CN116747696A - Carbon trapping system with waste heat recovery device - Google Patents
Carbon trapping system with waste heat recovery device Download PDFInfo
- Publication number
- CN116747696A CN116747696A CN202310851249.2A CN202310851249A CN116747696A CN 116747696 A CN116747696 A CN 116747696A CN 202310851249 A CN202310851249 A CN 202310851249A CN 116747696 A CN116747696 A CN 116747696A
- Authority
- CN
- China
- Prior art keywords
- liquid
- heat
- lean
- recovery device
- rich
- 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.)
- Pending
Links
- 238000011084 recovery Methods 0.000 title claims abstract description 49
- 239000002918 waste heat Substances 0.000 title claims abstract description 49
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 26
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 26
- 239000007788 liquid Substances 0.000 claims abstract description 164
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 146
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 73
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 73
- 230000008929 regeneration Effects 0.000 claims abstract description 58
- 238000011069 regeneration method Methods 0.000 claims abstract description 58
- 239000007789 gas Substances 0.000 claims abstract description 42
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 19
- 239000003546 flue gas Substances 0.000 claims abstract description 19
- 150000001412 amines Chemical class 0.000 claims abstract description 16
- 239000002253 acid Substances 0.000 claims abstract description 12
- 239000002131 composite material Substances 0.000 claims abstract description 12
- 230000001172 regenerating effect Effects 0.000 claims abstract description 6
- 238000010521 absorption reaction Methods 0.000 claims description 46
- 239000003507 refrigerant Substances 0.000 claims description 38
- 238000005406 washing Methods 0.000 claims description 10
- 239000013505 freshwater Substances 0.000 claims description 7
- 230000001105 regulatory effect Effects 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 239000000498 cooling water Substances 0.000 claims description 4
- 238000005261 decarburization Methods 0.000 claims description 3
- -1 compound amine Chemical class 0.000 claims description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 abstract 1
- 238000004458 analytical method Methods 0.000 description 11
- 238000004064 recycling Methods 0.000 description 9
- 239000002904 solvent Substances 0.000 description 9
- 238000000034 method Methods 0.000 description 7
- 238000010586 diagram Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000001502 supplementing effect Effects 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000001926 trapping 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/343—Heat recovery
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/80—Organic bases or salts
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The invention discloses a carbon trapping system with a waste heat recovery device, which comprises a composite amine liquid absorbing device, a rich liquid regenerating device, a waste heat recovery device I and a waste heat recovery device II, wherein an absorbing tower of the composite amine liquid absorbing device utilizes lean liquid to trap carbon dioxide in flue gas to generate deacidified gas and rich liquid, the rich liquid regenerating device removes carbon dioxide of the rich liquid to generate sour gas and lean liquid, and the lean liquid returns to the composite amine liquid absorbing device for continuous utilization; the waste heat recovery device I comprises a heat pump unit A and a heat pump unit B, and is used for recovering heat in the lean solution and exchanging the heat to the rich solution regeneration device to heat the rich solution; the system also comprises a second waste heat recovery device, and the second waste heat recovery device further recovers the waste heat in the acid gas; according to the invention, the heat of the lean solution is efficiently recycled through the heat pump unit A and the heat pump unit B, the heat exchange efficiency of the heat pump unit A and the heat pump unit B is high, the heat is fully recycled, the heat is supplemented into the carbon capturing system, and the consumption of the system to external energy sources is reduced.
Description
Technical Field
The invention relates to the technical field of carbon dioxide trapping, in particular to a carbon trapping system with a waste heat recovery device.
Background
Along with the improvement of social development and living standard of people, the demand of people for energy is increased, meanwhile, the total carbon dioxide emission amount of China is also increased rapidly, as carbon dioxide in the atmosphere absorbs long wave radiation, the greenhouse effect is caused, the global warming is caused, data show that the average surface temperature of the global ocean and the land is increased by 0.85 ℃ within 1880 to 2012, the final result of global warming is glacier melting, the sea level is increased, the living environment of people is endangered, so that the problem of carbon dioxide emission reduction is more and more focused, and in various domestic fields, the application of carbon dioxide trapping work is required to be researched in the fields, such as power plants, heat supply source plants and the like, in consideration of how to combine the existing technology, the running cost of the enterprises is reduced, and the energy conservation and emission reduction work is well done.
