CN108236831B - Carbon dioxide trapping system based on waste heat utilization - Google Patents
Carbon dioxide trapping system based on waste heat utilization Download PDFInfo
- Publication number
- CN108236831B CN108236831B CN201711181818.8A CN201711181818A CN108236831B CN 108236831 B CN108236831 B CN 108236831B CN 201711181818 A CN201711181818 A CN 201711181818A CN 108236831 B CN108236831 B CN 108236831B
- Authority
- CN
- China
- Prior art keywords
- outlet
- inlet
- liquid
- carbon dioxide
- tower
- 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.)
- Active
Links
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 186
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 93
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 93
- 239000002918 waste heat Substances 0.000 title claims abstract description 50
- 239000007788 liquid Substances 0.000 claims abstract description 182
- 238000003795 desorption Methods 0.000 claims abstract description 141
- 238000010521 absorption reaction Methods 0.000 claims abstract description 92
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 78
- 238000011084 recovery Methods 0.000 claims abstract description 15
- 239000007789 gas Substances 0.000 claims description 35
- 239000006096 absorbing agent Substances 0.000 claims description 30
- 230000002745 absorbent Effects 0.000 claims description 24
- 239000002250 absorbent Substances 0.000 claims description 24
- 238000010992 reflux Methods 0.000 claims description 23
- 238000005406 washing Methods 0.000 claims description 20
- 239000002994 raw material Substances 0.000 claims description 8
- 238000000034 method Methods 0.000 claims description 7
- 238000004891 communication Methods 0.000 claims description 4
- 238000009835 boiling Methods 0.000 claims description 3
- 239000000428 dust Substances 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 239000010808 liquid waste Substances 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 239000000779 smoke Substances 0.000 claims description 3
- 239000002253 acid Substances 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- 239000002699 waste material Substances 0.000 abstract description 9
- 239000012530 fluid Substances 0.000 description 3
- 150000001412 amines Chemical class 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000126 substance 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
- B01D53/18—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 invention provides a carbon dioxide trapping system based on waste heat utilization, which comprises a water scrubber, a gas-liquid separator, an induced draft fan, an absorption tower, a rich liquid pump, a plurality of distributed heat exchangers, a desorption tower, a reboiler, a flash tank and a Roots blower. In the carbon dioxide trapping system based on waste heat utilization, the lean solution flowing out of the first outlet of the desorption tower has higher heat, and the desorption tower, the reboiler, the flash tank and the Roots blower in the carbon dioxide trapping system based on waste heat utilization form a lean solution waste heat recovery circulation loop, so that the lean solution is converted into high-temperature steam under the action of the reboiler, the flash tank and the Roots blower to be fed into the desorption tower again to provide heat for desorption of the rich solution, thereby realizing high-efficiency utilization of the lean solution waste heat and reducing energy waste.
Description
Technical Field
The invention relates to the field of waste heat recovery, in particular to a carbon dioxide capturing system based on waste heat utilization.
Background
At present, the overall energy consumption of a carbon dioxide capturing system by a chemical absorption method is higher, and the main point is that the carbon dioxide absorption process needs to be carried out at a lower temperature, and the carbon dioxide desorption process needs to be completed at a higher temperature. In the process, a plurality of places of energy are not fully utilized, wherein the energy mainly comprises the waste heat of the lean solution at the bottom of the desorption tower and the waste heat of the regenerated gas at the top of the desorption tower, and the heat is not effectively recycled, so that the energy utilization rate is low. Thereby causing a great waste of heat energy.
Disclosure of Invention
In view of the problems existing in the background art, the invention aims to provide a carbon dioxide capturing system based on waste heat utilization, which can recover waste heat of lean solution at the bottom of a desorption tower, realize effective utilization of the waste heat of the lean solution and reduce energy waste.
In order to achieve the above object, the present invention provides a carbon dioxide capturing system based on waste heat utilization, comprising: the system comprises a water scrubber, a gas-liquid separator, an induced draft fan, an absorption tower, a rich liquid pump, a plurality of distributed heat exchangers, a desorption tower, a reboiler, a flash tank and a Roots blower.
The water washing tower comprises: a first inlet of the water washing tower is positioned at the upper part of the water washing tower and used for flowing in external water washing water; the first outlet of the water washing tower is positioned at the top of the water washing tower; a second inlet of the water scrubber is positioned at the lower part of the water scrubber and is used for entering external raw material gas with carbon dioxide; the second outlet of the water washing tower is positioned at the bottom of the water washing tower.
The gas-liquid separator has: the inlet of the gas-liquid separator is communicated with the first outlet of the water scrubber; the first outlet of the gas-liquid separator is positioned at the top of the gas-liquid separator; the second outlet of the gas-liquid separator is positioned at the bottom of the gas-liquid separator.
The induced draft fan has: an inlet of the induced draft fan is communicated with a first outlet of the gas-liquid separator; and an outlet of the induced draft fan.
The absorption tower has: the first inlet of the absorption tower is positioned at the bottom of the absorption tower and is communicated with the outlet of the induced draft fan; the first outlet of the absorption tower is positioned at the bottom of the absorption tower; the second inlet of the absorption tower is positioned at the upper part of the absorption tower; the second outlet of the absorption tower is positioned at the top of the absorption tower; the third inlet of the absorption tower is positioned at the top of the absorption tower; and a third outlet of the absorption tower is positioned at the upper part of the absorption tower.
The rich liquid pump comprises: the rich liquid pump inlet is communicated with the first outlet of the absorption tower; and a rich liquid pump outlet.
Carbon dioxide capture system based on waste heat utilization still includes: a plurality of distributed heat exchangers, each distributed heat exchanger having: the first inlet of the distribution heat exchanger is communicated with the rich liquid pump outlet; a first outlet of the distributed heat exchanger; a distributed heat exchanger second inlet; and the second outlet of the distribution heat exchanger is communicated with the second inlet of the absorption tower.
The desorption column has: a first inlet of the desorption tower is positioned at the upper part of the desorption tower and is communicated with at least one of a plurality of first outlets of the distribution heat exchangers; the first outlet of the desorption tower is positioned at the bottom of the desorption tower; the second inlet of the desorption tower is positioned in the middle of the desorption tower and is communicated with at least one of the first outlets of the plurality of distribution heat exchangers; the second outlet of the desorption tower is positioned at the top of the desorption tower; a third inlet of the desorption tower is positioned at the lower part of the desorption tower; and a fourth inlet of the desorption tower is positioned at the lower part of the desorption tower.
The reboiler has: a reboiler inlet communicated with the first outlet of the desorption tower; a first outlet of the reboiler is communicated with a third inlet of the desorption tower; and a reboiler second outlet.
The flash tank has: the flash tank inlet is communicated with the reboiler second outlet; the first outlet of the flash tank is positioned at the top of the flash tank; the second outlet of the flash tank is positioned at the bottom of the flash tank and communicated with the second inlets of the distribution heat exchangers.
