanger first entrance 15A1
Liquid carries out aforementioned third heat exchange, lean solution heat release cooling.
The lean solution of third heat exchange is completed via the second poor rich liquid heat exchanger second outlet 15B2, the first poor rich liquid heat exchanger
Second entrance 13A2 enters in the first poor rich liquid heat exchanger 13, and enters via the first poor rich liquid heat exchanger first entrance 13A1
Rich solution carries out aforementioned first heat exchange, and heat release cools down lean solution again, and the lean solution for completing the first heat exchange is changed via the first rich or poor liquid
Hot device second outlet 13B2, lean pump 19 enter lean solution cooler 20 in is cooled again, then be cooled after lean solution via
Lean solution cooler 20, absorption tower second entrance 11A2 enter in absorption tower 11, are used using the absorbent as absorbing carbon dioxide.
In the chemical absorption method carbon dioxide capture system according to the present invention utilized based on Waste Heat Recovery, via absorption
The rich solution (for cold rich solution) of tower first outlet 11B1 discharge experienced the first heat under the action of the first poor rich liquid heat exchanger 13 and hand over
Change and heating of absorbing heat, then divide via rich solution current divider 14 for two-way, the second road rich solution via the second poor rich liquid heat exchanger 15 with
The lean solution (hot lean solution) that desorber 17 flows out desorb in third heat exchange, then inflow desorber 17, effectively utilizes
The waste heat of hot lean solution；And the heat that first via rich solution is transmitted via the working medium in heat pump system 16 (comes from 17 top row of desorber
The working medium in gas and evaporator 16 out carries out the 5th heat exchange, working medium heat absorption heating) and desorber 17 is absorbed indirectly
Heat entrained by the carbon dioxide that top row goes out efficiently utilizes the waste heat of the gas on the top of desorber 17 to heat first via richness
Liquid；Two-way rich solution had not only absorbed the waste heat of the hot lean solution via the outflow of 17 bottom of desorber, but also the outflow of the top of desorber 17 is utilized
Rich solution is divided into two-way for all the way by the waste heat of gas, and rich solution is enabled to absorb more waste heat and reach higher
Temperature, largely reduce rich solution required heat when desorber 17 desorbs, thereby reduce boiling device 18 and generate steaming
The energy consumption of vapour.
Absorption tower 11 further include: absorption tower third entrance 11A3, positioned at absorption tower 11 middle part and be located at absorption tower second
The lower section of entrance 11A2；Absorption tower third export 11B3, positioned at absorption tower 11 middle part and be located at absorption tower third entrance 11A3
Top.
It further include interstage cooler 21 based on the chemical absorption method carbon dioxide capture system that Waste Heat Recovery utilizes.It is cold between grade
But 21 side of device is connected to absorption tower third entrance 11A3, and the other side is connected to absorption tower third outlet 11B3.
Wherein, the absorbent in absorption tower 11 (descends via absorption tower second entrance 11A2 spray and is stored in absorption tower
Absorbent in 11) it is flowed into interstage cooler 21 via absorption tower third outlet 11B3 to cool down, via cold between grade
But the absorbent after device 21 cools down is flowed back into absorption tower 11 via absorption tower third entrance 11A3 and is sprayed downwards, is sprayed downwards
Absorbent contacted with the flue gas adverse current entered via absorption tower first entrance 11A1, absorbent absorb flue gas at least partly
Carbon dioxide and become rich solution, rich solution settles downwards；Removing at least partly carbon dioxide flue gas continue up and with warp
It is sprayed and lower absorbent counter current contacting and by via absorption tower second entrance 11A2 spray again by absorption tower second entrance 11A2
Leaching and lower absorbent the second secondary response of progress and the flue gas for becoming rich solution and carbon dioxide removal, the rich solution of generation is to sinking
Drop, and the flue gas of carbon dioxide removal continues to move upwards, and the flue gas of the carbon dioxide removal moved upwards can carry portion
Divide absorbent.
It should be noted that the absorption of carbon dioxide needs to carry out at a lower temperature, to guarantee in absorption tower 11
The uptake of carbon dioxide reach maximization, and the setting of interstage cooler 21 creates a further reduction the suction in absorption tower 11
The temperature of agent is received, the absorbent after cooling is flowed back into absorption tower 11 with smoke reaction again, improved to the dioxy in flue gas
The uptake and absorption rate for changing carbon, thereby reduce the use of absorbent, have saved cost；Via absorption tower first entrance
The flue gas that 11A1 enters successively is sprayed by absorption tower third entrance 11A3, absorption tower third entrance 11A2 during moving upwards
Leaching and lower absorbent absorption, so that the carbon dioxide in flue gas is fully absorbed, improve the absorptivity to carbon dioxide.
In one embodiment, interstage cooler 21 is water cooler.
Washing water is pre-stored in the cavity on the top on absorption tower 11.Absorption tower 11 further include: the 4th entrance of absorption tower
11A4, the top positioned at absorption tower 11 and the top positioned at absorption tower second entrance 11A2；Absorption tower the 4th exports 11B4, is located at
The top on absorption tower 11 and the top for being located at absorption tower second entrance 11A2 are flowed out for the washing water being pre-stored in absorption tower 11.