The research work on carbon dioxide trapping in China has been carried out in the last 70 th century, the related technology starts to be popularized in the year 2000, the post-combustion trapping method is more applied now, and the chemical absorption method is more applied according to trapping effect and process complexity, but the heat generated in the existing carbon dioxide trapping technology is not recycled or has low utilization efficiency, so that resource waste is caused.
Patent document No. CN114632402a discloses a flue gas carbon dioxide capturing system and capturing method, including an absorption portion and a desorption portion, the absorption portion including an absorption tower for absorbing carbon dioxide; the resolving part comprises a first resolving tower and a second resolving tower, the first resolving tower and the second resolving tower are used for thermally resolving and regenerating carbon dioxide, and the pressure of the first resolving tower is larger than that of the second resolving tower; the bottom of the absorption tower can be communicated with a first rich liquid branch and a second rich liquid branch, the first rich liquid branch is communicated with the top of the first analysis tower, and the second rich liquid branch is communicated with the second analysis tower; the first analytic tower is communicated with a first barren liquor branch, and the first barren liquor branch can be communicated with the second analytic tower; the second analysis tower is communicated with the absorption tower through a second lean liquid branch and a third lean liquid branch.
The invention adopts two desorbers with different pressures, is suitable for increasing the pressure, improves the speed of regeneration reaction, and reduces the residence time required by rich liquor regeneration. But at the same time there is also: the system of the invention recycles the heat of lean liquid and rich liquid, but does not effectively recycle the heat carried by the analysis gas at the top of the analysis tower.
Patent document No. CN114225623B discloses a carbon capturing system, which discloses a carbon capturing system including an absorption tower for absorbing carbon dioxide with a semi-lean liquid and producing a rich liquid, a desorption tower, and a circulation device; the analysis tower is communicated with the absorption tower and is used for receiving the rich liquid generated by the absorption tower and analyzing the rich liquid to generate semi-lean liquid; the circulating device is respectively communicated with the absorption tower and the analysis tower, and is used for circulating and refluxing the semi-lean liquid generated by the analysis tower to the absorption tower.
According to the carbon trapping system provided by the embodiment of the invention, through the arrangement of the absorption tower, the analysis tower and the circulating device, the semi-lean solution is utilized to absorb the carbon dioxide in the absorption tower to form the rich solution, the rich solution generates the carbon dioxide and the semi-lean solution in the analysis tower, and the semi-lean solution returns to the absorption tower through the circulating device, so that the flow of the trapping system is shortened. But at the same time there is also: the method is mainly applied to carbon trapping before combustion of the synthesis gas, and is not applicable to carbon trapping in the flue gas with high carbon content; meanwhile, the waste heat of the lean solution, the rich solution and the resolved carbon dioxide is not effectively utilized, so that the energy waste is caused, and the energy input is increased.
Patent number CN114247272B discloses an energy-saving system based on carbon dioxide trapping technology, which comprises an absorption tower, wherein lean solution captures carbon dioxide in flue gas in the absorption tower and is converted into rich solution, the rich solution is heated by a heat exchanger and then enters a regeneration tower, the rich solution in the regeneration tower is heated and is converted into lean solution and high-temperature regenerated gas, the lean solution reenters the absorption tower by the heat exchanger, and the high-temperature regenerated gas is discharged from an air outlet of the regeneration tower; the waste heat recovery system is used for recovering waste heat. The invention only utilizes the heat in the regenerated amine liquid, and the absorption heat pump also needs to provide a heat source from the outside for supplementing during the operation, so that the heat pump has low efficiency and insufficient energy recovery.
In reality, the improvement of the carbon capture system is needed, the utilization of heat carried by lean liquid at the bottom of the regeneration tower and heat carried by carbon dioxide coming out from the top of the regeneration tower is increased, and the requirement of the system on external energy is reduced.
Disclosure of Invention
In view of the above problems, the present invention aims to provide a carbon capture system with a waste heat recovery device, which can capture carbon dioxide in flue gas, efficiently recycle heat generated in the capture process, reduce energy consumption of the capture system, and effectively recycle heat of lean solution in the capture system, thereby reducing operation cost of the system.