The Roots blower has: the Roots blower inlet is communicated with the first outlet of the flash tank; and the outlet of the Roots blower is communicated with the fourth inlet of the desorption tower.
The external raw material gas with carbon dioxide enters the lower part of the water scrubber through the second inlet of the water scrubber, and is in countercurrent contact with water scrubber sprayed from the upper part of the water scrubber and supplied through the first inlet of the water scrubber, the water scrubber absorbs acid impurity gas and smoke dust in the raw material gas, and the rest raw material gas with carbon dioxide moves upwards and enters the gas-liquid separator through the first outlet of the water scrubber and the inlet of the gas-liquid separator for gas-liquid separation.
The liquid separated in the gas-liquid separator is discharged through the second outlet of the gas-liquid separator, and the separated carbon dioxide raw gas enters the induced draft fan through the first outlet of the gas-liquid separator and the inlet of the induced draft fan, and enters the absorption tower through the outlet of the induced draft fan and the first inlet of the absorption tower under the action of the induced draft fan.
The carbon dioxide raw gas introduced into the absorber is in countercurrent contact with the absorbent sprayed from the upper part of the absorber and fed through the second inlet of the absorber, the absorbent absorbs carbon dioxide in the carbon dioxide raw gas to become rich liquid, and the rest raw gas moves upward.
The rich liquid enters the rich liquid pump through the first outlet of the absorption tower and the inlet of the rich liquid pump, and then enters the distribution heat exchangers through the outlet of the rich liquid pump and the first inlets of the distribution heat exchangers to exchange heat under the action of the rich liquid pump so as to absorb heat and raise temperature.
The rich liquid subjected to heat exchange enters the desorption tower through the first outlet of each distribution heat exchanger, the first inlet of the desorption tower and the second inlet of the desorption tower, is heated and desorbed, and is decomposed into carbon dioxide and lean liquid.
The decomposed carbon dioxide moves upward and is discharged through the second outlet of the desorber.
The lean solution enters the reboiler through the first outlet of the desorption tower and the reboiler inlet to be heated to the boiling point, part of lean solution is changed into steam, and the steam enters the desorption tower again through the first outlet of the reboiler and the third inlet of the desorption tower to provide heat for desorption of the desorption tower.
The lean liquid which does not become steam enters the flash tank through the second outlet of the reboiler and the inlet of the flash tank, most of lean liquid in the flash tank is instantaneously vaporized to become secondary steam due to the pressure reduction in the flash tank, the secondary steam enters the Roots blower through the first outlet of the flash tank and the inlet of the Roots blower, the secondary steam is pressurized and heated in the Roots blower, and enters the desorption tower through the outlet of the Roots blower and the fourth inlet of the desorption tower under the action of the Roots blower to provide heat for desorption of the desorption tower, wherein the desorption tower, the reboiler, the flash tank and the Roots blower form a lean liquid waste heat recovery circulation loop, and a small part of the rest lean liquid in the lean liquid entering the flash tank enters the distribution heat exchangers through the second outlet of the flash tank and the second inlets of the distribution heat exchangers and returns to the absorption tower through the second outlets of the distribution heat exchangers and the second inlets of the absorption tower after the heat exchange.
The beneficial effects of the invention are as follows:
in the carbon dioxide trapping system based on waste heat utilization, the lean solution flowing out of the first outlet of the desorption tower has higher heat, and the desorption tower, the reboiler, the flash tank and the Roots blower in the carbon dioxide trapping system based on waste heat utilization form a lean solution waste heat recovery circulation loop, so that the lean solution is converted into high-temperature steam under the action of the reboiler, the flash tank and the Roots blower to be fed into the desorption tower again to provide heat for desorption of the rich solution, thereby realizing high-efficiency utilization of the lean solution waste heat and reducing energy waste.
Drawings
FIG. 1 is a schematic process flow diagram of a waste heat utilization based carbon dioxide capture system in accordance with the present invention.
Wherein reference numerals are as follows:
11 water scrubber
11A1 water scrubber first inlet
11B1 water scrubber first outlet
11A2 water scrubber second inlet
11B2 water scrubber second outlet
12 gas-liquid separator
12A gas-liquid separator inlet
12B1 gas-liquid separator first outlet
Second outlet of 12B2 gas-liquid separator
13 induced draft fan
13A induced draft fan inlet
13B induced draft fan outlet
14 absorption tower
First inlet of 14A1 absorption tower
First outlet of 14B1 absorption tower
Second inlet of 14A2 absorption tower
Second outlet of 14B2 absorption tower
Third inlet of 14A3 absorption tower
Third outlet of 14B3 absorption tower
15 rich liquid pump
15A rich liquor pump inlet
15B rich liquor pump outlet
16-distributed heat exchanger
First inlet of 16A1 distributed heat exchanger
First outlet of 16B1 distributed heat exchanger
Second inlet of 16A2 distributed heat exchanger
Second outlet of 16B2 distributed heat exchanger
17 desorber
17A1 Desorption column first inlet
17B1 desorber first outlet
17A2 desorber second inlet
17B2 desorber second outlet
Third inlet of 17A3 desorber
Third outlet of 17B3 desorber
17A4 desorber fourth inlet
17A5 desorber fifth inlet
18 reboiler
18A reboiler inlet
First outlet of 18B1 reboiler
Second outlet of 18B2 reboiler
19 flash tank
19A flash tank inlet
19B1 flash tank first outlet
19B2 flash tank second outlet
20 Roots blower
20A Roots blower inlet
20B Roots blower outlet
21 evaporator
First inlet of 21A1 evaporator
First outlet of 21B1 evaporator
Second inlet of 21A2 evaporator
21B2 evaporator second outlet 22 reflux drum
22A reflux drum inlet
22B1 reflux drum first outlet
22B2 reflux drum second outlet
23 compressor
23A compressor inlet
23B compressor outlet
24 condenser
24A1 condenser first inlet
24B1 condenser first outlet
Second inlet of 24A2 condenser
Second outlet of 24B2 condenser
25 throttle valve
26 phase separator
26A phase separator inlet
26B1 phase separator first outlet
26B2 phase separator second outlet
27 dilute phase pump
27A dilute phase pump inlet
27B dilute phase pump outlet
28 mixer
First inlet of 28A1 mixer
28B mixer outlet
Second inlet of 28A2 mixer
29 cooler
29A cooler inlet
29B cooler outlet
30 lean solution pump
30A lean solution pump inlet
30B lean liquid Pump out
31 washing pump
31A washing pump inlet
31B washing pump outlet
32 liquid storage tank
32A liquid storage tank inlet
32B liquid storage tank outlet
Detailed Description
The carbon dioxide capturing system based on the waste heat utilization according to the present invention will be described in detail with reference to the accompanying drawings.
Referring to fig. 1, a carbon dioxide capture system based on waste heat utilization according to the present invention includes: a water scrubber 11, a gas-liquid separator 12, an induced draft fan 13, an absorber 14, a rich liquid pump 15, a plurality of distributed heat exchangers 16, a desorber 17, a reboiler 18, a flash tank 19 and a Roots blower 20.
The water washing tower 11 has: a first inlet 11A1 of the water scrubber, which is positioned at the upper part of the water scrubber 11 and into which external water scrubber water flows; a first outlet 11B1 of the water scrubber, which is located at the top of the water scrubber 11; a second inlet 11A2 of the water scrubber, which is positioned at the lower part of the water scrubber 11 and is used for entering the external raw material gas with carbon dioxide; the second outlet 11B2 of the water scrubber is located at the bottom of the water scrubber 11.
The gas-liquid separator 12 has: an inlet 12A of the gas-liquid separator is communicated with a first outlet 11B1 of the water scrubber; a gas-liquid separator first outlet 12B1 located at the top of the gas-liquid separator 12; the gas-liquid separator second outlet 12B2 is located at the bottom of the gas-liquid separator 12.
The induced draft fan 13 has: an induced draft fan inlet 13A is communicated with a first outlet 12B1 of the gas-liquid separator; and an induced draft fan outlet 13B.
The absorption tower 14 has: the first inlet 14A1 of the absorption tower is positioned at the bottom of the absorption tower 14 and is communicated with the outlet 13B of the induced draft fan; an absorber first outlet 14B1 located at the bottom of the absorber 14; an absorber second inlet 14A2 located at an upper portion of the absorber 14; an absorber second outlet 14B2 located at the top of the absorber 14; an absorber third inlet 14A3 located at the top of the absorber 14; the third outlet 14B3 of the absorption column is located at the upper portion of the absorption column 14.
The rich liquid pump 15 has: a rich liquid pump inlet 15A communicated with the first outlet 14B1 of the absorption tower; and a rich liquid pump outlet 15B.
Carbon dioxide capture system based on waste heat utilization still includes: a plurality of distributed heat exchangers 16, each distributed heat exchanger 16 having: a first inlet 16A1 of the distribution heat exchanger is communicated with a rich liquid pump outlet 15B; a distributed heat exchanger first outlet 16B1; a distributed heat exchanger second inlet 16A2; the distributed heat exchanger second outlet 16B2 communicates with the absorber second inlet 14A2.
The desorption column 17 has: a first desorber inlet 17A1 located at the upper part of the desorber 17 and communicating with at least one of the plurality of first distribution heat exchanger outlets 16B1; a first outlet 17B1 of the desorption column, which is located at the bottom of the desorption column 17; a second inlet 17A2 of the desorption tower is positioned in the middle of the desorption tower 17 and is communicated with at least one of the first outlets 16B1 of the plurality of distribution heat exchangers; a second outlet 17B2 of the desorber, which is located at the top of the desorber 17; a third inlet 17A3 of the desorption column is positioned at the lower part of the desorption column 17; a fourth inlet 17A4 of the desorption column is located at the lower part of the desorption column 17.
The reboiler 18 has: a reboiler inlet 18A communicating with the first outlet 17B1 of the desorber; a reboiler first outlet 18B1 communicating with the third inlet 17A3 of the desorber; reboiler second outlet 18B2.
The flash tank 19 has: flash tank inlet 19A, communicating with reboiler second outlet 18B2; a flash tank first outlet 19B1 located at the top of the flash tank 19; the flash tank second outlet 19B2 is located at the bottom of the flash tank 19 and is communicated with the second inlets 16A2 of the distribution heat exchangers.
The Roots blower 20 has: roots blower inlet 20A, communicating flash tank first outlet 19B1; the Roots blower outlet 20B is communicated with the fourth inlet 17A4 of the desorption tower.
Wherein the external carbon dioxide-containing raw gas enters the lower part of the water scrubber 11 through the second inlet 11A2 of the water scrubber, and is in countercurrent contact with the water scrubber water sprayed from the upper part of the water scrubber 11 and supplied through the first inlet 11A1 of the water scrubber, and the water scrubber absorbs acidic impurity gases (such as SO X 、NO X ) And smoke dust, and the rest of raw gas with carbon dioxide moves upwards and enters the gas-liquid separator 12 through the first outlet 11B1 of the water scrubber and the inlet 12A of the gas-liquid separator to carry out gas-liquid separation;
the liquid separated in the gas-liquid separator 12 is discharged through a gas-liquid separator second outlet 12B2, and the separated carbon dioxide raw gas enters the induced draft fan 13 through a gas-liquid separator first outlet 12B1 and an induced draft fan inlet 13A, and enters the absorption tower 14 through an induced draft fan outlet 13B and an absorption tower first inlet 14A1 under the action of the induced draft fan 13;
the carbon dioxide raw gas introduced into the absorber 14 is in countercurrent contact with the absorbent sprayed from the upper part of the absorber 14 fed through the absorber second inlet 14A2, and the absorbent absorbs carbon dioxide in the carbon dioxide raw gas to become rich liquid, and the remaining raw gas moves upward;
the rich liquid enters the rich liquid pump 15 through the first outlet 14B1 of the absorption tower and the rich liquid pump inlet 15A, and then enters each distributed heat exchanger 16 through the rich liquid pump outlet 15B and the first inlets 16A1 of each distributed heat exchanger for heat exchange under the action of the rich liquid pump 15 so as to absorb heat and raise temperature;
the rich liquid subjected to heat exchange enters the desorption tower 17 through a first outlet 16B1 of each distribution heat exchanger, a first inlet 17A1 of the desorption tower and a second inlet 17A2 of the desorption tower, is heated and desorbed, and is decomposed into carbon dioxide and lean liquid;
the decomposed carbon dioxide moves upward and is discharged through the desorber second outlet 17B2;
the lean solution enters the reboiler 18 through the first outlet 17B1 of the desorption tower and the reboiler inlet 18A to be heated to the boiling point, part of the lean solution is changed into steam, and the steam enters the desorption tower 17 again through the first outlet 18B1 of the reboiler and the third inlet 17A3 of the desorption tower to provide heat for desorption of the desorption tower 17 (firstly, waste heat recovery is carried out once, and energy waste is reduced);
the lean liquid which is not changed into steam enters the flash tank 19 through the reboiler second outlet 18B2 and the flash tank inlet 19A, the lean liquid entering the flash tank 19 is vaporized into secondary steam instantaneously due to the pressure reduction in the flash tank 19, the secondary steam enters the Roots blower 20 through the flash tank first outlet 19B1 and the Roots blower inlet 20A, the secondary steam is pressurized and heated in the Roots blower 20, the Roots blower 20 is used for supplying heat for desorption by the desorption tower 17 through the Roots blower outlet 20B and the desorption tower fourth inlet 17A4, the desorption tower 17, the reboiler 18, the flash tank 19 and the Roots blower 20 form a lean liquid waste heat recovery circulation loop, and the rest small part of lean liquid entering the flash tank 19 enters the distribution heat exchangers 16 through the flash tank second outlet 19B2 and the distribution heat exchangers second inlets 16A2 and exchanges heat with the rich liquid in the distribution heat exchangers 16, and then enters the desorption tower 17 through the distribution heat exchanger second outlets 16B2 and the absorption tower second inlet 14A2 to realize heat exchange between the lean liquid and the rich liquid in the absorption tower 16.