Further include once washing pump 22 based on the chemical absorption method carbon dioxide capture system that Waste Heat Recovery utilizes, once wash
Wash cooler 23.
Once washing pump 22 includes: once washing pump intake 22A, is connected to absorption tower the 4th and exports 11B4；Once washing
Pump discharge 22B.
23 side of once washing cooler is connected to once washing pump discharge 22B, and the other side is connected to absorption tower the 4th and enters
Mouth 11A4.
Wherein, absorption tower 11, once washing pump 22, once washing cooler 23 form once washing circuit, wash when once
After washing 22 unlatching of pump, the washing water in absorption tower 11 exports 11B4 via absorption tower the 4th, once washing pump intake 22A is flowed into
In once washing pump 22, then it is flowed into once washing cooler 23 and is cooled down via once washing pump discharge 22B, it is cooling
Washing water afterwards flow back into the top on absorption tower 11 again and spray and under, and the flue gas of carbon dioxide removal described above exists
It is also carried when being moved upwards in absorption tower 11 and partially absorbs agent, carbon dioxide removal and carrying partially absorbs the flue gas of agent and inhaling
It receives and is moved upwards in tower 11 and with cooling washing water counter current contacting, at least partly absorbent in flue gas is dissolved in washing water
In, then the flue gas after once washing continues up to be discharged via absorption tower second outlet 11B2.
The process of once washing has washed entrained by the flue gas of carbon dioxide removal at least absorbent, it is therefore prevented that is washed with water
The flue gas that the absorbent of water dissolution is removed carbon dioxide is taken out of outside absorption tower 11, and the loss of absorbent is reduced.
In one embodiment, absorption tower 11 further includes absorption tower silk screen, is set to the top on absorption tower 11, for de-
Mixed amine steam (absorbent) is filtered in the flue gas of removing carbon dioxide, thereby further reduces the loss of absorbent.
It should be noted that then can still be carried via the flue gas of absorption tower second outlet 11B2 discharge by once washing
Partially absorb agent.
Further include the first gas-liquid separator 24 based on the chemical absorption method carbon dioxide capture system that Waste Heat Recovery utilizes, wash
Wash tower 25.
First gas-liquid separator 24 includes: the first gas-liquid separator entrance 24A, is connected to absorption tower second outlet 11B2；The
One gas-liquid separator first outlet 24B1, positioned at the bottom of the first gas-liquid separator 24；First gas-liquid separator second outlet
24B2, positioned at the top of the first gas-liquid separator 24.In one embodiment, the first gas-liquid separator 24 further includes the first gas-liquid point
From device silk screen, it is set to the top of the first gas-liquid separator 24, for condensation mixed in the flue gas to carbon dioxide removal
Dilute amine liquid (absorbent) be filtered, to further reduced the loss of absorbent.
Washing water is stored in scrubbing tower 25, scrubbing tower 25 includes: scrubbing tower first entrance 25A1, positioned at scrubbing tower 25
Middle part is simultaneously connected to the first gas-liquid separator second outlet 24B2；Scrubbing tower second entrance 25A2 is located at scrubbing tower first entrance
The top of 25A1；Scrubbing tower first outlet 25B1, positioned at the top of scrubbing tower 25；Scrubbing tower second outlet 25B2 is located at washing
The lower part of tower 25；Scrubbing tower third exports 25B3, positioned at the bottom of scrubbing tower 25.
In one embodiment, scrubbing tower 25 can also be equipped with scrubbing tower silk screen, be set to the top of scrubbing tower 25, for pair
Dilute amine liquid (droplet) of mixed condensation is filtered in the flue gas of carbon dioxide removal, further reduced the damage of absorbent
Consumption.
Secondary washing pump 26 includes: secondary washing pump intake 26A, is connected to scrubbing tower second outlet 25B2；Secondary washing pump
Export 26B.
27 side of secondary washing cooler is connected to secondary washing pump discharge 26B, and the other side is connected to scrubbing tower second and enters
Mouth 25A2.
Lean solution current divider 28 includes: lean solution current divider first entrance 28A1, is connected to the first gas-liquid separator first outlet
24B1；Lean solution current divider second entrance 28A2, connection scrubbing tower third export 25B3；Lean solution current divider exports 28B.
Absorbent reservoir 29 includes: absorbent storage reservoir entrance 29A, and connection lean solution current divider exports 28B；Absorbent
Reservoir exports 29B, is connected to the side of lean solution cooler 20.
Wherein, the flue gas that the carrying of absorption tower second outlet 11B2 discharge partially absorbs agent enters via the first gas-liquid separator
Mouth 24A enters in the first gas-liquid separator 24, and the first gas-liquid separator 24 will at least partly absorbent be separated with flue gas.