The aim of the invention can be achieved by the following technical scheme: a carbon trapping system with a waste heat recovery device comprises a composite amine liquid absorbing device, a rich liquid regenerating device and a waste heat recovery device I;
the composite amine liquid absorption device comprises an absorption tower, wherein the absorption tower utilizes lean liquid to trap carbon dioxide in the flue gas to generate decarburization tail gas and rich liquid;
the rich liquid regeneration device is used for removing carbon dioxide of the rich liquid, generating lean liquid and returning the lean liquid to the composite amine liquid absorption device;
the waste heat recovery device is used for recovering heat in the lean solution and exchanging the heat to the rich solution regeneration device for generating lean solution by carbon dioxide for removing the rich solution;
the waste heat recovery device I comprises a heat pump unit A and a heat pump unit B, and the heat pump unit A is connected with the heat pump unit B in series.
Further: the rich liquid regeneration device comprises a rich liquid pump, a lean and rich liquid heat exchanger, a regeneration tower, a lean liquid pump and a lean liquid cooler;
the rich liquid flows out from the bottom of the absorption tower, enters a lean-rich liquid heat exchanger through a rich liquid pump to exchange heat, then enters a regeneration tower, carbon dioxide in the rich liquid separated by the regeneration tower generates lean liquid, the lean liquid flows out from the bottom of the regeneration tower and enters the lean-rich liquid heat exchanger to exchange heat, and the lean liquid after heat exchange enters a waste heat recovery device I through the lean liquid pump to exchange heat, and then enters the top of the absorption tower after being cooled by a lean liquid cooler.
Further: the regeneration tower comprises a heater, the heater is arranged at the bottom of the regeneration tower, and the heater heats and analyzes the rich liquid to remove carbon dioxide and then generate lean liquid.
Further: the heat pump unit A comprises an evaporator A, a compressor A and a throttle valve A; the heat pump unit B comprises an evaporator B, a compressor B and a throttle valve B;
the lean solution enters an evaporator A through a lean solution pump, the lean solution exchanges heat with a refrigerant A of a heat pump unit A in the evaporator A, the refrigerant A after heat exchange enters an evaporator B after being compressed by a compressor A, the refrigerant A after heat exchange continuously exchanges heat with a refrigerant B of the heat pump unit B in the evaporator B, and the refrigerant A after heat exchange returns to the evaporator A after being regulated by a throttle valve A;
the refrigerant B after heat exchange enters a heater after being compressed by a compressor B, exchanges heat with rich liquid in the regeneration tower through the heater, and returns to the evaporator B after being regulated by a throttle valve B of the refrigerant B after heat exchange.
Further: the waste heat recovery device II comprises a heat exchanger, an acid gas cooler, a gas-liquid separator and a condensate pump;
carbon dioxide flows out from the top of the regeneration tower and enters a heat exchanger, heat exchange is carried out between the carbon dioxide and fresh water in the heat exchanger, and the fresh water is converted into hot water through heat exchange;
the carbon dioxide after heat exchange continuously enters an acid gas cooler, and exchanges heat with cooling water in the acid gas cooler;
the carbon dioxide after the secondary heat exchange enters a gas-liquid separator, condensate and non-condensable gas are obtained after the carbon dioxide is separated by the gas-liquid separator, the condensate is returned to the top of the regeneration tower through a condensate pump, and the non-condensable gas is discharged through the top of the gas-liquid separator and then is subjected to subsequent utilization treatment.
Further: the composite amine liquid absorption device also comprises an alkaline washing tower, and the flue gas enters the absorption tower after passing through the alkaline washing tower.
The invention has the beneficial effects that:
1. according to the invention, the heat pump unit in the first waste heat recovery device is used for efficiently recycling the heat carried by the barren solution, the heat pump unit is high in heat exchange efficiency, the waste heat is fully recycled, the recycled heat is supplemented into the carbon trapping system, the heating requirement of the rich solution regeneration device can be met, the external energy consumption of the trapping system is reduced, meanwhile, the temperature of the barren solution is reduced, and the cooling water consumption of the barren solution cooler can be reduced by more than 76%.
2. The performance coefficient of the unit reaches more than 2.6 through the evaporation heat pump unit A and the heat pump unit B which are connected in series, secondary compression heat exchange is carried out on the refrigerant after heat exchange, the temperature of the refrigerant B is further improved, the heat requirement of a heater can be met, the utilization efficiency of heat recovery in lean solution is improved, and the heat pump can reduce the regeneration energy consumption by more than 40%.
3. According to the invention, the waste heat recovery device II is arranged, and the heat of carbon dioxide discharged from the top of the regeneration tower is exchanged and recycled through the heat exchanger to obtain hot water for production and living, so that the heat of the carbon capture system is further recovered, the heat recovery rate is improved, the temperature of the carbon dioxide is also reduced, and the method is beneficial to the subsequent working procedures of the carbon dioxide.
4. The lean solution is effectively recycled through the rich solution regeneration device, the running cost of the system is reduced, meanwhile, the gas-liquid separator is arranged for treatment, the condensate returns to the top of the regeneration tower through the condensate pump for recycling, the solution contained in the condensate is further recycled, the consumption of the system solution is reduced, and the running cost of the system is reduced.
5. Part of heat of the lean solution can be exchanged to the rich solution through the lean-rich solution heat exchanger, the heat of the lean solution is recycled, the temperature of the rich solution is increased, the recycling of the lean solution after the temperature reduction is facilitated, and the heating analysis of the rich solution is facilitated.
Drawings
FIG. 1 is a schematic diagram of a carbon capture system with a waste heat recovery device according to the present invention;
FIG. 2 is a schematic structural view of a complex amine liquid absorbing device of the present invention;
FIG. 3 is a schematic diagram of a rich liquid regeneration apparatus according to the present invention;
FIG. 4 is a schematic diagram of a first waste heat recovery device according to the present invention;
fig. 5 is a schematic structural diagram of a second waste heat recovery device according to the present invention.
100. A complex amine liquid absorbing device; 110. an absorption tower; 120. an alkaline washing tower; 130. an alkaline washing pump;
200. a rich liquid regeneration device; 210. a rich liquid pump; 220. a lean rich liquid heat exchanger; 230. a regeneration tower; 231. a heater; 240. a lean liquid pump; 250. a lean solution cooler;
300. a waste heat recovery device I; 310. a heat pump unit A; 311. an evaporator A; 312. a compressor A; 313. a throttle valve A; 320. a heat pump unit B; 321. an evaporator B; 322. a compressor B; 323. a throttle valve B;
400. a second waste heat recovery device; 410. a heat exchanger; 420. an acid gas cooler; 430. a gas-liquid separator; 440. and a condensate pump.
Detailed Description
Embodiments of the present invention are described in detail below, examples of which are illustrated in the accompanying drawings, wherein like or similar symbols indicate like or similar elements or elements having like or similar functions throughout. The embodiments described below by referring to the drawings are exemplary only for explaining the present invention and are not to be construed as limiting the present invention.
As shown in fig. 1 to 5, the invention discloses a carbon capture system with a waste heat recovery device, which comprises a composite amine liquid absorbing device 100, a rich liquid regenerating device 200 and a waste heat recovery device 300;
the compound amine liquid absorbing device 100 comprises an absorbing tower 110, wherein the absorbing tower 110 utilizes lean liquid to trap carbon dioxide in the flue gas to generate decarburization tail gas and rich liquid;
the rich liquid regeneration device 200 is used for removing carbon dioxide of the rich liquid, generating lean liquid and returning the lean liquid to the composite amine liquid absorption device 100;
the first waste heat recovery device 300 is configured to recover heat in the lean solution, and exchange the heat to the rich solution regeneration device 200 to remove carbon dioxide in the rich solution to generate the lean solution;
the first waste heat recovery device 300 comprises a heat pump unit A and a heat pump unit B, and the heat pump unit A is connected with the heat pump unit B in series.
As shown in fig. 1 and 2, the flue gas firstly enters an alkaline washing tower 120, alkaline washing liquid in the alkaline washing tower 120 circularly flows through an alkaline washing pump 130 to remove sulfur-containing gas in the flue gas, the desulfurized flue gas enters the absorption tower 110 from the bottom of the absorption tower 110, the solvent adopted by the absorption tower 110 can be sterically hindered Amine (AMP) and a compound solution thereof, the solvent is lean liquid before absorbing carbon dioxide in the flue gas, the carbon dioxide in the flue gas is absorbed to form rich liquid, the lean liquid flows down from the upper part of the absorption tower 110 and is convected with the flue gas entering from the bottom of the absorption tower 110, the absorption efficiency of the lean liquid on the carbon dioxide in the flue gas is improved through convection, decarbonized tail gas from which the carbon dioxide is removed is about 40 ℃ and 100Pa, and the carbon dioxide in the flue gas is absorbed by the lean liquid to form the rich liquid from the top of the absorption tower 110 to a subsequent treatment link; the rich liquid passes through the bottom of the absorption tower 110 to the rich liquid regeneration apparatus 200.
As shown in fig. 3, the structure of the rich liquid regeneration device 200 is that the rich liquid regeneration device 200 is used for recycling the solvent, improving the recycling efficiency of the solvent, reducing the cost of flue gas purification, and the rich liquid regeneration device 200 comprises a rich liquid pump 210, a lean-rich liquid heat exchanger 220, a regeneration tower 230, a lean liquid pump 240 and a lean liquid cooler 250;
the rich liquid flows out from the bottom of the absorption tower 110, is pressurized by the rich liquid pump 210, enters the lean-rich liquid heat exchanger 220 for heat exchange at about 450kPa, is heated to about 90 ℃, and then enters the regeneration tower 230.
As shown in fig. 3, a heater 231 is disposed at the bottom of the regeneration tower 230, the heater 231 heats the rich liquid by using the refrigerant B circulated in the heat pump assembly, the rich liquid is heated to about 115 ℃ by the heater 231, the rich liquid is resolved and regenerated to remove carbon dioxide in the rich liquid to generate lean liquid, the lean liquid is about 115 ℃, the lean liquid flows out from the bottom of the regeneration tower 230, after entering the lean-rich liquid heat exchanger 220 to exchange heat with the rich liquid, the rich liquid is heated to about 90 ℃, the lean liquid is reduced to about 85 ℃ by the heat exchange temperature, the lean liquid is continuously sent to the waste heat recovery device 300 by the lean liquid pump 240 to exchange heat, the lean liquid after heat exchange by the waste heat recovery device 300 is reduced to about 52 ℃, and is continuously cooled to about 40 ℃ by the lean liquid cooler 250 to enter the top of the absorption tower 110.
As shown in fig. 4, the heat pump unit a310 includes an evaporator a311, a compressor a312, and a throttle valve a313, and the heat pump unit B320 includes an evaporator B321, a compressor B322, and a throttle valve B323; the lean solution enters an evaporator A311 through a lean solution pump 240, the lean solution exchanges heat with a refrigerant A of a heat pump unit A310 in the evaporator A311, the refrigerant A after heat exchange is compressed by a compressor A312 and enters an evaporator B321, the refrigerant A after heat exchange continuously exchanges heat with a refrigerant B of the heat pump unit B320 in the evaporator B321, and the refrigerant A after heat exchange returns to the evaporator A311 after being regulated by a throttle valve A313; the refrigerant B after heat exchange is compressed by the compressor B322, enters the heater 231, exchanges heat with the rich liquid in the regeneration tower by the heater 231, and returns to the evaporator B321 after being regulated by the throttle valve B323 of the refrigerant B after heat exchange.
Specifically, the low-temperature low-pressure gas liquid refrigerant A (1.3-1.4 MPa, 43-45 ℃) in the heat pump unit A310 exchanges heat with lean solution through the evaporator A311, the refrigerant A (1.3-1.4 MPa, 55-60 ℃) after heat exchange enters the compressor A312 for compression, the high-temperature high-pressure gas refrigerant A (3-3.2 MPa, 90-100 ℃) after compression enters the evaporator B321 for continuous heat exchange with the refrigerant B, the high-temperature high-pressure liquid refrigerant A (3-3.2 MPa, 90-100 ℃) after heat exchange is reduced in pressure through the throttle valve A313 and is changed into the low-temperature low-pressure gas liquid refrigerant A (1.3-1.4 MPa, 43-45 ℃) to return to the evaporator A311 for heat exchange with the lean solution.
The low-temperature low-pressure gas liquid refrigerant B (-0.05-0.03 MPa, 80-90 ℃) exchanges heat with the high-temperature high-pressure gas refrigerant A (3-3.2 MPa, 90-100 ℃) in the evaporator B321, then the refrigerant is sent to the compressor B322, the compressed high-temperature high-pressure gas refrigerant B (0.13-0.17 MPa, 125-130 ℃) is sent to the heater 231 to exchange heat with rich liquid, and the high-temperature high-pressure liquid refrigerant B (0.13-0.17 MPa, 125-130 ℃) after heat exchange is throttled and depressurized by the throttle valve B323 and then the low-temperature high-pressure gas liquid refrigerant B (-0.05-0.03 MPa, 80-90 ℃) returns to the evaporator B321 to exchange heat with the refrigerant A continuously.
The heat recovered by the first waste heat recovery device 300 is used for providing heat for the heater 231, so that the normal operation of the carbon capture system is ensured, and as shown in fig. 3, an additional heat medium interface is further arranged on the heater 231, and the heat medium interface is used for supplementing and heating the rich liquid by accessing steam and other heat mediums when the system is in initial operation or the refrigerant B cannot provide enough heat.
Further, as shown in fig. 5, the carbon capturing system further includes a second waste heat recovery device 400, where the second waste heat recovery device 400 includes a heat exchanger 410, an acid gas cooler 420, a gas-liquid separator 430, and a condensate pump 440; carbon dioxide flows out from the top of the regeneration tower 230 and enters the heat exchanger 410, heat exchange is carried out between the carbon dioxide and fresh water in the heat exchanger 410, and the fresh water is converted into hot water through heat exchange; the carbon dioxide subjected to heat exchange continuously enters an acid gas cooler 420, and heat exchange is continuously carried out between the carbon dioxide and cooling water in the acid gas cooler 420, so that the temperature of the carbon dioxide is further reduced; the carbon dioxide after the secondary heat exchange enters a gas-liquid separator 430, and is separated by the gas-liquid separator 430 to obtain condensate and noncondensable gas, the condensate is returned to the top of the regeneration tower 230 through a condensate pump 440, and the noncondensable gas is discharged from the top of the gas-liquid separator 430 and is subjected to subsequent utilization treatment.
Specifically, the temperature of the carbon dioxide analyzed by the regeneration tower 230 is about 95 ℃, the carbon dioxide enters the heat exchanger 410 from the top of the regeneration tower 230, hot water is obtained by heat exchange of fresh water and carbon dioxide in the heat exchanger 410, and the hot water can be used in production and life; the carbon dioxide after heat exchange is cooled to about 50 ℃, is continuously cooled to 30 ℃ by an acid gas cooler 420, enters a gas-liquid separator 430, is subjected to gas-liquid separation to obtain condensate and noncondensable gas, the condensate is returned to the top of the regeneration tower 230 through a condensate pump 440, and the noncondensable gas is discharged from the top of the gas-liquid separator 430 and is subjected to carbon dioxide liquefaction and utilization treatment.
Because the internal temperature of the regeneration tower 230 is high, part of the solvent volatilizes and is discharged from the top of the regeneration tower 230 together with the carbon dioxide, thereby increasing the consumption of the solvent. As shown in fig. 5, the heat-exchanged carbon dioxide may be subjected to a gas-liquid separation treatment by using a gas-liquid separator 430, wherein the condensate collects the solvent component in the carbon dioxide, and the condensate returns to the top of the regeneration tower 230 for reuse through a condensate pump 440, so that the solvent is recovered, and the consumption of the solvent is reduced.
The main component of the noncondensable gas is carbon dioxide, and the noncondensable gas contains moisture after being subjected to gas-liquid separation treatment, so that the noncondensable gas is not beneficial to recycling, needs to be dehydrated, is filtered and is subjected to liquefaction and recycling, and the carbon dioxide recycling flow is briefly described below:
the dehydration and filtration process mainly comprises the following steps: the carbon dioxide is dehydrated through a molecular sieve of the drying tower, filtered by a dust filter to remove dust, and then sent to a liquefying device for liquefying and recycling.
The liquefaction recovery flow mainly comprises: the dehydrated and filtered carbon dioxide is cooled firstly, then enters a separator, non-condensable gas in the carbon dioxide is primarily separated, then enters a purification tower for liquefaction, and further refined separation of the non-condensable gas is carried out, and the liquefied finished carbon dioxide enters a carbon dioxide subcooler for storage and utilization after being cooled.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include at least one such feature. In the description of the present invention, the meaning of "plurality" means at least two, for example, two, three, etc., unless specifically defined otherwise.
In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; may be mechanically connected, may be electrically connected or may be in communication with each other; either directly or indirectly, through intermediaries, or both, may be in communication with each other or in interaction with each other, unless expressly defined otherwise. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
Claims (6)
1. The utility model provides a take waste heat recovery device's carbon entrapment system which characterized in that: comprises a compound amine liquid absorbing device (100), a rich liquid regenerating device (200) and a waste heat recovery device I (300);
the composite amine liquid absorption device (100) comprises an absorption tower (110), wherein the absorption tower (110) utilizes lean liquid to trap carbon dioxide in flue gas to generate decarburization tail gas and rich liquid;
the rich liquid regeneration device (200) is used for removing carbon dioxide of the rich liquid, generating lean liquid and returning the lean liquid to the composite amine liquid absorption device (100);
the waste heat recovery device I (300) is used for recovering heat in the lean solution and exchanging the heat to the rich solution regeneration device (200) for generating lean solution by carbon dioxide for removing the rich solution;
the waste heat recovery device I (300) comprises a heat pump unit A and a heat pump unit B, and the heat pump unit A is connected with the heat pump unit B in series.
2. The carbon capture system with waste heat recovery device of claim 1, wherein: the rich liquid regeneration device (200) comprises a rich liquid pump (210), a lean and rich liquid heat exchanger (220), a regeneration tower (230), a lean liquid pump (240) and a lean liquid cooler (250);
the rich liquid flows out from the bottom of the absorption tower (110), enters a lean-rich liquid heat exchanger (220) through a rich liquid pump (210) for heat exchange, then enters a regeneration tower (230), carbon dioxide in the rich liquid is removed through the regeneration tower (230) to generate lean liquid, the lean liquid flows out from the bottom of the regeneration tower (230), firstly enters the lean-rich liquid heat exchanger (220) for heat exchange, and the lean liquid after heat exchange enters a waste heat recovery device I (300) for heat exchange through a lean liquid pump (240), and then enters the top of the absorption tower (110) after being cooled through a lean liquid cooler (250).
3. The carbon capture system with waste heat recovery device of claim 2, wherein: the regeneration tower (230) comprises a heater (231), the heater (231) is arranged at the bottom of the regeneration tower (230), and the heater (231) heats and analyzes the rich liquid to remove carbon dioxide and then generate lean liquid.
4. The carbon capture system with waste heat recovery device of claim 1, wherein: the heat pump unit A (310) comprises an evaporator A (311), a compressor A (312) and a throttle valve A (313); the heat pump unit B (320) comprises an evaporator B (321), a compressor B (322) and a throttle valve B (323);
the lean solution enters an evaporator A (311) through a lean solution pump (240), the lean solution exchanges heat with a refrigerant A of a heat pump unit A (310) in the evaporator A (311), the refrigerant A after heat exchange enters an evaporator B (321) after being compressed by a compressor A (312), the refrigerant A continues to exchange heat with a refrigerant B of the heat pump unit B (320) in the evaporator B (321), and the refrigerant A after heat exchange returns to the evaporator A (311) after being regulated by a throttle valve A (313);
the refrigerant B after heat exchange enters the heater (231) after being compressed by the compressor B (322), exchanges heat with rich liquid in the heater (231), and returns to the evaporator B (321) after being regulated by the throttle valve B (323) of the refrigerant B after heat exchange.
5. The carbon capture system with waste heat recovery device of claim 1, wherein: the waste heat recovery device II (400) is further included, and the waste heat recovery device II (400) comprises a heat exchanger (410), an acid gas cooler (420), a gas-liquid separator (430) and a condensate pump (440);
carbon dioxide flows out from the top of the regeneration tower (230) and enters a heat exchanger (410), heat exchange is carried out between the carbon dioxide and fresh water in the heat exchanger (410), and the fresh water is converted into hot water through heat exchange;
the carbon dioxide after heat exchange continuously enters an acid gas cooler (420), and exchanges heat with cooling water in the acid gas cooler (420);
the carbon dioxide subjected to secondary heat exchange enters a gas-liquid separator (430), condensate and non-condensable gas are obtained after the carbon dioxide is separated by the gas-liquid separator (430), the condensate returns to the top of the regeneration tower (230) through a condensate pump (440), and the non-condensable gas is discharged from the top of the gas-liquid separator (430) and is subjected to subsequent utilization treatment.
6. The carbon capture system with waste heat recovery device of claim 1, wherein: the composite amine liquid absorption device (100) further comprises an alkaline washing tower (120), and the flue gas enters the absorption tower (110) after passing through the alkaline washing tower (120).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310851249.2A CN116747696A (en) | 2023-07-12 | 2023-07-12 | Carbon trapping system with waste heat recovery device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310851249.2A CN116747696A (en) | 2023-07-12 | 2023-07-12 | Carbon trapping system with waste heat recovery device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116747696A true CN116747696A (en) | 2023-09-15 |
Family
ID=87955178
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310851249.2A Pending CN116747696A (en) | 2023-07-12 | 2023-07-12 | Carbon trapping system with waste heat recovery device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116747696A (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010088982A (en) * | 2008-10-06 | 2010-04-22 | