CN108236831A - Carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN - Google Patents
Carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN Download PDFInfo
- Publication number
- CN108236831A CN108236831A CN201711181818.8A CN201711181818A CN108236831A CN 108236831 A CN108236831 A CN 108236831A CN 201711181818 A CN201711181818 A CN 201711181818A CN 108236831 A CN108236831 A CN 108236831A
- Authority
- CN
- China
- Prior art keywords
- outlet
- entrance
- desorber
- absorption tower
- carbon dioxide
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 158
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 79
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 78
- 238000010521 absorption reaction Methods 0.000 claims abstract description 128
- 239000007788 liquid Substances 0.000 claims abstract description 73
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 69
- 239000002918 waste heat Substances 0.000 claims abstract description 16
- 238000003795 desorption Methods 0.000 claims abstract description 15
- 238000011084 recovery Methods 0.000 claims abstract description 11
- 239000007789 gas Substances 0.000 claims description 36
- 230000002745 absorbent Effects 0.000 claims description 24
- 239000002250 absorbent Substances 0.000 claims description 24
- 239000012530 fluid Substances 0.000 claims description 20
- 238000005406 washing Methods 0.000 claims description 13
- 238000010438 heat treatment Methods 0.000 claims description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 11
- 229910052799 carbon Inorganic materials 0.000 claims description 11
- 239000000126 substance Substances 0.000 claims description 9
- 238000004064 recycling Methods 0.000 claims description 7
- 239000002994 raw material Substances 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 6
- 238000000354 decomposition reaction Methods 0.000 claims description 4
- 238000010025 steaming Methods 0.000 claims description 4
- 239000002253 acid Substances 0.000 claims description 3
- 238000009835 boiling Methods 0.000 claims description 3
- 239000003500 flue dust Substances 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000009834 vaporization Methods 0.000 claims description 3
- 230000008016 vaporization Effects 0.000 claims description 3
- 241000790917 Dioxys <bee> Species 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 claims description 2
- 238000001816 cooling Methods 0.000 claims description 2
- 239000004744 fabric Substances 0.000 claims description 2
- 239000006210 lotion Substances 0.000 claims description 2
- 230000001737 promoting effect Effects 0.000 claims 1
- 239000002699 waste material Substances 0.000 abstract description 9
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 7
- 238000000034 method Methods 0.000 description 4
- 235000010215 titanium dioxide Nutrition 0.000 description 4
- 239000004408 titanium dioxide Substances 0.000 description 3
- 150000001412 amines Chemical class 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000007701 flash-distillation Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000001939 inductive effect Effects 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
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 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
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—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
- B01D53/185—Liquid distributors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Abstract
The present invention provides a kind of carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN, including water scrubber, gas-liquid separator, air-introduced machine, absorption tower, rich solution pump, multiple distribution heat exchangers, desorber, reboiler, flash tank and roots blower.In the carbon dioxide capture system according to the present invention based on UTILIZATION OF VESIDUAL HEAT IN, the lean solution flowed out from desorber first outlet carries higher heat, and the desorber, reboiler, flash tank and roots blower in the carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN of the present invention form lean solution waste heat recovery circulation loop, lean solution is converted into the high steam of temperature under the action of reboiler, flash tank and roots blower and is again introduced into desorber and provides the desorption of rich solution heat, the efficient utilization to lean solution waste heat is realized, reduces the waste of the energy.
Description
Technical field
The present invention relates to waste heat recovery field more particularly to a kind of carbon dioxide capture systems based on UTILIZATION OF VESIDUAL HEAT IN.
Background technology
At present, the whole energy consumption of chemical absorption method trapping carbon dioxide system is higher, essentially consists in carbon dioxide absorption mistake
Journey needs carry out under relatively low temperature condition, and carbon dioxide process needs are completed under higher temperature condition.
Many places energy is underutilized during this, wherein the mainly waste heat including desorber bottom lean solution, desorption tower top regeneration
The waste heat of gas, these heats are not carried out effective recycling, cause capacity usage ratio low.The very big of thermal energy is thereby resulted in
Waste.
Invention content
In view of the problem of background technology, the purpose of the present invention is to provide a kind of titanium dioxides based on UTILIZATION OF VESIDUAL HEAT IN
Carbon trapping system can recycle the waste heat of the lean solution of the bottom of desorber, realize efficiently using for lean solution waste heat, reduce the energy
Waste.
To achieve these goals, the present invention provides a kind of carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN, packets
It includes：Water scrubber, gas-liquid separator, air-introduced machine, absorption tower, rich solution pump, multiple distribution heat exchangers, desorber, reboiler, flash tank
And roots blower.
Water scrubber has：Water scrubber first entrance positioned at the top of water scrubber, is flowed into for external washing water；Water scrubber
First outlet, positioned at the top of water scrubber；Positioned at the lower part of water scrubber, titanium dioxide is carried for external for water scrubber second entrance
The unstripped gas of carbon enters；Water scrubber second outlet, positioned at the bottom of water scrubber.
Gas-liquid separator has：Gas-liquid separator entrance connects water scrubber first outlet；Gas-liquid separator first outlet,
Positioned at the top of gas-liquid separator；Gas-liquid separator second outlet, positioned at the bottom of gas-liquid separator.
Air-introduced machine has：Air-introduced machine entrance connects gas-liquid separator first outlet；Air-introduced machine exports.
Absorption tower has：Absorption tower first entrance, positioned at the bottom on absorption tower, the outlet of connection air-introduced machine；Absorption tower first
Outlet, positioned at the bottom on absorption tower；Absorption tower second entrance, positioned at the top on absorption tower；Absorption tower second outlet, positioned at absorption
The top of tower；Absorption tower third entrance, positioned at the top on absorption tower；Absorption tower third outlet, positioned at the top on absorption tower.
Rich solution pump has：Rich solution pump intake connects absorption tower first outlet；And rich solution pump discharge.
Carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN further includes：Multiple distribution heat exchangers, each heat exchanger that is distributed have：
Heat exchanger first entrance is distributed, connects rich solution pump discharge；It is distributed heat exchanger first outlet；It is distributed heat exchanger second entrance；Distribution
Heat exchanger second outlet connects absorption tower second entrance.
Desorber has：Desorber first entrance positioned at the top of desorber, connects multiple distribution heat exchanger first outlets
At least one of；Desorber first outlet, positioned at the bottom of desorber；Desorber second entrance, positioned at the middle part of desorber,
Connect at least one of multiple distribution heat exchanger first outlets；Desorber second outlet, positioned at the top of desorber；Desorber
Third entrance, positioned at the lower part of desorber；The 4th entrance of desorber, positioned at the lower part of desorber.
Reboiler has：Reboiler entrance connects desorber first outlet；Reboiler first outlet, connection desorber the
Three entrances；Reboiler second outlet.
Flash tank has：Flash tank entrance connects reboiler second outlet；Flash tank first outlet, positioned at flash tank
Top；Flash tank second outlet positioned at the bottom of flash tank, connects each distribution heat exchanger second entrance.
Roots blower has：Roots blower entrance connects flash tank first outlet；Roots blower exports, and connects desorber
4th entrance.
Wherein, the external unstripped gas with carbon dioxide enters water scrubber lower part via water scrubber second entrance, with warp
The top spray of the slave water scrubber fed by water scrubber first entrance and lower washing water counter current contacting, washing water absorption unstripped gas
In acid impurities gas and flue dust, remaining moves upwards and goes out via water scrubber first with unstripped gas of carbon dioxide
Mouth, gas-liquid separator entrance enter gas-liquid separator and carry out gas-liquid separation.
The liquid isolated in gas-liquid separator is discharged via gas-liquid separator second outlet, and the titanium dioxide isolated
Carbon raw material gas enters air-introduced machine via gas-liquid separator first outlet, air-introduced machine entrance, and under the action of air-introduced machine via
Air-introduced machine outlet, absorption tower first entrance enter absorption tower.
The CO 2 raw material gas entered in absorption tower with via absorption tower second entrance feed from the upper of absorption tower
Portion spray and under absorbent counter current contacting, carbon dioxide in absorbent absorbing carbon dioxide unstripped gas and become rich solution, it is remaining
Under unstripped gas move upwards.
Rich solution enters rich solution pump via absorption tower first outlet, rich solution pump intake, then under the action of rich solution pump via
Rich solution pump discharge, each distribution heat exchanger first entrance, which enter in each distribution heat exchanger, carries out heat exchange, with heating of absorbing heat.
The rich solution after heat exchange is carried out via each distribution heat exchanger first outlet, desorber first entrance and desorber second
Entrance enters desorber and by heating desorption, is decomposed into carbon dioxide and lean solution.
The carbon dioxide of decomposition is moved upwards and is discharged via desorber second outlet.
And lean solution enters reboiler via desorber first outlet, reboiler entrance and is heated up to boiling point, part
Lean solution becomes steam, and steam is re-introduced into desorber with for desorber via reboiler first outlet, desorber third entrance
Desorption provides heat.
The lean solution for not becoming steam enters flash tank via reboiler second outlet, flash tank entrance, into flash tank
Lean solution due to the pressure in flash tank reduces and most of lean solution instant vaporization becomes indirect steam, indirect steam is via flash distillation
Tank first outlet, roots blower entrance enter roots blower, and indirect steam is pressurized heating in roots blower, in roots blower
Under the action of exported via roots blower, the 4th entrance of desorber enter desorber with for desorber desorption heat is provided, wherein,
Desorber, reboiler, flash tank and roots blower form lean solution waste heat recovery circulation loop, and enter the lean solution in flash tank
In remaining sub-fraction lean solution enter each distribution via flash tank second outlet, each distribution heat exchanger second entrance and exchange heat
Device is simultaneously distributed heat exchanger second outlet, absorption tower second with being passed through after the aforementioned heat exchange of rich solution progress in each distribution heat exchanger by each
Entrance is returned in absorption tower, wherein respectively realizing the heat exchange between lean solution and rich solution in distribution heat exchanger.
Beneficial effects of the present invention are as follows：
In the carbon dioxide capture system according to the present invention based on UTILIZATION OF VESIDUAL HEAT IN, flowed out from desorber first outlet
Lean solution carry higher heat, and the present invention the carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN in desorber, reboiler,
Flash tank and roots blower form lean solution waste heat recovery circulation loop, and lean solution is in reboiler, flash tank and roots blower
The high steam of temperature is converted under effect and is again introduced into desorber and provides heat to the desorption of rich solution, is realized to more than lean solution
The efficient utilization of heat, reduces the waste of the energy.
Description of the drawings
Fig. 1 is the process flow diagram of the carbon dioxide capture system according to the present invention based on UTILIZATION OF VESIDUAL HEAT IN.
Wherein, the reference numerals are as follows：
11 water scrubbers
11A1 water scrubber first entrances
11B1 water scrubber first outlets
11A2 water scrubber second entrances
11B2 water scrubber second outlets
12 gas-liquid separators
12A gas-liquid separator entrances
12B1 gas-liquid separator first outlets
12B2 gas-liquid separator second outlets
13 air-introduced machines
13A air-introduced machine entrances
13B air-introduced machines export
14 absorption towers
14A1 absorption towers first entrance
14B1 absorption towers first outlet
14A2 absorption towers second entrance
14B2 absorption towers second outlet
14A3 absorption towers third entrance
The third outlet of 14B3 absorption towers
15 rich solution pumps
15A rich solution pump intakes
15B rich solution pump discharges
16 distribution heat exchangers
16A1 is distributed heat exchanger first entrance
16B1 is distributed heat exchanger first outlet
16A2 is distributed heat exchanger second entrance
16B2 is distributed heat exchanger second outlet
17 desorbers
17A1 desorber first entrances
17B1 desorber first outlets
17A2 desorber second entrances
17B2 desorber second outlets
17A3 desorber third entrances
17B3 desorbers third exports
The 4th entrance of 17A4 desorbers
The 5th entrance of 17A5 desorbers
18 reboilers
18A reboiler entrances
18B1 reboiler first outlets
18B2 reboiler second outlets
19 flash tanks
19A flash tank entrances
19B1 flash tank first outlets
19B2 flash tank second outlets
20 roots blowers
20A roots blower entrances
20B roots blowers export
21 evaporators
21A1 evaporator first entrances
21B1 evaporator first outlets
21A2 evaporator second entrances
22 return tank of 21B2 evaporators second outlet
22A return tank entrances
22B1 return tank first outlets
22B2 return tank second outlets
23 compressors
23A suctions port of compressor
23B compressor outlets
24 condensers
24A1 condenser first entrances
24B1 condenser first outlets
24A2 condenser second entrances
24B2 condenser second outlets
25 throttle valves
26 phase-splitters
26A phase-splitter entrances
26B1 phase-splitter first outlets
26B2 phase-splitter second outlets
27 dilute phases pump
27A dilute phase pump intakes
27B dilute phase pump discharges
28 mixers
28A1 mixer first entrances
28B mixer outlets
28A2 mixer second entrances
29 coolers
29A cooler entrances
29B cooler outlets
30 lean pumps
30A lean solution pump intakes
30B lean solution pump discharges
31 washing pumps
31A washs pump intake
31B washs pump discharge
32 fluid reservoirs
32A fluid reservoir entrances
32B fluid reservoirs export
Specific embodiment
It is described in detail the carbon dioxide capture system according to the present invention based on UTILIZATION OF VESIDUAL HEAT IN with reference to the accompanying drawings.
With reference to Fig. 1, the carbon dioxide capture system according to the present invention based on UTILIZATION OF VESIDUAL HEAT IN includes：Water scrubber 11, gas-liquid
Separator 12, air-introduced machine 13, absorption tower 14, rich solution pump 15, multiple distribution heat exchangers 16, desorber 17, reboiler 18, flash tank
19 and roots blower 20.
Water scrubber 11 has：Water scrubber first entrance 11A1, positioned at the top of water scrubber 11, for external washing flow
Enter；Water scrubber first outlet 11B1, positioned at the top of water scrubber 11；Water scrubber second entrance 11A2, under water scrubber 11
Portion enters for the external unstripped gas with carbon dioxide；Water scrubber second outlet 11B2, positioned at the bottom of water scrubber 11.
Gas-liquid separator 12 has：Gas-liquid separator entrance 12A, connection water scrubber first outlet 11B1；Gas-liquid separator
First outlet 12B1, positioned at the top of gas-liquid separator 12；Gas-liquid separator second outlet 12B2, positioned at gas-liquid separator 12
Bottom.
Air-introduced machine 13 has：Air-introduced machine entrance 13A, connection gas-liquid separator first outlet 12B1；Air-introduced machine exports 13B.
Absorption tower 14 has：Absorption tower first entrance 14A1, positioned at the bottom on absorption tower 14, connection air-introduced machine outlet 13B；
Absorption tower first outlet 14B1, positioned at the bottom on absorption tower 14；Absorption tower second entrance 14A2, positioned at the top on absorption tower 14；
Absorption tower second outlet 14B2, positioned at the top on absorption tower 14；Absorption tower third entrance 14A3, positioned at the top on absorption tower 14；
Absorption tower third outlet 14B3, positioned at the top on absorption tower 14.
Rich solution pump 15 has：Rich solution pump intake 15A connects absorption tower first outlet 14B1；And rich solution pump discharge 15B.
Carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN further includes：Multiple distribution heat exchangers 16, it is each to be distributed heat exchanger 16
Have：It is distributed heat exchanger first entrance 16A1, connection rich solution pump discharge 15B；It is distributed heat exchanger first outlet 16B1；Distribution heat exchange
Device second entrance 16A2；Heat exchanger second outlet 16B2 is distributed, connects absorption tower second entrance 14A2.
Desorber 17 has：Desorber first entrance 17A1 positioned at the top of desorber 17, connects multiple distribution heat exchangers
At least one of first outlet 16B1；Desorber first outlet 17B1, positioned at the bottom of desorber 17；Desorber second entrance
17A2 positioned at the middle part of desorber 17, connects at least one of multiple distribution heat exchanger first outlet 16B1；Desorber second
17B2 is exported, positioned at the top of desorber 17；Desorber third entrance 17A3, positioned at the lower part of desorber 17；Desorber the 4th
Entrance 17A4, positioned at the lower part of desorber 17.
Reboiler 18 has：Reboiler entrance 18A, connection desorber first outlet 17B1；Reboiler first outlet 18B1,
Connect desorber third entrance 17A3；Reboiler second outlet 18B2.
Flash tank 19 has：Flash tank entrance 19A, connection reboiler second outlet 18B2；Flash tank first outlet 19B1,
Positioned at the top of flash tank 19；Flash tank second outlet 19B2 positioned at the bottom of flash tank 19, connects each distribution heat exchanger second
Entrance 16A2.
Roots blower 20 has：Roots blower entrance 20A, connection flash tank first outlet 19B1；Roots blower exports
20B, the 4th entrance 17A4 of connection desorber.
Wherein, the external unstripped gas with carbon dioxide enters via water scrubber second entrance 11A2 under water scrubber 11
Portion, with the top spray of the slave water scrubber 11 that is fed via water scrubber first entrance 11A1 and under washing water counter current contacting, water
Wash water absorbs acid impurities gas (such as the SO in the unstripped gas with carbon dioxideX、NOX) and flue dust, remaining carries dioxy
The unstripped gas for changing carbon moves upwards and enters gas-liquid separator via water scrubber first outlet 11B1, gas-liquid separator entrance 12A
12 and carry out gas-liquid separation；
The liquid isolated in gas-liquid separator 12 is discharged via gas-liquid separator second outlet 12B2, and is isolated
CO 2 raw material gas enters air-introduced machine 13, and in air inducing via gas-liquid separator first outlet 12B1, air-introduced machine entrance 13A
Under the action of machine 13 absorption tower 14 is entered via air-introduced machine outlet 13B, absorption tower first entrance 14A1；
The CO 2 raw material gas that enters in absorption tower 14 with via absorption tower second entrance 14A2 feed from absorption
The top spray of tower 14 and under absorbent counter current contacting, carbon dioxide in absorbent absorbing carbon dioxide unstripped gas and become
Rich solution, remaining unstripped gas move upwards；
Rich solution enters rich solution pump 15 via absorption tower first outlet 14B1, rich solution pump intake 15A, then in rich solution pump 15
Enter in each distribution heat exchanger 16 via rich solution pump discharge 15B, each distribution heat exchanger first entrance 16A1 under effect and carry out hot friendship
It changes, with heating of absorbing heat；
The rich solution after heat exchange is carried out to conciliate via each distribution heat exchanger first outlet 16B1, desorber first entrance 17A1
It inhales tower second entrance 17A2 and enters desorber 17 and by heating desorption, be decomposed into carbon dioxide and lean solution；
The carbon dioxide of decomposition is moved upwards and is discharged via desorber second outlet 17B2；
And lean solution enter reboiler 18 via desorber first outlet 17B1, reboiler entrance 18A and be heated up to
Boiling point, part lean solution become steam, and steam is re-introduced into via reboiler first outlet 18B1, desorber third entrance 17A3
Desorber 17 provides heat (carrying out a waste heat recovery first, reduce the waste of the energy) to be desorbed for desorber 17；
The lean solution for not becoming steam enters flash tank 19 via reboiler second outlet 18B2, flash tank entrance 19A, enters
Lean solution in flash tank 19 due to the pressure in flash tank 19 reduces and most of lean solution instant vaporization becomes indirect steam, it is secondary
Steam enters roots blower 20 via flash tank first outlet 19B1, roots blower entrance 20A, and indirect steam is in roots blower 20
In be pressurized heating, enter solution via roots blower outlet 20B, the 4th entrance 17A4 of desorber under the action of roots blower 20
Tower 17 is inhaled to provide heat for the desorption of desorber 17, wherein, desorber 17, reboiler 18, flash tank 19 and roots blower 20
Lean solution waste heat recovery circulation loop is formed, and enters the remaining sub-fraction lean solution in the lean solution in flash tank 19 via flash distillation
Tank second outlet 19B2, each distribution heat exchanger second entrance 16A2 enter each distribution heat exchanger 16 and are distributed heat exchanger 16 with each
It passes through after the interior aforementioned heat exchange of rich solution progress and is returned to by each distribution heat exchanger second outlet 16B2, absorption tower second entrance 14A2
In absorption tower 14, wherein respectively realizing the heat exchange between lean solution and rich solution in distribution heat exchanger 16.
In the carbon dioxide capture system according to the present invention based on UTILIZATION OF VESIDUAL HEAT IN, flowed from desorber first outlet 17B1
The lean solution gone out carry higher heat, and the present invention the carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN in desorber 17,
Reboiler 18, flash tank 19 and roots blower 20 form lean solution waste heat recovery circulation loop, and lean solution is in reboiler 18, flash tank
19 and roots blower 20 under the action of be converted into the high steam of temperature and be again introduced into desorber 17 and the desorption of rich solution is carried
Heating load realizes the efficient utilization to lean solution waste heat, reduces the waste of the energy.
Desorber 17 also has：The 5th entrance 17A5 of desorber, positioned at the top of desorber 17；Desorber third exports
17B3, positioned at the middle part of desorber 17.
The carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN further includes：Evaporator 21, return tank 22, compressor
23rd, condenser 24 and throttle valve 25.
Evaporator 21 has：Evaporator first entrance 21A1, connection desorber second outlet 17B2；Evaporator first outlet
21B1；Evaporator second entrance 21A2；And evaporator second outlet 21B2.
Return tank 22 has：Return tank entrance 22A, connection evaporator first outlet 21B1；Return tank first outlet 22B1；
And return tank second outlet 22B2.
Compressor 23 has：Suction port of compressor 23A, connection evaporator second outlet 21B2；Compressor outlet 23B.
Condenser 24 has：Condenser first entrance 24A1, connection compressor outlet 23B；Condenser first outlet 24B1；
Condenser second entrance 24A2, connection desorber third outlet 17B3；And condenser second outlet 24B2, connection desorber the
Five entrance 17A5.
Throttle valve 25 is set between condenser 24 and evaporator 21, the controlled connection condenser first outlet 24B1 in one end,
The controlled connection evaporator second entrance 21A2 of the other end.
Wherein, from the desorber second outlet 17B2 carbon dioxide discharged steaming is entered via evaporator first entrance 21A1
The worker quality liquid sent out in device 21, with evaporator 21 carries out heat exchange；
Carbon dioxide heat release cools down, and enters return tank 22 via evaporator first outlet 21B1, return tank entrance 22A,
Carbon dioxide is detached with the vapor carried in return tank 22, and carbon dioxide gas is discharged from return tank first outlet 22B1,
Condensed water is discharged from return tank second outlet 22B2；
Worker quality liquid heat absorption heating becomes working substance steam；
Working substance steam enters compressor 23 via evaporator second outlet 21B2, suction port of compressor 23A, and compressor 23 is right
Working substance steam is compressed, and becomes superheated steam by compressed working substance steam increasing temperature and pressure；
Superheated steam enters condenser 24 via compressor outlet 23B, condenser first entrance 24A1, and from desorber
Third outlet 17B3 outflow rich solution via condenser second entrance 24A2 enter condenser 24 and with the overheat in condenser 24
Steam carries out heat exchange, and rich solution heat absorption heats up and is desorbed, desorbs for carbon dioxide and lean solution and via condenser second outlet
24B2, the 5th entrance 17A5 of desorber are again introduced into desorber 17, and superheated steam heat release cooling becomes high-pressure working medium liquid；
High-pressure working medium liquid flows into throttle valve 25 and is depressurized as low pressure working fluid liquid, and low pressure working fluid liquid is throttling
Evaporator 21 is re-introduced into via evaporator second entrance 21A2 under the action of valve 25, so as to complete one cycle process,
In, desorber 17, evaporator 21, compressor 23, condenser 24 and throttle valve 25 form carbon dioxide-vapor waste heat recovery and follow
Loop back path.
In the carbon dioxide capture system according to the present invention based on UTILIZATION OF VESIDUAL HEAT IN, arranged from desorber second outlet 17B2
The carbon dioxide-vapor gone out carry higher heat, and the present invention the carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN in solution
Tower 17, evaporator 21, compressor 23, condenser 24 and the formation carbon dioxide-vapor waste heat recovery of throttle valve 25 is inhaled to be recycled back to
Road, carbon dioxide-vapor transfer heat to the working medium in circulation loop, and working medium becomes under the action of evaporator and compressor
Superheated steam, superheated steam heat up and are desorbed as lean solution and titanium dioxide with rich solution heat exchange, rich solution heat absorption in condenser 24
Carbon, lean solution and carbon dioxide after rich solution desorption are flow back into again in desorber 17, it is thus achieved that the top to desorber 17
The recycling of the heat of the carbon dioxide-vapor of discharge reduces the waste of the energy.
In the carbon dioxide capture system according to the present invention based on UTILIZATION OF VESIDUAL HEAT IN, the carbon dioxide based on UTILIZATION OF VESIDUAL HEAT IN
Trapping system has multiple distribution heat exchangers 16, between multiple distribution heat exchangers 16 can there are many connecting mode, specifically,
In one embodiment, with reference to Fig. 1, the carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN includes two distribution heat exchangers 16, one point
The distribution heat exchanger first outlet 16B1 connections desorber first entrance 17A1 and desorber second entrance 17A2 of cloth heat exchanger 16
And it is distributed heat exchanger second entrance 16A2 connection flash tank second outlets 19B2；
The distribution heat exchanger first outlet 16B1 connection desorber first entrance 17A1 reconciliation of another distribution heat exchanger 16
It inhales tower second entrance 17A2 and is distributed the one distribution heat exchanger for being distributed heat exchanger 16 of heat exchanger second entrance 16A2 connections
Second outlet 16B2.Lean solution carries out heat exchange with rich solution in each distribution heat exchanger 16, significantly reduces lean solution, the temperature of rich solution
Difference is spent, heat exchange efficiency is improved, and fully recycled the heat of lean solution, further reduces the waste of lean solution heat；In addition,
Using distributed heat exchanger 16, each distribution heat exchanger first outlet 16B1 connection desorber first entrances for being distributed heat exchanger 16
17A1 and desorber second entrance 17A2, rich solution branch to the top and middle part of desorber 17 via distribution heat exchanger 16, can
Effectively reduce the loss of heat and evaporated quantity of water.Specifically, rich solution is fully entered via single heat exchanger exit in the prior art
To the top of desorber 17, a part of steam can be flashed off due to being depressured suddenly when rich solution enters the top of desorber 17,
The steam flashed off can thereby result in a large amount of water directly from the desorber second outlet 17B2 discharges positioned at 17 top of desorber
Loss；If rich solution is all introduced into the middle part of desorber 17 via single heat exchanger exit, desorption not exclusively (i.e. air lift can be caused
The height of decomposition reduces), therefore the present invention branches to the top and middle part of desorber 17 using distribution heat exchanger 16, effectively
Reduce the loss of heat and evaporated quantity of water.
The carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN further includes：Phase-splitter 26, dilute phase pump 27, mixer 28,
Cooler 29 and lean pump 30.
Phase-splitter 26 has：Phase-splitter entrance 26A connects absorption tower first outlet 14B1；Phase-splitter first outlet 26B1；
And phase-splitter second outlet 26B2.
Dilute phase pump 27 has：Dilute phase pump intake 27A, connection phase-splitter second outlet 26B2；Dilute phase pump discharge 27B.
Mixer 28 has：Mixer first entrance 28A1, connection dilute phase pump discharge 27B；Mixer outlet 28B；Mixing
Device second entrance 28A2.
Cooler 29 has：Cooler entrance 29A, connection mixer outlet 28B；Cooler outlet 29B connects absorption tower
Second entrance 14A2.
Lean pump 30 has：Lean solution pump intake 30A connects each distribution heat exchanger second outlet 16B2；And lean solution pumps out
Mouth 30B, connection mixer second entrance 28A2.
Wherein, rich solution is divided into two layers up and down by phase-splitter 26, the upper strata dilute phase liquid few for carbon dioxide content, lower floor two
Concentrated phase liquid more than content of carbon oxide, the dilute phase liquid on upper strata is via phase-splitter second outlet 26B2, dilute phase pump intake 27A and then dilute phase
Pump 27 is pumped into via dilute phase pump discharge 27B, mixer first entrance 28A1 in mixer 28 under the action of dilute phase pump 27,
Concentrated phase liquid more than the carbon dioxide content of lower floor is as the rich solution for entering rich solution pump 15 via rich solution pump intake 15A；
The lean solution after heat exchange is carried out via each distribution heat exchanger second outlet with rich solution in each distribution heat exchanger 16
16B2, lean solution pump intake 30A are entered in lean pump 30, and lean solution is via lean solution pump discharge 30B, mixed under the action of lean pump 30
Clutch second entrance 28A2 enters mixer 28 and the dilute phase liquid few with the carbon dioxide content in mixer 28 mixes；
Mixed liquid enters cooler 29, then via cooler via mixer outlet 28B, cooler entrance 29A
Outlet 29B, absorption tower second entrance 14A2 are re-introduced into absorption tower 14, to be recycled as absorbent, wherein, it absorbs
Tower 14, phase-splitter 26, dilute phase pump 27, mixer 28, cooler 29 form an absorbent recycling circulation loop；And absorption tower
14th, phase-splitter 26, rich solution pump 15, each distribution heat exchanger 16, desorber 17, reboiler 18, flash tank 19, lean pump 30, mixing
Device 28 and cooler 29 form another absorbent recycling circulation loop.The design of two absorbent recycling circulation loops is effective
The extraction raffinate in the carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN is utilized in ground, reduces the waste of the energy.
Absorption tower 14 also has：Absorption tower third entrance 14A3, positioned at the top on absorption tower 14；Absorption tower third outlet
14B3, positioned at the top on absorption tower 14；
Washing pump 31 has：Wash pump intake 31A, connection absorption tower third outlet 14B3；Wash pump discharge 31B, connection
Absorption tower third entrance 14A3；
Wherein, the unabsorbed exhaust gas in absorption tower 14 moves upwards and via washing pump discharge 31B, absorption tower third
Entrance 14A3 enters the water lotion counter current contacting at the top of absorption tower 14, the contained absorbent and carbon dioxide reaction in exhaust gas
The absorbent steam while being Amine Solutions (such as absorbent the amine steam that generates) of generation is absorbed, and remaining exhaust gas via
Absorption tower second outlet 14B2 is discharged.
Carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN further includes fluid reservoir 32.
Fluid reservoir 32 has：Fluid reservoir entrance 32A provides fresh absorbent from external；Fluid reservoir exports 32B, connection
Absorption tower second entrance 14A2；
Wherein, external fresh absorbent enters fluid reservoir 32 via fluid reservoir entrance 32A and is exported via fluid reservoir
32B, absorption tower second entrance 14A2 enter absorption tower 14, to provide sufficient absorbent for absorption tower 14.
Claims (6)
1. a kind of carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN, including：
Water scrubber (11), has：
Water scrubber first entrance (11A1) positioned at the top of water scrubber (11), is flowed into for external washing water；
Water scrubber first outlet (11B1), positioned at the top of water scrubber (11)；
Water scrubber second entrance (11A2), positioned at the lower part of water scrubber (11), for the external unstripped gas with carbon dioxide into
Enter；
Water scrubber second outlet (11B2), positioned at the bottom of water scrubber (11)；
Gas-liquid separator (12), has：
Gas-liquid separator entrance (12A), connection water scrubber first outlet (11B1)；
Gas-liquid separator first outlet (12B1), positioned at the top of gas-liquid separator (12)；
Gas-liquid separator second outlet (12B2), positioned at the bottom of gas-liquid separator (12)；Air-introduced machine (13), has：
Air-introduced machine entrance (13A), connection gas-liquid separator first outlet (12B1)；
Air-introduced machine exports (13B)；
Absorption tower (14), has：
Absorption tower first entrance (14A1), positioned at the bottom of absorption tower (14), connection air-introduced machine outlet (13B)；
Absorption tower first outlet (14B1), positioned at the bottom of absorption tower (14)；
Absorption tower second entrance (14A2), positioned at the top of absorption tower (14)；
Absorption tower second outlet (14B2), positioned at the top of absorption tower (14)；
Absorption tower third entrance (14A3), positioned at the top of absorption tower (14)；
Absorption tower third outlet (14B3), positioned at the top of absorption tower (14)；
Rich solution pump (15), has：
Rich solution pump intake (15A), connection absorption tower first outlet (14B1)；And
Rich solution pump discharge (15B)；
It is characterized in that, the carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN further includes：
Multiple distribution heat exchangers (16), being respectively distributed heat exchanger (16) has：
It is distributed heat exchanger first entrance (16A1), connection rich solution pump discharge (15B)；
It is distributed heat exchanger first outlet (16B1)；
It is distributed heat exchanger second entrance (16A2)；
It is distributed heat exchanger second outlet (16B2), connection absorption tower second entrance (14A2)；
Desorber (17), has：
Desorber first entrance (17A1) positioned at the top of desorber (17), connects multiple distribution heat exchanger first outlets
At least one of (16B1)；
Desorber first outlet (17B1), positioned at the bottom of desorber (17)；
Desorber second entrance (17A2) positioned at the middle part of desorber (17), connects multiple distribution heat exchanger first outlets
At least one of (16B1)；
Desorber second outlet (17B2), positioned at the top of desorber (17)；
Desorber third entrance (17A3), positioned at the lower part of desorber (17)；
The 4th entrance (17A4) of desorber, positioned at the lower part of desorber (17)；
Reboiler (18), has：
Reboiler entrance (18A), connection desorber first outlet (17B1)；
Reboiler first outlet (18B1), connection desorber third entrance (17A3)；
Reboiler second outlet (18B2)；
Flash tank (19), has：
Flash tank entrance (19A), connection reboiler second outlet (18B2)；
Flash tank first outlet (19B1), positioned at the top of flash tank (19)；
Flash tank second outlet (19B2) positioned at the bottom of flash tank (19), connects each distribution heat exchanger second entrance (16A2)；
Roots blower (20), has：
Roots blower entrance (20A), connection flash tank first outlet (19B1)；
Roots blower exports (20B), connects the 4th entrance (17A4) of desorber；
Wherein, the external unstripped gas with carbon dioxide via water scrubber second entrance (11A2) under water scrubber (11)
Portion, with the top spray of the slave water scrubber (11) that is fed via water scrubber first entrance (11A1) and lower washing water countercurrently connects
It touches, washing water absorbs the acid impurities gas and flue dust in unstripped gas, remaining unstripped gas with carbon dioxide moves upwards
And it goes forward side by side promoting the circulation of qi liquid point into gas-liquid separator (12) via water scrubber first outlet (11B1), gas-liquid separator entrance (12A)
From；
The liquid isolated in gas-liquid separator (12) is discharged via gas-liquid separator second outlet (12B2), and is isolated
CO 2 raw material gas enters air-introduced machine (13) via gas-liquid separator first outlet (12B1), air-introduced machine entrance (13A), and
(13B) is exported via air-introduced machine, absorption tower first entrance (14A1) enters absorption tower (14) under the action of air-introduced machine (13)；
The CO 2 raw material gas that enters in absorption tower (14) with via absorption tower second entrance (14A2) feed from absorption
The top spray of tower (14) and under absorbent counter current contacting, carbon dioxide in absorbent absorbing carbon dioxide unstripped gas and become
For rich solution, remaining unstripped gas moves upwards；
Rich solution via absorption tower first outlet (14B1), rich solution pump intake (15A) into rich solution pump (15), then in rich solution pump
(15) enter each distribution heat exchanger via rich solution pump discharge (15B), each distribution heat exchanger first entrance (16A1) under the action of
(16) heat exchange is carried out in, with heating of absorbing heat；
The rich solution after heat exchange is carried out to conciliate via each distribution heat exchanger first outlet (16B1), desorber first entrance (17A1)
Tower second entrance (17A2) is inhaled into desorber (17) and by heating desorption, is decomposed into carbon dioxide and lean solution；
The carbon dioxide of decomposition is moved upwards and is discharged via desorber second outlet (17B2)；
And lean solution is heated up via desorber first outlet (17B1), reboiler entrance (18A) into reboiler (18)
To boiling point, part lean solution becomes steam, steam via reboiler first outlet (18B1), desorber third entrance (17A3) again
Desorber (17) is entered to provide heat for desorber (17) desorption；
Do not become the lean solution of steam via reboiler second outlet (18B2), flash tank entrance (19A) into flash tank (19), into
Enter lean solution in flash tank (19) due to the pressure in flash tank (19) reduces and most of lean solution instant vaporization becomes secondary steaming
Vapour, indirect steam is via flash tank first outlet (19B1), roots blower entrance (20A) into roots blower (20), secondary steaming
Vapour is pressurized heating in roots blower (20), and (20B), desorption are exported via roots blower under the action of roots blower (20)
The 4th entrance (17A4) of tower provides heat into desorber (17) to be desorbed for desorber (17), wherein, desorber (17) boils again
Device (18), flash tank (19) and roots blower (20) form lean solution waste heat recovery circulation loop, and enter in flash tank (19)
Lean solution in remaining sub-fraction lean solution via flash tank second outlet (19B2), each distribution heat exchanger second entrance
(16A2) enter each distribution heat exchanger (16) and with the rich solution in each distribution heat exchanger (16) pass through after aforementioned heat exchange by
Each distribution heat exchanger second outlet (16B2), absorption tower second entrance (14A2) are back in absorption tower (14), wherein each distribution
The heat exchange between lean solution and rich solution is realized in heat exchanger (16).
2. the carbon dioxide capture system according to claim 1 based on UTILIZATION OF VESIDUAL HEAT IN, which is characterized in that
Desorber (17) also has：
The 5th entrance (17A5) of desorber, positioned at the top of desorber (17)；
Desorber third exports (17B3), positioned at the middle part of desorber (17)；
The carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN further includes：
Evaporator (21), has：
Evaporator first entrance (21A1), connection desorber second outlet (17B2)；
Evaporator first outlet (21B1)；
Evaporator second entrance (21A2)；And
Evaporator second outlet (21B2)；
Return tank (22), has：
Return tank entrance (22A), connection evaporator first outlet (21B1)；
Return tank first outlet (22B1)；And
Return tank second outlet (22B2)；
Compressor (23), has：
Suction port of compressor (23A), connection evaporator second outlet (21B2)；
Compressor outlet (23B)；
Condenser (24), has：
Condenser first entrance (24A1), connection compressor outlet (23B)；
Condenser first outlet (24B1)；
Condenser second entrance (24A2), connection desorber third outlet (17B3)；And condenser second outlet (24B2), even
The 5th entrance (17A5) of logical desorber；
Throttle valve (25) is set between condenser (24) and evaporator (21), the controlled connection condenser first outlet in one end
(24B1), the controlled connection evaporator second entrance (21A2) of the other end；
Wherein, the carbon dioxide discharged from desorber second outlet (17B2) enters steaming via evaporator first entrance (21A1)
Device (21) is sent out, heat exchange is carried out with the worker quality liquid in evaporator (21)；
Carbon dioxide heat release cools down, and via evaporator first outlet (21B1), return tank entrance (22A) into return tank
(22), carbon dioxide is detached with the vapor carried in return tank (22), and carbon dioxide gas is from return tank first outlet
(22B1) is discharged, and condensed water is discharged from return tank second outlet (22B2)；
Worker quality liquid heat absorption heating becomes working substance steam；
Working substance steam enters compressor (23), compressor via evaporator second outlet (21B2), suction port of compressor (23A)
(23) working substance steam is compressed, becomes superheated steam by compressed working substance steam increasing temperature and pressure；
Superheated steam enters condenser (24) via compressor outlet (23B), condenser first entrance (24A1), and from desorption
The rich solution of tower third outlet (17B3) outflow is via condenser second entrance (24A2) into condenser (24) and and condenser
(24) superheated steam in carries out heat exchange, and rich solution heat absorption heats up and is desorbed, desorbs for carbon dioxide and lean solution and via cold
Condenser second outlet (24B2), the 5th entrance (17A5) of desorber are again introduced into desorber (17), and superheated steam heat release is dropped
Temperature becomes high-pressure working medium liquid；
High-pressure working medium liquid flows into throttle valve (25) and is depressurized as low pressure working fluid liquid, and low pressure working fluid liquid is in throttle valve
(25) evaporator (21) is re-introduced into via evaporator second entrance (21A2) under the action of, so as to complete one cycle mistake
Journey, wherein, desorber (17), evaporator (21), compressor (23), condenser (24) and throttle valve (25) form carbon dioxide
Steam heat recovery circulation loop.
3. the carbon dioxide capture system according to claim 1 based on UTILIZATION OF VESIDUAL HEAT IN, which is characterized in that
Carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN includes two distribution heat exchangers (16),
Distribution heat exchanger first outlet (16B1) the connection desorber first entrance (17A1) of one distribution heat exchanger (16) is conciliate
It inhales tower second entrance (17A2) and is distributed heat exchanger second entrance (16A2) connection flash tank second outlet (19B2)；
Another distribution heat exchanger (16) distribution heat exchanger first outlet (16B1) connection desorber first entrance (17A1) and
Desorber second entrance (17A2) and be distributed heat exchanger second entrance (16A2) connection it is one distribution heat exchanger (16) point
Cloth heat exchanger second outlet (16B2).
4. the carbon dioxide capture system according to claim 3 based on UTILIZATION OF VESIDUAL HEAT IN, which is characterized in that described based on remaining
The carbon dioxide capture system of heat utilization further includes：
Phase-splitter (26), has：
Phase-splitter entrance (26A), connection absorption tower first outlet (14B1)；
Phase-splitter first outlet (26B1)；And
Phase-splitter second outlet (26B2)；
Dilute phase pumps (27), has：
Dilute phase pump intake (27A), connection phase-splitter second outlet (26B2)；
Dilute phase pump discharge (27B)；
Mixer (28), has：
Mixer first entrance (28A1), connection dilute phase pump discharge (27B)；
Mixer outlet (28B)；
Mixer second entrance (28A2)；
Cooler (29), has：
Cooler entrance (29A), connection mixer outlet (28B)；
Cooler outlet (29B), connection absorption tower second entrance (14A2)；
Lean pump (30), has：
Lean solution pump intake (30A) connects each distribution heat exchanger second outlet (16B2)；And lean solution pump discharge (30B), connection are mixed
Clutch second entrance (28A2)；
Wherein, rich solution is divided into two layers up and down by phase-splitter (26), and the upper strata dilute phase liquid few for carbon dioxide content, lower floor is dioxy
Change the concentrated phase liquid more than carbon content, the dilute phase liquid on upper strata is via phase-splitter second outlet (26B2), dilute phase pump intake (27A) and then dilute
Mutually pump (27) is pumped under the action of dilute phase pumps (27) via dilute phase pump discharge (27B), mixer first entrance (28A1) mixed
In clutch (28), concentrated phase liquid more than the carbon dioxide content of lower floor is used as via rich solution pump intake (15A) into rich solution pump (15)
Rich solution；
The lean solution after heat exchange is carried out via each distribution heat exchanger second outlet with rich solution in each distribution heat exchanger (16)
(16B2), lean solution pump intake (30A) are entered in lean pump (30), and lean solution is pumped out via lean solution under the action of lean pump (30)
Mouthful (30B), mixer second entrance (28A2) enter mixer (28) and few with the carbon dioxide content in mixer (28)
Dilute phase liquid mixing；
Mixed liquid via mixer outlet (28B), cooler entrance (29A) into cooler (29), then via cooling
Device outlet (29B), absorption tower second entrance (14A2) are re-introduced into absorption tower (14), to be recycled as absorbent,
Wherein, absorption tower (14), phase-splitter (26), dilute phase pump (27), mixer (28), cooler (29) form an absorbent recycling
Circulation loop；And absorption tower (14), phase-splitter (26), rich solution pump (15), respectively distribution heat exchanger (16), desorber (17), boil again
Device (18), flash tank (19), lean pump (30), mixer (28) and cooler (29) form another absorbent recycling cycle
Circuit.
5. the carbon dioxide capture system according to claim 1 based on UTILIZATION OF VESIDUAL HEAT IN, which is characterized in that
Absorption tower (14) also has：
Absorption tower third entrance (14A3), positioned at the top of absorption tower (14)；
Absorption tower third outlet (14B3), positioned at the top of absorption tower (14)；
Washing pump (31), has：
Wash pump intake (31A), connection absorption tower third outlet (14B3)；
Wash pump discharge (31B), connection absorption tower third entrance (14A3)；
Wherein, the unabsorbed exhaust gas in absorption tower (14) moves upwards and via washing pump discharge (31B), absorption tower third
Entrance (14A3) is into the water lotion counter current contacting at the top of absorption tower (14), the contained absorbent and carbon dioxide in exhaust gas
The absorbent steam that reaction generates is absorbed, and remaining exhaust gas is discharged via absorption tower second outlet (14B2).
6. the carbon dioxide capture system according to claim 1 based on UTILIZATION OF VESIDUAL HEAT IN, which is characterized in that
Carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN further includes：
Fluid reservoir (32), has：
Fluid reservoir entrance (32A) provides fresh absorbent from external；
Fluid reservoir exports (32B), connection absorption tower second entrance (14A2)；
Wherein, external fresh absorbent is exported into fluid reservoir (32) and via fluid reservoir entrance (32A) via fluid reservoir
(32B), absorption tower second entrance (14A2) enter absorption tower (14), to provide sufficient absorbent for absorption tower (14).
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| CN109999618A (en) * | 2019-04-25 | 2019-07-12 | 华能国际电力股份有限公司 | The separation system and method for carbon dioxide in a kind of mesohigh gas source |
| CN110124464A (en) * | 2019-06-26 | 2019-08-16 | 中石化石油工程技术服务有限公司 | Carbon dioxide capture system based on Steam-injection Boiler Burning Pulverized Coal system power supply |
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