Flue gas is discharged via the first gas-liquid separator second outlet 24B2, and the flue gas of discharge, which still contains, at least partly to be absorbed
Agent, the flue gas containing at least partly absorbent enter in scrubbing tower 25 and move upwards via scrubbing tower first entrance 25A1, wash
The washing water washed in tower 25 enters in secondary washing pump 26 via scrubbing tower second outlet 25B2, secondary washing pump intake 26A,
Then be flowed into secondary washing cooler 27 and cooled down via secondary washing pump discharge 26B, cooled washing water via
Scrubbing tower second entrance 25A2 enter in scrubbing tower 25 and spray and under, spray and lower washing water is at least partly absorbed with carrying
The flue gas adverse current of agent contacts, and the absorbent in flue gas is washed with water water dissolution, is stripped of the flue gas of absorbent via scrubbing tower first
25B1 discharge is exported, and the washing water dissolved with absorbent exports 25B3, lean solution current divider second entrance via scrubbing tower third
28A2 is flowed into lean solution current divider 28.
The absorbent isolated via the first gas-liquid separator 24 is via the first gas-liquid separator first outlet 24B1, lean solution
Current divider first entrance 28A1 is flowed into lean solution current divider 28.
Lean solution current divider 28 is by above-mentioned two-way absorbent (absorbent that lean solution current divider first entrance 28A1 is flowed into and poor
The absorbent that liquid current divider second entrance 28A2 is flowed into) it is mixed, mixed absorbent is exported via lean solution current divider
28B, 29 entrance of absorbent reservoir enter in absorbent reservoir 29, then cold via absorbent reservoir outlet 29B, lean solution
But device 20 flows into absorption tower 11 and is re-circulated use.
During above-mentioned secondary washing, the first gas-liquid separator 24 isolates at least partly absorbent in flue gas
Come, then into lean solution current divider 28；Flue gas by gas-liquid separation, which is again introduced into scrubbing tower 25, carries out secondary washing,
After flue gas is washed via scrubbing tower 25, absorbent entrained by flue gas is dissolved in scrubbing tower 25, subsequently into lean solution current divider
In 28, the absorbent that the absorbent and scrubbing tower 25 isolated via the first gas-liquid separator 24 wash out separately flows into poor
It in liquid current divider 28 and is mixed, mixed absorbent is again returned in absorption tower 11 and reused, this mistake
Journey significantly reduces the loss of absorbent, has saved cost；In addition, the first gas-liquid separator of the first gas-liquid separator 24 is used
The setting of the scrubbing tower silk screen of silk screen and scrubbing tower 25 further reduced the loss of absorbent.
It further include flash tank 30, roots blower based on the chemical absorption method carbon dioxide capture system that Waste Heat Recovery utilizes
31, steam condenser 32.
Flash tank 30 includes: flash tank entrance 30A, is connected to desorber second outlet 17B2；Flash tank first outlet 30B1；
Flash tank second outlet 30B2 is connected to the second poor rich liquid heat exchanger second entrance 15A2.
Roots blower 31 includes: roots blower entrance 31A, is connected to flash tank first outlet 30B1；Roots blower outlet
31B。
32 side of steam condenser is connected to roots blower outlet 31B, and the other side is connected to desorber third entrance 17A3.
Directly enter in flash tank 30 via flash tank entrance 30A via the lean solution that desorber second outlet 17B2 flows out,
Lean solution is flashed in flash tank 30, and to flash off some vapor, (steam is largely water vapour, and very little part is amine steaming
Vapour), the steam flashed off enters roots blower 31 via flash tank first outlet 30B1, roots blower entrance 31A, and steam is in sieve
Heating is pressurized in thatch blower 31, it is cooling then via roots blower outlet 31B, into being cooled down in steam condenser 32
Steam afterwards enters in desorber 17 via desorber third entrance 17A3, to provide auxiliary for the rich solution desorption in desorber 17
Heat；Lean solution after flash distillation process via flash tank second outlet 30B2, the second poor rich liquid heat exchanger second entrance 15A2 into
Enter in the second poor rich liquid heat exchanger 15, is carried out with the second road rich solution entered via the second poor rich liquid heat exchanger first entrance 15A1
Aforementioned third heat exchange, lean solution heat release cooling.
Lean solution releases a large amount of steam via the flash distillation of flash tank 30, this some vapor temperature after the pressurization of roots blower 31
Degree and pressure improve (such as being forced into 110-120 DEG C by 70-90 DEG C), and the quality of steam is substantially improved, and are higher than desorber
Lean solution temperature in 17, it should be noted that if vapor (steam) temperature is excessively high (such as more than 130 degree), if being passed directly into desorber
When 17, it will make the lean solution desorbed that the adverse effects such as thermal degradation occur, and the setting of steam condenser 32 can be by hot steam
Temperature reduce (dropping to 130 degree or less), thus for desorber 17 desorb rich solution optimal desorption heat is provided, meanwhile, reduction
The demand of steam from boiling device 18 reduces the energy consumption that boiling device 18 generates steam.
Based on the chemical absorption method carbon dioxide capture system that Waste Heat Recovery utilizes further include purifying column 33, self-fractionating pump 34,
Purify cooler 35.
Cleanser is stored in purifying column 33, purifying column 33 includes: purifying column first entrance 33A1, positioned at purifying column 33
Lower part enters for external flue gas；Purifying column second entrance 33A2, positioned at the top of purifying column 33；Purifying column first outlet 33B1,
Positioned at the top of purifying column 33, it is connected to absorption tower first entrance 11A1；Purifying column second outlet 33B2, under purifying column 33
Portion and the lower section for being located at purifying column first entrance 33A1.
In one embodiment, purifying column 33 further includes purifying column silk screen, for removing steam and mist in flue gas.
Self-fractionating pump 34 includes: purification pump intake 34A, is connected to purifying column second outlet 33B2；Purify pump discharge 34B.
35 side of cooler connection purification pump discharge 34B is purified, the other side is connected to purifying column second entrance 33A2.
Wherein, purifying column 33, self-fractionating pump 34, purification cooler 35 form external gas cleaning circulation loop, work as self-fractionating pump
After 34 open, the cleanser in purifying column 33 is pumped into purification via purifying column second outlet 33B2 discharge, via self-fractionating pump 34
Cooler 35 cooled down, later via purifying column second entrance 33A2 back to spraying in purifying column 33 and downwards, external cigarette
Gas enters in purifying column 33 and moves upwards via purifying column first entrance 33A1, the external flue gas moved upwards with via purification
Tower second entrance 33A2 spray and lower cleanser counter current contacting, cleanser absorb outside acid impurities gas and cigarette in flue gas
Dirt, and the carbon dioxide in external flue gas is not cleaned agent absorption, flue gas moves upwards after purification and via purifying column
First outlet 33B1, absorption tower first entrance 11A1 enter in absorption tower 11, to supply to absorption tower 11.
In one embodiment, the purifying column first entrance 33A1 of purifying column 33 can be connected to power-plant flue gas pipeline.Cleanser
It can be sodium bicarbonate solution.It is certainly not limited to this, those skilled in the art can choose any suitable cleanser.
The setting of purifying column 33 has carried out effective purification to the flue gas entered in absorption tower 11, avoids in absorption tower 11
Absorbent absorbs foreign gas, and then improves the purity of product gas.
The carbon dioxide being discharged from desorber first outlet 17B1 also carries part lean solution.
In one embodiment, desorber 17 further includes desorber silk screen, and the amine steam for carrying to carbon dioxide is (poor
Liquid steam) it is filtered, reduce the loss of a part of lean solution.
It further include desorption gas condenser 36, second based on the chemical absorption method carbon dioxide capture system that Waste Heat Recovery utilizes
Gas-liquid separator 37.
Desorbing gas condenser 36 includes: stripping gas condenser inlet 36A, is connected to evaporator first outlet 161B1；Desorption device
Condensator outlet 36B.
Second gas-liquid separator 37 includes: the second gas-liquid separator entrance 37A, is connected to stripping gas condensator outlet 36B；The
Two gas-liquid separator first outlet 37B1, positioned at the top of the second gas-liquid separator 37；Second gas-liquid separator second outlet
37B2, positioned at the bottom of the second gas-liquid separator 37.
In one embodiment, the second gas-liquid separator 37 further includes the second gas-liquid separator silk screen, for product gas
In the amine liquid (lean solution) of mixed condensation be filtered.
Wherein, the carbon dioxide with part lean solution (presence in the form of amine steam) is via evaporator first outlet
161B1, stripping gas condenser inlet 36A, which enter in condenser 163, to be cooled down, through the overcooled dioxy with part lean solution
Change carbon to enter in the second gas-liquid separator 37 via the second gas-liquid separator entrance 37A, the carbon dioxide warp with part lean solution
Gas-liquid separation is carried out by the second gas-liquid separator 37 and is separated into carbon dioxide product gas and lean solution, carbon dioxide product gas warp
It is discharged by the second gas-liquid separator first outlet 37B1, to carry out next step operation.
The lean solution isolated is then refluxed for absorbent reservoir via the second gas-liquid separator second outlet 37B2 discharge
In 29, to be used as absorbent.
A large amount of waste heat is had from the carbon dioxide with part lean solution of the discharge of desorber 17, two with part lean solution
Waste heat is effectively passed to working medium by carrying out heat exchange with the working medium in heat pump system 16 by carbonoxide, and then will by working medium
Heat transfer gives the first via rich solution distributed via rich solution current divider 14, and the rich solution for heating of absorbing heat is in entering desorber 17
Desorption, heat needed for reducing desorption efficiently utilize the waste heat of the gas on the top of desorber 17；In addition, via the second gas
The lean solution that liquid/gas separator 36 is separated again returns in absorbent reservoir 29, reduces the loss of lean solution, meanwhile, second
The setting of gas-liquid separator silk screen captures at least partly lean solution of product gas carrying, further reduced the loss of lean solution.
Claims (9)
1. a kind of chemical absorption method carbon dioxide capture system utilized based on Waste Heat Recovery characterized by comprising
Absorption tower (11), comprising:
Absorption tower first entrance (11A1) is located at the lower part of absorption tower (11), enters for flue gas, and flue gas has carbon dioxide；
Absorption tower second entrance (11A2) is located at the top of absorption tower (11), enters for absorbent；
Absorption tower first outlet (11B1) is located at the bottom of absorption tower (11), flows out for rich solution；
Absorption tower second outlet (11B2) is located at the top of absorption tower (11)；
Rich solution pump (12), comprising:
Rich solution pump intake (12A) is connected to absorption tower first outlet (11B1)；
Rich solution pump discharge (12B)；
First poor rich liquid heat exchanger (13), comprising:
First poor rich liquid heat exchanger first entrance (13A1) is connected to rich solution pump discharge (12B)；
First poor rich liquid heat exchanger second entrance (13A2)；
First poor rich liquid heat exchanger first outlet (13B1)；
First poor rich liquid heat exchanger second outlet (13B2)；
Rich solution current divider (14), comprising:
Rich solution splitter inlet (14A) is connected to the first poor rich liquid heat exchanger first outlet (13B1)；
Rich solution current divider first outlet (14B1)；
Rich solution current divider second outlet (14B2)；
Second poor rich liquid heat exchanger (15), comprising:
Second poor rich liquid heat exchanger first entrance (15A1) is connected to rich solution current divider second outlet (14B2)；
Second poor rich liquid heat exchanger second entrance (15A2)；
Second poor rich liquid heat exchanger first outlet (15B1)；
Second poor rich liquid heat exchanger second outlet (15B2) is connected to the first poor rich liquid heat exchanger second entrance (13A2)；
Heat pump system (16), including evaporator (161), compressor (162), condenser (163) and throttle valve (164),
Evaporator (161), comprising:
Evaporator first entrance (161A1)；
Evaporator second entrance (161A2)；
Evaporator first outlet (161B1)；
Evaporator second outlet (161B2)；
Compressor (162), comprising:
Suction port of compressor (162A) is connected to evaporator second outlet (161B2)；
Compressor outlet (162B)；
Condenser (163), comprising:
Condenser first entrance (163A1) is connected to rich solution current divider first outlet (14B1)；
Condenser second entrance (163A2) is connected to compressor outlet (162B)；
Condenser first outlet (163B1)；
Condenser second outlet (163B2)；
Throttle valve (164) is set between condenser (163) and evaporator (161), the controlled connection condenser second outlet in one end
(163B2), the controlled connection evaporator second entrance (161A2) of the other end；
Desorber (17), comprising:
Desorber first entrance (17A1) is located at desorber (17) top, is connected to condenser first outlet (163B1)；
Desorber second entrance (17A2) is located at the top of desorber (17) and is lower than desorber first entrance (17A1), connection
Second poor rich liquid heat exchanger first outlet (15B1)；
Desorber third entrance (17A3) is located at the middle part of desorber (17) and is lower than desorber second entrance (17A2)；
The 4th entrance (17A4) of desorber is located at the lower part of desorber (17) and is lower than desorber third entrance (17A3)；
Desorber first outlet (17B1) is located at the top of desorber (17), is connected to evaporator first entrance (161A1)；
Desorber second outlet (17B2) is located at desorber (17) bottom；
Desorber third exports (17B3), is located at the lower part of desorber (17)；
Boiling device (18), comprising:
Boiling device first entrance (18A1), connection desorber third outlet (17B3)；
Boiling device second entrance (18A2) is flowed into for external saturated vapor；
Boiling device first outlet (18B1) is connected to the 4th entrance (17A4) of desorber；
Boiling device second outlet (18B2)；
Lean pump (19), comprising:
Lean solution pump intake (19A) is connected to the first poor rich liquid heat exchanger second outlet (13B2)；
Lean solution pump discharge (19B)；
Lean solution cooler (20), side are connected to lean solution pump discharge (19B), and the other side is connected to absorption tower second entrance
(11A2)；
Wherein, flue gas enters in absorption tower (11) via absorption tower first entrance (11A1) and from the bottom up moves, absorbent warp
Entered in absorption tower (11) by absorption tower second entrance (11A2) and down sprayed, the absorbent sprayed down connects with flue gas adverse current
Touching, so that absorbent absorbs the carbon dioxide in flue gas and becomes rich solution, rich solution is settled downwards, is stripped of the flue gas of carbon dioxide
It continues up；
Rich solution enters rich solution pump (12) via absorption tower first outlet (11B1), rich solution pump intake (12A), then via rich solution pump
Export (12B), the first poor rich liquid heat exchanger first entrance (13A1) enters the first heat of progress in the first poor rich liquid heat exchanger (13)
Exchange, with heating of absorbing heat；
The rich solution of the first heat exchange is completed via the first poor rich liquid heat exchanger first outlet (13B1), rich solution splitter inlet
(14A) enters in rich solution current divider (14), to be split into two-way,
First via rich solution enters condenser via rich solution current divider first outlet (14B1), condenser first entrance (163A1)
(163) to carry out the second heat exchange and heating of absorbing heat in, the first via rich solution for completing the second heat exchange goes out via condenser first
Mouth (163B1), desorber first entrance (17A1) enter in desorber (17)；
Second road rich solution enters via rich solution current divider second outlet (14B2), the second poor rich liquid heat exchanger first entrance (15A1)
Carry out third heat exchange and heating of absorbing heat in second poor rich liquid heat exchanger (15), the second road rich solution of completion third heat exchange via
Second poor rich liquid heat exchanger first outlet (15B1), desorber second entrance (17A2) carry out in desorber (17)；
First via rich solution and the second road rich solution are heated in desorber (17) to be desorbed and is decomposed into lean solution and carbon dioxide, lean solution
It is settled downwards in desorber (17), carbon dioxide moves upwards；
The partially liq at desorber (17) bottom enters via desorber third outlet (17B3), boiling device first entrance (18A1) to be boiled
It boils in device (18), and carries out the 4th heat exchange, the part with the saturated vapor flowed into via boiling device second entrance (18A2)
Liquid is partially vaporized in the middle heat absorption heating of boiling device (18) and by boiling device first outlet (18B1), the 4th entrance of desorber
(17A4) enters in desorber (17), provides steam and heat for the rich solution desorption in desorber (17)；In boiling device (18)
Saturated vapor heat release cooling becomes condensed water, and condensed water is discharged via boiling device second outlet (18B2)；
The carbon dioxide moved upwards can carry part lean solution, then via desorber first outlet (17B1), evaporator first
Entrance (161A1), which enters in evaporator (161), carries out the 5th heat exchange, worker quality liquid with the worker quality liquid in evaporator (161)
Heat absorption heating becomes working substance steam, and working substance steam enters pressure via evaporator second outlet (161B2), suction port of compressor (162A)
In contracting machine (162), compressor (162) compresses working substance steam, becomes via compressed working substance steam increasing temperature and pressure
Hot steam, superheated steam enter in condenser (163) via compressor outlet (162B), condenser second entrance (163A2), and
Aforementioned second heat exchange, the heat absorption of first via rich solution are carried out with the first via rich solution flowed into via condenser first entrance (163A1)
Heating, and superheated steam heat release cooling becomes high-pressure working medium liquid, high-pressure working medium liquid flow into throttle valve (164) and be depressurized and
As the worker quality liquid of initial conditions, worker quality liquid is under the action of throttle valve (164) via evaporator second entrance (161A2)
It is again introduced into evaporator (161), so that worker quality liquid completes one cycle use process；
The lean solution desorbed in desorber (17) is via desorber second outlet (17B2), the second poor rich liquid heat exchanger second entrance
(15A2) enters in the second poor rich liquid heat exchanger (15), with enter via the second poor rich liquid heat exchanger first entrance (15A1) the
Two road rich solutions carry out aforementioned third heat exchange, lean solution heat release cooling；
The lean solution of third heat exchange is completed via the second poor rich liquid heat exchanger second outlet (15B2), the first poor rich liquid heat exchanger the
Two entrances (13A2) enter the first poor rich liquid heat exchanger (13) in, with via the first poor rich liquid heat exchanger first entrance (13A1) into
The rich solution entered carries out aforementioned first heat exchange, lean solution heat release cooling, and the lean solution for completing the first heat exchange is changed via the first rich or poor liquid
Hot device second outlet (13B2), lean pump (19), which enter in lean solution cooler (20), to be cooled again, poor after being then cooled
Liquid enters in absorption tower (11) via lean solution cooler (20), absorption tower second entrance (11A2), using as absorbing carbon dioxide
Absorbent use.
2. the chemical absorption method carbon dioxide capture system according to claim 1 utilized based on Waste Heat Recovery, feature
It is,
Absorption tower (11) further include:
Absorption tower third entrance (11A3) is located at the middle part of absorption tower (11) and is located under absorption tower second entrance (11A2)
Side；
Absorption tower third exports (11B3), is located at the middle part of absorption tower (11) and is located at the upper of absorption tower third entrance (11A3)
Side；
The chemical absorption method carbon dioxide capture system utilized based on Waste Heat Recovery further include: interstage cooler (21), side connect
Absorption tower third entrance (11A3) is passed through, the other side is connected to absorption tower third outlet (11B3)；
Wherein, the absorbent in absorption tower (11) via absorption tower third outlet (11B3) be flowed into interstage cooler (21) with
Cool down, flows back into absorption tower via absorption tower third entrance (11A3) via the absorbent after interstage cooler (21) cooling
(11) it sprays in and downwards, the absorbent sprayed downwards connects with the flue gas adverse current entered via absorption tower first entrance (11A1)
Touching, absorbent absorb at least partly carbon dioxide in flue gas and become rich solution, and rich solution settles downwards；Removing at least partly dioxy
Change carbon flue gas continue up and with via absorption tower second entrance (11A2) spray and under absorbent countercurrently connect again
Touch and sprayed via absorption tower second entrance (11A2) and lower absorbent the second secondary response of progress and become rich solution and removing
The rich solution of the flue gas of carbon dioxide, generation settles downwards, and the flue gas of carbon dioxide removal continues to move upwards, and fortune upwards
The flue gas of dynamic carbon dioxide removal can carry and partially absorb agent.
3. the chemical absorption method carbon dioxide capture system according to claim 2 utilized based on Waste Heat Recovery, feature
It is,
Absorption tower (11) further include:
The 4th entrance (11A4) of absorption tower is located at the top of absorption tower (11) and positioned at the upper of absorption tower second entrance (11A2)
Portion；
Absorption tower the 4th exports (11B4), is located at the top of absorption tower (11) and positioned at the upper of absorption tower second entrance (11A2)
Side is flowed out for the washing water being pre-stored in absorption tower (11)；
The chemical absorption method carbon dioxide capture system utilized based on Waste Heat Recovery further include:
Once washing pumps (22), comprising:
Once washing pump intake (22A) is connected to absorption tower the 4th and exports (11B4)；
Once washing pump discharge (22B)；
Once washing cooler (23), side are connected to once washing pump discharge (22B), and the other side is connected to absorption tower the 4th and enters
Mouth (11A4)；
Wherein, absorption tower (11), once washing pump (22), once washing cooler (23) form once washing circuit, when primary
After washing pump (22) is opened, the washing water in absorption tower (11) exports (11B4), once washing pump intake via absorption tower the 4th
(22A) is flowed into once washing pump (22), is then flowed into once washing cooler via once washing pump discharge (22B)
(23) cooled down in, washing water after cooling flow back into the top on absorption tower (11) again and spray and under, remove titanium dioxide
Carbon and carrying partially absorbs the washing water counter current contacting that the flue gas of agent is moved upwards and is cooled in absorption tower (11), in flue gas
At least partly absorbent be dissolved in washing water, the flue gas after once washing continue up then via absorption tower
Second outlet (11B2) discharge.
4. the chemical absorption method carbon dioxide capture system according to claim 3 utilized based on Waste Heat Recovery, feature
It is,
It is also carried via the flue gas that absorption tower second outlet (11B2) is discharged and partially absorbs agent；
The chemical absorption method carbon dioxide capture system utilized based on Waste Heat Recovery further include:
First gas-liquid separator (24), comprising:
First gas-liquid separator entrance (24A) is connected to absorption tower second outlet (11B2)；
First gas-liquid separator first outlet (24B1) is located at the bottom of the first gas-liquid separator (24)；
First gas-liquid separator second outlet (24B2) is located at the top of the first gas-liquid separator (24)；
Scrubbing tower (25) is stored with washing water in scrubbing tower (25), and scrubbing tower (25) includes:
Scrubbing tower first entrance (25A1) is located at the middle part of scrubbing tower (25) and is connected to the first gas-liquid separator second outlet
(24B2)；
Scrubbing tower second entrance (25A2) is located at the top of scrubbing tower (25)；
Scrubbing tower first outlet (25B1) is located at the top of scrubbing tower (25)；
Scrubbing tower second outlet (25B2) is located at the lower part of scrubbing tower (25)；
Scrubbing tower third exports (25B3), is located at the bottom of scrubbing tower (25)；
Secondary washing pumps (26), comprising:
Secondary washing pump intake (26A) is connected to scrubbing tower second outlet (25B2)；
Secondary washing pump discharge (26B)；
Secondary washing cooler (27), side are connected to secondary washing pump discharge (26B), and the other side is connected to scrubbing tower second and enters
Mouth (25A2)；
Lean solution current divider (28), comprising:
Lean solution current divider first entrance (28A1) is connected to the first gas-liquid separator first outlet (24B1)；
Lean solution current divider second entrance (28A2), connection scrubbing tower third outlet (25B3)；
Lean solution current divider exports (28B)；
Absorbent reservoir (29), comprising:
Absorbent stores up reservoir entrance (29A), connection lean solution current divider outlet (28B)；
Absorbent reservoir exports (29B), is connected to the side of lean solution cooler (20)；
Wherein, the carrying of absorption tower second outlet (11B2) discharge partially absorbs the flue gas of agent via the first gas-liquid separator entrance
(24A) enters in the first gas-liquid separator (24), and the first gas-liquid separator (24) will at least partly absorbent be separated with flue gas,
Flue gas is discharged via the first gas-liquid separator second outlet (24B2), and the flue gas of discharge still contains at least partly absorbent,
Flue gas containing at least partly absorbent enters in scrubbing tower (25) and moves upwards via scrubbing tower first entrance (25A1), washes
The washing water washed in tower (25) enters secondary washing via scrubbing tower second outlet (25B2), secondary washing pump intake (26A)
It pumps in (26), is then flowed into secondary washing cooler (27) and is cooled down via secondary washing pump discharge (26B), be cooled
Washing water via scrubbing tower second entrance (25A2) enter in scrubbing tower (25) and spray and under, spray and lower washing water and
The flue gas adverse current contact of at least partly absorbent is carried, the absorbent in flue gas is washed with water water dissolution, is stripped of the cigarette of absorbent
Gas is discharged via scrubbing tower first outlet (25B1), and the washing water dissolved with absorbent is exported via scrubbing tower third
(25B3), lean solution current divider second entrance (28A2) are flowed into lean solution current divider (28)；
The absorbent isolated via the first gas-liquid separator (24) is via the first gas-liquid separator first outlet (24B1), lean solution
Current divider first entrance (28A1) is flowed into lean solution current divider (28)；
Lean solution current divider (28) mixes two-way absorbent, mixed absorbent via lean solution current divider outlet (28B),
Absorbent reservoir (29) entrance enters in absorbent reservoir (29), then exports (29B), lean solution via absorbent reservoir
Cooler (20) flows into absorption tower (11) and is re-circulated use.
5. the chemical absorption method carbon dioxide capture system according to claim 1 utilized based on Waste Heat Recovery, feature
It is, the chemical absorption method carbon dioxide capture system utilized based on Waste Heat Recovery further include:
Flash tank (30), comprising:
Flash tank entrance (30A) is connected to desorber second outlet (17B2)；
Flash tank first outlet (30B1)；
Flash tank second outlet (30B2) is connected to the second poor rich liquid heat exchanger second entrance (15A2)；
Roots blower (31), comprising:
Roots blower entrance (31A) is connected to flash tank first outlet (30B1)；
Roots blower exports (31B)；
Steam condenser (32), side are connected to roots blower outlet (31B), and the other side is connected to desorber third entrance
(17A3)；
Directly enter flash tank (30) via flash tank entrance (30A) via the lean solution of desorber second outlet (17B2) outflow
Interior, lean solution is flashed the steam flashed off to flash off some vapor via flash tank first outlet in flash tank (30)
(30B1), roots blower entrance (31A) enter roots blower (31), and steam is pressurized heating in roots blower (31), then
Via roots blower outlet (31B), into being cooled down in steam condenser (32), steam after cooling is via desorber third
Entrance (17A3) enters in desorber (17), to provide the heat of auxiliary for the rich solution desorption in desorber (17)；Flash distillation process
Lean solution afterwards enters the second rich or poor liquid via flash tank second outlet (30B2), the second poor rich liquid heat exchanger second entrance (15A2)
In heat exchanger (15), aforementioned third is carried out with the second road rich solution entered via the second poor rich liquid heat exchanger first entrance (15A1)
Heat exchange, lean solution heat release cooling.
6. the chemical absorption method carbon dioxide capture system according to claim 1 utilized based on Waste Heat Recovery, feature
It is, the chemical absorption method carbon dioxide capture system utilized based on Waste Heat Recovery further include:
Purifying column (33), purifying column (33) is interior to be stored with cleanser, and purifying column (33) includes:
Purifying column first entrance (33A1) is located at the lower part of purifying column (33), enters for external flue gas；
Purifying column second entrance (33A2) is located at the top of purifying column (33)；
Purifying column first outlet (33B1) is located at the top of purifying column (33), is connected to absorption tower first entrance (11A1)；
Purifying column second outlet (33B2) is located at the lower part of purifying column (33) and is located under purifying column first entrance (33A1)
Side；
Self-fractionating pump (34), comprising:
It purifies pump intake (34A), is connected to purifying column second outlet (33B2)；
It purifies pump discharge (34B)；
It purifies cooler (35), side connection purification pump discharge (34B), the other side is connected to purifying column second entrance (33A2)；
Wherein, purifying column (33), self-fractionating pump (34), purification cooler (35) form external gas cleaning circulation loop, work as purification
After pumping (34) unlatching, the cleanser in purifying column (33) is discharged, via self-fractionating pump (34) via purifying column second outlet (33B2)
Purification cooler (35) is pumped into be cooled down, is interior simultaneously back to purifying column (33) via purifying column second entrance (33A2) later
Spray downwards, external flue gas enter in purifying column (33) and move upwards via purifying column first entrance (33A1), move upwards
External flue gas sprayed and lower cleanser counter current contacting with via purifying column second entrance (33A2), cleanser absorb outside cigarette
Acid impurities gas and flue dust in gas, and the carbon dioxide in external flue gas is not cleaned agent absorption, flue gas moves upwards
And enter in absorption tower (11) via purifying column first outlet (33B1), absorption tower first entrance (11A1), with to absorption tower
(11) it supplies.
7. the chemical absorption method carbon dioxide capture system according to claim 6 utilized based on Waste Heat Recovery, feature
It is,
Cleanser is sodium bicarbonate solution.
8. the chemical absorption method carbon dioxide capture system according to claim 1 utilized based on Waste Heat Recovery, feature
It is,
The carbon dioxide being discharged from desorber first outlet (17B1) also carries part lean solution；
The chemical absorption method carbon dioxide capture system utilized based on Waste Heat Recovery further include:
It desorbs gas condenser (36), comprising:
Stripping gas condenser inlet (36A) is connected to evaporator first outlet (161B1)；
Desorption device condensator outlet (36B)；
Second gas-liquid separator (37), comprising:
Second gas-liquid separator entrance (37A) is connected to stripping gas condensator outlet (36B)；
Second gas-liquid separator first outlet (37B1) is located at the top of the second gas-liquid separator (37)；
Second gas-liquid separator second outlet (37B2) is located at the bottom of the second gas-liquid separator (37)；
Wherein, the carbon dioxide with part lean solution is via evaporator first outlet (161B1), stripping gas condenser inlet
(36A), which enters in condenser (163), to be cooled down, through the overcooled carbon dioxide with part lean solution via the second gas-liquid point
Enter in the second gas-liquid separator (37) from device entrance (37A), the carbon dioxide with part lean solution is via the second gas-liquid separation
Device (37) carries out gas-liquid separation and is separated into carbon dioxide product gas and lean solution, and carbon dioxide product gas is via the second gas-liquid point
It is discharged from device first outlet (37B1), to carry out next step operation；
The lean solution isolated is then refluxed for absorbent reservoir via the discharge of the second gas-liquid separator second outlet (37B2)
(29) in.
9. the chemical absorption method carbon dioxide capture system according to claim 1 utilized based on Waste Heat Recovery, feature
It is, absorbent is Amine Solutions.
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