In the carbon dioxide capturing system based on waste heat utilization, the lean solution flowing out of the first outlet 17B1 of the desorption tower has higher heat, the desorption tower 17, the reboiler 18, the flash tank 19 and the Roots blower 20 in the carbon dioxide capturing system based on waste heat utilization form a lean solution waste heat recovery circulation loop, and the lean solution is converted into high-temperature steam under the action of the reboiler 18, the flash tank 19 and the Roots blower 20 and then enters the desorption tower 17 again to provide heat for desorption of the rich solution, so that the high-efficiency utilization of the lean solution waste heat is realized, and the waste of energy sources is reduced.
The desorber 17 further has: a fifth inlet 17A5 of the desorption column, which is located at the upper part of the desorption column 17; the third outlet 17B3 of the desorber is located in the middle of the desorber 17.
The carbon dioxide trapping system based on waste heat utilization also comprises: an evaporator 21, a reflux drum 22, a compressor 23, a condenser 24 and a throttle valve 25.
The evaporator 21 has: the first inlet 21A1 of the evaporator is communicated with the second outlet 17B2 of the desorption tower; an evaporator first outlet 21B1; an evaporator second inlet 21A2; and an evaporator second outlet 21B2.
The reflux drum 22 has: a reflux drum inlet 22A communicating with the evaporator first outlet 21B1; a reflux drum first outlet 22B1; and a reflux drum second outlet 22B2.
The compressor 23 has: a compressor inlet 23A communicating with the evaporator second outlet 21B2; compressor outlet 23B.
The condenser 24 has: a condenser first inlet 24A1 communicating with the compressor outlet 23B; a condenser first outlet 24B1; a condenser second inlet 24A2 is communicated with a third outlet 17B3 of the desorption tower; and a condenser second outlet 24B2 communicating with the fifth inlet 17A5 of the desorber.
A throttle valve 25 is provided between the condenser 24 and the evaporator 21, with one end being in controlled communication with the condenser first outlet 24B1 and the other end being in controlled communication with the evaporator second inlet 21A2.
Wherein, the carbon dioxide discharged from the second outlet 17B2 of the desorption tower enters the evaporator 21 through the first inlet 21A1 of the evaporator and exchanges heat with the working medium liquid in the evaporator 21;
the carbon dioxide releases heat and is cooled, and enters the reflux drum 22 through the first outlet 21B1 of the evaporator and the inlet 22A of the reflux drum, the carbon dioxide is separated from the carried water vapor in the reflux drum 22, the carbon dioxide gas is discharged from the first outlet 22B1 of the reflux drum, and the condensed water is discharged from the second outlet 22B2 of the reflux drum;
the working medium liquid absorbs heat and heats up to become working medium steam;
the working medium steam enters the compressor 23 through the second outlet 21B2 of the evaporator and the inlet 23A of the compressor, the compressor 23 compresses the working medium steam, and the compressed working medium steam is heated and boosted to become superheated steam;
superheated steam enters the condenser 24 through the compressor outlet 23B and the condenser first inlet 24A1, the rich liquid flowing out of the third outlet 17B3 of the desorption tower enters the condenser 24 through the condenser second inlet 24A2 and exchanges heat with the superheated steam in the condenser 24, the rich liquid absorbs heat and heats up to be desorbed, the rich liquid is desorbed into carbon dioxide and lean liquid, the carbon dioxide and lean liquid enter the desorption tower 17 again through the condenser second outlet 24B2 and the fifth inlet 17A5 of the desorption tower, and the superheated steam releases heat and reduces temperature to be changed into high-pressure working medium liquid;
the high-pressure working fluid flows into the throttle valve 25 and is depressurized to become low-pressure working fluid, and the low-pressure working fluid enters the evaporator 21 again through the evaporator second inlet 21A2 under the action of the throttle valve 25, thereby completing a cycle process, wherein the desorption tower 17, the evaporator 21, the compressor 23, the condenser 24 and the throttle valve 25 form a carbon dioxide vapor waste heat recovery cycle.
In the carbon dioxide capturing system based on waste heat utilization according to the present invention, the carbon dioxide vapor discharged from the second outlet 17B2 of the desorption tower has higher heat, while the desorption tower 17, the evaporator 21, the compressor 23, the condenser 24 and the throttle valve 25 in the carbon dioxide capturing system based on waste heat utilization of the present invention form a carbon dioxide vapor waste heat recovery circulation loop, the carbon dioxide vapor transfers heat to the working medium in the circulation loop, the working medium becomes superheated vapor under the action of the evaporator and the compressor, the superheated vapor exchanges heat with the rich liquid in the condenser 24, the rich liquid absorbs heat and heats up and is desorbed into lean liquid and carbon dioxide, the lean liquid and the carbon dioxide after the desorption of the rich liquid flow back into the desorption tower 17 again, thereby realizing the recovery and reutilization of the heat of the carbon dioxide vapor discharged from the top of the desorption tower 17, and reducing the waste of energy.
In the carbon dioxide capturing system based on waste heat utilization according to the present invention, the carbon dioxide capturing system based on waste heat utilization has a plurality of distribution heat exchangers 16, and a plurality of connection manners are possible between the plurality of distribution heat exchangers 16, specifically, in an embodiment, referring to fig. 1, the carbon dioxide capturing system based on waste heat utilization includes two distribution heat exchangers 16, a distribution heat exchanger first outlet 16B1 of one distribution heat exchanger 16 is communicated with a desorption column first inlet 17A1 and a desorption column second inlet 17A2, and a distribution heat exchanger second inlet 16A2 is communicated with a flash tank second outlet 19B2;
the distribution heat exchanger first outlet 16B1 of the other distribution heat exchanger 16 communicates with the desorber first inlet 17A1 and the desorber second inlet 17A2 and the distribution heat exchanger second inlet 16A2 communicates with the distribution heat exchanger second outlet 16B2 of the one distribution heat exchanger 16. The lean solution and the rich solution are subjected to heat exchange in each distribution heat exchanger 16, so that the temperature difference between the lean solution and the rich solution is effectively reduced, the heat exchange efficiency is improved, the heat of the lean solution is fully recovered, and the waste of the heat of the lean solution is further reduced; in addition, with the distributed heat exchangers 16, the distributed heat exchanger first outlet 16B1 of each distributed heat exchanger 16 communicates with the desorber first inlet 17A1 and the desorber second inlet 17A2, and the rich liquid is split to the upper portion and the middle portion of the desorber 17 via the distributed heat exchanger 16, so that the loss of heat and water evaporation amount can be effectively reduced. Specifically, in the prior art, the rich liquid completely enters the upper part of the desorption tower 17 through a single heat exchanger outlet, when the rich liquid enters the upper part of the desorption tower 17, part of water vapor is flashed out due to sudden pressure reduction, and the flashed water vapor is directly discharged from a second outlet 17B2 of the desorption tower positioned at the top of the desorption tower 17, so that a large amount of water is lost; if the rich liquid completely enters the middle part of the desorption tower 17 through a single heat exchanger outlet, incomplete desorption (namely, the height of stripping decomposition is reduced) is caused, so the invention adopts the distributed heat exchanger 16 to be shunted to the upper part and the middle part of the desorption tower 17, and the loss of heat and water evaporation is effectively reduced.
The carbon dioxide capture system based on waste heat utilization further comprises: a phase separator 26, a dilute phase pump 27, a mixer 28, a cooler 29, and a lean liquid pump 30.
The phase separator 26 has: a phase separator inlet 26A communicating with the absorber first outlet 14B1; a phase separator first outlet 26B1; and a phase separator second outlet 26B2.
The dilute phase pump 27 has: a dilute phase pump inlet 27A communicated with the second outlet 26B2 of the phase separator; dilute phase pump outlet 27B.
The mixer 28 has: a mixer first inlet 28A1 communicating with the dilute phase pump outlet 27B; mixer outlet 28B; mixer second inlet 28A2.
The cooler 29 has: a cooler inlet 29A in communication with the mixer outlet 28B; the cooler outlet 29B communicates with the absorber second inlet 14A2.
The lean liquid pump 30 has: a lean solution pump inlet 30A communicated with the second outlets 16B2 of the distribution heat exchangers; and a lean liquid pump outlet 30B communicating with the mixer second inlet 28A2.
The phase separator 26 divides the rich liquid into an upper layer and a lower layer, the upper layer is a dilute phase liquid with less carbon dioxide content, the lower layer is a concentrated phase liquid with more carbon dioxide content, the dilute phase liquid of the upper layer is pumped into the mixer 28 through the dilute phase pump outlet 27B and the mixer first inlet 28A1 under the action of the dilute phase pump 27 through the dilute phase second outlet 26B2 and the dilute phase pump inlet 27A and then the dilute phase pump 27 is pumped into the rich liquid pump 15 through the rich liquid pump inlet 15A by the dilute phase liquid of the upper layer;
the lean liquid after heat exchange with the rich liquid in each distribution heat exchanger 16 enters the lean liquid pump 30 through the second outlet 16B2 of each distribution heat exchanger and the lean liquid pump inlet 30A, and the lean liquid enters the mixer 28 through the lean liquid pump outlet 30B and the mixer second inlet 28A2 under the action of the lean liquid pump 30 and is mixed with the lean phase liquid with low carbon dioxide content in the mixer 28;
the mixed liquid enters the cooler 29 through the mixer outlet 28B and the cooler inlet 29A, and then enters the absorption tower 14 again through the cooler outlet 29B and the absorption tower second inlet 14A2 to be recycled as the absorbent, wherein the absorption tower 14, the phase separator 26, the dilute phase pump 27, the mixer 28 and the cooler 29 form an absorbent recycling loop; and the absorption column 14, the phase separator 26, the rich liquid pump 15, the respective distribution heat exchangers 16, the desorption column 17, the reboiler 18, the flash tank 19, the lean liquid pump 30, the mixer 28, and the cooler 29 form another absorbent recovery circulation circuit. The design of the two absorbent recovery circulation loops effectively utilizes the residual liquid in the carbon dioxide trapping system based on waste heat utilization, and reduces the waste of energy sources.
The absorption tower 14 further has: an absorber third inlet 14A3 located at the top of the absorber 14; an absorber third outlet 14B3 located at an upper portion of the absorber 14;
the washing pump 31 has: a wash pump inlet 31A communicating with the absorber third outlet 14B3; a washing pump outlet 31B communicating with the third inlet 14A3 of the absorption column;
wherein the unabsorbed exhaust gas in the absorption tower 14 moves upward to be in countercurrent contact with the water wash liquid entering the top of the absorption tower 14 through the wash pump outlet 31B and the absorption tower third inlet 14A3, the absorbent vapor (for example, amine vapor generated when the absorbent is an organic amine solution) generated by the reaction of the absorbent contained in the exhaust gas and carbon dioxide is absorbed, and the rest of the exhaust gas is discharged through the absorption tower second outlet 14B 2.
The waste heat utilization based carbon dioxide capture system also includes a liquid storage tank 32.
The liquid storage tank 32 has: a tank inlet 32A for supplying fresh absorbent from the outside; a tank outlet 32B communicating with the absorber second inlet 14A2;
wherein external fresh absorbent enters the liquid storage tank 32 via the liquid storage tank inlet 32A and enters the absorber column 14 via the liquid storage tank outlet 32B, the absorber column second inlet 14A2 to provide sufficient absorbent to the absorber column 14.
Claims (5)
1. A waste heat utilization based carbon dioxide capture system comprising:
a water washing tower (11) is provided with:
a first inlet (11A 1) of the water scrubber, which is positioned at the upper part of the water scrubber (11) and into which external water scrubber water flows;
a first outlet (11B 1) of the water scrubber is positioned at the top of the water scrubber (11);
a second inlet (11A 2) of the water scrubber, which is positioned at the lower part of the water scrubber (11) and is used for entering the external raw gas with carbon dioxide;
a second outlet (11B 2) of the water scrubber is positioned at the bottom of the water scrubber (11);
a gas-liquid separator (12) is provided with:
an inlet (12A) of the gas-liquid separator is communicated with a first outlet (11B 1) of the water scrubber;
a first outlet (12B 1) of the gas-liquid separator is positioned at the top of the gas-liquid separator (12);
a second outlet (12B 2) of the gas-liquid separator is positioned at the bottom of the gas-liquid separator (12);
an induced draft fan (13) comprising:
an induced draft fan inlet (13A) is communicated with a first outlet (12B 1) of the gas-liquid separator;
an induced draft fan outlet (13B);
an absorption tower (14) is provided with:
the first inlet (14A 1) of the absorption tower is positioned at the bottom of the absorption tower (14) and is communicated with the outlet (13B) of the induced draft fan;
a first outlet (14B 1) of the absorption tower, which is positioned at the bottom of the absorption tower (14);
an absorber second inlet (14A 2) located at the upper part of the absorber (14);
a second outlet (14B 2) of the absorption tower, which is positioned at the top of the absorption tower (14);
a third inlet (14A 3) of the absorption tower, which is positioned at the top of the absorption tower (14);
a third outlet (14B 3) of the absorption tower, which is positioned at the upper part of the absorption tower (14);
a rich liquid pump (15) is provided with:
a rich liquid pump inlet (15A) communicated with a first outlet (14B 1) of the absorption tower; and
a rich liquid pump outlet (15B);
the carbon dioxide trapping system based on waste heat utilization is characterized by further comprising:
a plurality of distributed heat exchangers (16), each distributed heat exchanger (16) having:
a first inlet (16A 1) of the distribution heat exchanger is communicated with a rich liquid pump outlet (15B);
-a distributed heat exchanger first outlet (16B 1);
-a distributed heat exchanger second inlet (16 A2);
a second outlet (16B 2) of the distribution heat exchanger is communicated with a second inlet (14A 2) of the absorption tower;
a desorption column (17) provided with:
a first inlet (17A 1) of the desorption tower, which is positioned at the upper part of the desorption tower (17) and is communicated with at least one of a plurality of first outlets (16B 1) of the distribution heat exchanger;
a first outlet (17B 1) of the desorption tower is positioned at the bottom of the desorption tower (17);
a second inlet (17A 2) of the desorption tower is positioned in the middle of the desorption tower (17) and is communicated with at least one of the first outlets (16B 1) of the plurality of distribution heat exchangers;
a second outlet (17B 2) of the desorption tower is positioned at the top of the desorption tower (17);
a third inlet (17A 3) of the desorption tower, which is positioned at the lower part of the desorption tower (17);
a fourth inlet (17A 4) of the desorption tower, which is positioned at the lower part of the desorption tower (17);
a reboiler (18) having:
a reboiler inlet (18A) communicated with a first outlet (17B 1) of the desorption tower;
a reboiler first outlet (18B 1) communicated with a third inlet (17A 3) of the desorption tower;
a reboiler second outlet (18B 2);
a flash tank (19) having:
a flash tank inlet (19A) communicated with a reboiler second outlet (18B 2);
a flash tank first outlet (19B 1) located at the top of the flash tank (19);
a flash tank second outlet (19B 2) positioned at the bottom of the flash tank (19) and communicated with a second inlet (16A 2) of each distribution heat exchanger;
roots blower (20) having:
a Roots blower inlet (20A) communicated with a flash tank first outlet (19B 1);
the Roots blower outlet (20B) is communicated with the fourth inlet (17A 4) of the desorption tower;
wherein, the external raw material gas with carbon dioxide enters the lower part of the water scrubber (11) through a second inlet (11A 2) of the water scrubber, and is in countercurrent contact with water scrubber water sprayed from the upper part of the water scrubber (11) and supplied through a first inlet (11A 1) of the water scrubber, the water scrubber absorbs acid impurity gas and smoke dust in the raw material gas, and the rest of raw material gas with carbon dioxide moves upwards and enters a gas-liquid separator (12) through a first outlet (11B 1) of the water scrubber and a gas-liquid separator inlet (12A) to carry out gas-liquid separation;
the liquid separated in the gas-liquid separator (12) is discharged through a second outlet (12B 2) of the gas-liquid separator, and the separated carbon dioxide raw gas enters an induced draft fan (13) through a first outlet (12B 1) of the gas-liquid separator and an induced draft fan inlet (13A) and enters an absorption tower (14) through an induced draft fan outlet (13B) and a first inlet (14A 1) of the absorption tower under the action of the induced draft fan (13);
the carbon dioxide raw gas entering the absorption tower (14) is in countercurrent contact with an absorbent sprayed from the upper part of the absorption tower (14) and fed through a second inlet (14A 2) of the absorption tower, the absorbent absorbs carbon dioxide in the carbon dioxide raw gas to become rich liquid, and the rest raw gas moves upwards;
the rich liquid enters a rich liquid pump (15) through a first outlet (14B 1) of the absorption tower and a rich liquid pump inlet (15A), and then enters each distributed heat exchanger (16) through a rich liquid pump outlet (15B) and a first inlet (16A 1) of each distributed heat exchanger under the action of the rich liquid pump (15) to exchange heat so as to absorb heat and raise temperature;
the rich liquid subjected to heat exchange enters a desorption tower (17) through a first outlet (16B 1) of each distribution heat exchanger, a first inlet (17A 1) of the desorption tower and a second inlet (17A 2) of the desorption tower, and is heated and desorbed, so that the rich liquid is decomposed into carbon dioxide and lean liquid;
the decomposed carbon dioxide moves upward and is discharged through a second outlet (17B 2) of the desorber;
the lean solution enters a reboiler (18) through a first outlet (17B 1) of the desorption tower and a reboiler inlet (18A) to be heated and heated to a boiling point, part of the lean solution is changed into steam, and the steam enters the desorption tower (17) again through the first outlet (18B 1) of the reboiler and a third inlet (17A 3) of the desorption tower to provide heat for desorption of the desorption tower (17);
the lean liquid which does not become steam enters the flash tank (19) through a reboiler second outlet (18B 2) and a flash tank inlet (19A), the lean liquid entering the flash tank (19) is instantaneously vaporized into secondary steam due to the pressure reduction in the flash tank (19), the secondary steam enters the Roots blower (20) through a flash tank first outlet (19B 1) and a Roots blower inlet (20A), the secondary steam is pressurized and heated in the Roots blower (20), enters the desorption tower (17) through the Roots blower outlet (20B) and a desorption tower fourth inlet (17A 4) under the action of the Roots blower (20) to provide heat for desorption of the desorption tower (17), wherein the desorption tower (17), the reboiler (18), the flash tank (19) and the Roots blower (20) form a lean liquid waste heat recovery circulation loop, and the rest of the lean liquid entering the flash tank (19) enters the distribution heat exchangers (16) through the flash tank second outlet (19B 2) and the distribution heat exchangers (16A 2) and the heat exchange is carried out between the distribution heat exchangers (16) and the rich liquid (16) and the second distribution heat exchanger (14) and the absorption tower (14) is realized after the heat exchange;
the desorption column (17) further comprises:
a fifth inlet (17A 5) of the desorption column, which is positioned at the upper part of the desorption column (17);
a third outlet (17B 3) of the desorption tower is positioned in the middle of the desorption tower (17);
the carbon dioxide trapping system based on waste heat utilization also comprises:
an evaporator (21) is provided with:
an evaporator first inlet (21A 1) communicated with a desorber second outlet (17B 2);
an evaporator first outlet (21B 1);
an evaporator second inlet (21 A2); and
an evaporator second outlet (21B 2);
a reflux drum (22) having:
a reflux drum inlet (22A) communicating with the evaporator first outlet (21B 1);
a reflux drum first outlet (22B 1); and
a reflux drum second outlet (22B 2);
a compressor (23) is provided with:
a compressor inlet (23A) communicating with the evaporator second outlet (21B 2);
a compressor outlet (23B);
a condenser (24) is provided with:
a condenser first inlet (24A 1) communicating with a compressor outlet (23B);
a condenser first outlet (24B 1);
a condenser second inlet (24A 2) communicated with a third outlet (17B 3) of the desorption tower; and
a condenser second outlet (24B 2) communicated with a fifth inlet (17A 5) of the desorption tower;
a throttle valve (25) arranged between the condenser (24) and the evaporator (21), one end of which is controlled to be communicated with the first outlet (24B 1) of the condenser, and the other end of which is controlled to be communicated with the second inlet (21A 2) of the evaporator;
wherein, carbon dioxide discharged from a second outlet (17B 2) of the desorption tower enters the evaporator (21) through a first inlet (21A 1) of the evaporator and exchanges heat with working medium liquid in the evaporator (21);
the carbon dioxide releases heat and is cooled, and enters a reflux tank (22) through a first outlet (21B 1) of the evaporator and an inlet (22A) of the reflux tank, the carbon dioxide is separated from carried water vapor in the reflux tank (22), carbon dioxide gas is discharged from the first outlet (22B 1) of the reflux tank, and condensed water is discharged from a second outlet (22B 2) of the reflux tank;
the working medium liquid absorbs heat and heats up to become working medium steam;
the working medium steam enters the compressor (23) through the second outlet (21B 2) of the evaporator and the inlet (23A) of the compressor, the compressor (23) compresses the working medium steam, and the compressed working medium steam is heated and boosted to become superheated steam;
superheated steam enters the condenser (24) through the compressor outlet (23B) and the condenser first inlet (24A 1), rich liquid flowing out of the third outlet (17B 3) of the desorption tower enters the condenser (24) through the condenser second inlet (24A 2) and exchanges heat with superheated steam in the condenser (24), the rich liquid absorbs heat and warms up to be desorbed, carbon dioxide and lean liquid are desorbed, the lean liquid enters the desorption tower (17) again through the condenser second outlet (24B 2) and the fifth inlet (17A 5) of the desorption tower, and the superheated steam releases heat and cools down to be high-pressure working medium liquid;
the high-pressure working medium liquid flows into the throttle valve (25) and is depressurized to become low-pressure working medium liquid, the low-pressure working medium liquid enters the evaporator (21) again through the second inlet (21A 2) of the evaporator under the action of the throttle valve (25), so that a primary circulation process is completed, and the desorption tower (17), the evaporator (21), the compressor (23), the condenser (24) and the throttle valve (25) form a carbon dioxide steam waste heat recovery circulation loop.
2. The waste heat utilization based carbon dioxide capture system of claim 1, wherein,
the carbon dioxide capture system based on waste heat utilization comprises two distributed heat exchangers (16),
a first outlet (16B 1) of the distribution heat exchanger (16) is communicated with a first inlet (17A 1) of the desorption tower and a second inlet (17A 2) of the desorption tower, and a second inlet (16A 2) of the distribution heat exchanger is communicated with a second outlet (19B 2) of the flash tank;
a first outlet (16B 1) of the distribution heat exchanger of the other distribution heat exchanger (16) is communicated with a first inlet (17A 1) of the desorption tower and a second inlet (17A 2) of the desorption tower, and a second inlet (16A 2) of the distribution heat exchanger is communicated with a second outlet (16B 2) of the distribution heat exchanger of the one distribution heat exchanger (16).
3. The waste heat utilization-based carbon dioxide capture system of claim 2, further comprising:
a phase separator (26) is provided with:
a phase separator inlet (26A) connected to the first outlet (14B 1) of the absorption column;
a phase separator first outlet (26B 1); and
a phase separator second outlet (26B 2);
a dilute phase pump (27) having:
a dilute phase pump inlet (27A) communicated with a second outlet (26B 2) of the phase separator;
a dilute phase pump outlet (27B);
a mixer (28) having:
a mixer first inlet (28A 1) communicating with the dilute phase pump outlet (27B);
a mixer outlet (28B);
a mixer second inlet (28 A2);
a cooler (29) having:
a cooler inlet (29A) communicating with the mixer outlet (28B);
a cooler outlet (29B) communicating with the absorber second inlet (14A 2);
a lean liquid pump (30) is provided with:
a lean solution pump inlet (30A) communicated with the second outlets (16B 2) of the distribution heat exchangers; and
a lean liquid pump outlet (30B) in communication with the mixer second inlet (28 A2);
the phase separator (26) divides the rich liquid into an upper layer and a lower layer, the upper layer is a dilute phase liquid with low carbon dioxide content, the lower layer is a concentrated phase liquid with high carbon dioxide content, the dilute phase liquid of the upper layer is pumped into the mixer (28) through the dilute phase pump outlet (27B) and the mixer first inlet (28A 1) under the action of the dilute phase pump (27) through the dilute phase pump second outlet (26B 2) and the dilute phase pump inlet (27A) and then the dilute phase pump (27) through the dilute phase pump inlet (15A), and the concentrated phase liquid with high carbon dioxide content of the lower layer is taken as the rich liquid entering the rich liquid pump (15) through the rich liquid pump inlet (15A);
the lean solution after heat exchange with the rich solution in each distribution heat exchanger (16) enters the lean solution pump (30) through a second outlet (16B 2) of each distribution heat exchanger and a lean solution pump inlet (30A), and under the action of the lean solution pump (30), the lean solution enters the mixer (28) through a lean solution pump outlet (30B) and a mixer second inlet (28A 2) and is mixed with the lean phase solution with low carbon dioxide content in the mixer (28);
the mixed liquid enters a cooler (29) through a mixer outlet (28B) and a cooler inlet (29A), and then enters the absorption tower (14) again through the cooler outlet (29B) and an absorption tower second inlet (14A 2) to be recycled as an absorbent, wherein the absorption tower (14), a phase separator (26), a dilute phase pump (27), the mixer (28) and the cooler (29) form an absorbent recycling loop; the absorption tower (14), the phase separator (26), the rich liquid pump (15), each distribution heat exchanger (16), the desorption tower (17), the reboiler (18), the flash tank (19), the lean liquid pump (30), the mixer (28) and the cooler (29) form another absorbent recovery circulation loop.
4. The waste heat utilization based carbon dioxide capture system of claim 1, wherein,
the absorption tower (14) further comprises:
a third inlet (14A 3) of the absorption tower, which is positioned at the top of the absorption tower (14);
a third outlet (14B 3) of the absorption tower, which is positioned at the upper part of the absorption tower (14);
a washing pump (31) is provided with:
a washing pump inlet (31A) communicated with a third outlet (14B 3) of the absorption tower;
a washing pump outlet (31B) communicated with a third inlet (14A 3) of the absorption tower;
wherein the unabsorbed exhaust gas in the absorption tower (14) moves upward to be in countercurrent contact with the water washing liquid entering the top of the absorption tower (14) through the washing pump outlet (31B) and the absorption tower third inlet (14A 3), the absorbent vapor generated by the reaction of the absorbent contained in the exhaust gas and the carbon dioxide is absorbed, and the rest of the exhaust gas is discharged through the absorption tower second outlet (14B 2).
5. The waste heat utilization based carbon dioxide capture system of claim 1, wherein,
carbon dioxide capture system based on waste heat utilization still includes:
a liquid storage tank (32) comprising:
a reservoir inlet (32A) for providing fresh absorbent from the outside;
a liquid storage tank outlet (32B) communicated with a second inlet (14A 2) of the absorption tower;
wherein the external fresh absorbent enters the liquid storage tank (32) via a liquid storage tank inlet (32A) and enters the absorption tower (14) via a liquid storage tank outlet (32B) and an absorption tower second inlet (14A 2) to provide sufficient absorbent for the absorption tower (14).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711181818.8A CN108236831B (en) | 2017-11-23 | 2017-11-23 | Carbon dioxide trapping system based on waste heat utilization |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711181818.8A CN108236831B (en) | 2017-11-23 | 2017-11-23 | Carbon dioxide trapping system based on waste heat utilization |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108236831A CN108236831A (en) | 2018-07-03 |
| CN108236831B true CN108236831B (en) | 2023-11-24 |
Family
ID=62700895
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711181818.8A Active CN108236831B (en) | 2017-11-23 | 2017-11-23 | Carbon dioxide trapping system based on waste heat utilization |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108236831B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109092020A (en) * | 2018-10-24 | 2018-12-28 | 中石化石油工程技术服务有限公司 | Carbon dioxide capture system suitable for phase transformation absorbent |
| 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 |
| CN111054187A (en) * | 2019-12-18 | 2020-04-24 | 国家能源投资集团有限责任公司 | Recovery system and gas recovery method |
| CN116492816B (en) * | 2023-03-23 | 2024-03-12 | 中国能源建设集团广东省电力设计研究院有限公司 | High CO 2 Loaded absorbent carbon capture desorption system and method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104043316A (en) * | 2014-06-03 | 2014-09-17 | 中国华能集团清洁能源技术研究院有限公司 | Low temperature multiple-effect distillation technology coupled carbon dioxide capturing or separating system |
| CN104826472A (en) * | 2015-04-23 | 2015-08-12 | 中石化石油工程设计有限公司 | Flue gas carbon dioxide capture recovery system |
| CN105268283A (en) * | 2015-09-28 | 2016-01-27 | 北京化工大学 | Combined absorption carbon dioxide trapping and compressing treatment technology |
| CN207562634U (en) * | 2017-11-23 | 2018-07-03 | 中石化石油工程技术服务有限公司 | Carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN |
-
2017
- 2017-11-23 CN CN201711181818.8A patent/CN108236831B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104043316A (en) * | 2014-06-03 | 2014-09-17 | 中国华能集团清洁能源技术研究院有限公司 | Low temperature multiple-effect distillation technology coupled carbon dioxide capturing or separating system |
| CN104826472A (en) * | 2015-04-23 | 2015-08-12 | 中石化石油工程设计有限公司 | Flue gas carbon dioxide capture recovery system |
| CN105268283A (en) * | 2015-09-28 | 2016-01-27 | 北京化工大学 | Combined absorption carbon dioxide trapping and compressing treatment technology |
| CN207562634U (en) * | 2017-11-23 | 2018-07-03 | 中石化石油工程技术服务有限公司 | Carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108236831A (en) | 2018-07-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108236831B (en) | Carbon dioxide trapping system based on waste heat utilization | |
| EP2089139B1 (en) | Improved absorbent regeneration | |
| CA2698906C (en) | Improved method for regeneration of absorbent | |
| CA2670395C (en) | Improved absorbent regeneration | |
| US8080089B1 (en) | Method and apparatus for efficient gas treating system | |
| CN108136321A (en) | For CO2The method and apparatus of trapping | |
| CN110152489B (en) | Carbon dioxide capture system and method based on steam turbine exhaust waste heat recovery | |
| CN110152457A (en) | The chemical absorption method carbon dioxide capture system utilized based on Waste Heat Recovery | |
| CN103318850A (en) | Low-temperature waste heat recovery system for pyrite and metallurgical off-gas acid making device | |
| CN207562634U (en) | Carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN | |
| CN114028911A (en) | Efficient carbon capture system based on waste heat recovery and utilization of interstage compressor | |
| KR101956927B1 (en) | Carbon dioxide capture process using steam condensate vapor recycle and system using the same | |
| CN107754568B (en) | Low-energy-consumption device for capturing and recovering carbon dioxide by flue gas and gas recovery process | |
| CN207533246U (en) | A kind of carbon trapping system regeneration gas heat reclaim unit | |
| CN108815993A (en) | The carbon dioxide capture system utilized based on Waste Heat Recovery | |
| CN113457381A (en) | Energy-saving process for capturing and recovering carbon dioxide from chimney exhaust gas | |
| CN111054187A (en) | Recovery system and gas recovery method | |
| CN102824818A (en) | Device for reducing energy consumption of flue gas CO2 capturing system and increasing CO2 recovery rate | |
| KR101375645B1 (en) | CO2 Absorption Device using heat of reboiler steam condensate | |
| CN115445423A (en) | Ammonia process decarburization device and operation method thereof | |
| CN203612956U (en) | Low-temperature waste heat recovery system used in pyrite and smelting exhaust gas acid preparing device | |
| CN103663398B (en) | Method and device for utilizing heat energy of diammonium phosphate neutralization tail gas | |
| CN203602362U (en) | Device for using heat energy of diammonium phosphate neutralizing tail gas | |
| CN106000009A (en) | Twin-tower MEDA landfill treating gas system | |
| CN114669177B (en) | Low-energy-consumption CO 2 Trapping and compression refining process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information | ||
| CB02 | Change of applicant information |
Address after: 100029 Chaoyang District, Beijing Hui Xin Street six, Twelfth level. Applicant after: SINOPEC OILFIELD SERVICE Corp. Applicant after: SINOPEC PETROLEUM ENGINEERING JIANGHAN Corp. Address before: 100029 Chaoyang District, Beijing Hui Xin Street six, Twelfth level. Applicant before: SINOPEC OILFIELD SERVICE Corp. Applicant before: SINOPEC ENERGY CONSERVATION AND ENVIRONMENTAL PROTECTION ENGINEERING TECHNOLOGY Co.,Ltd. |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant |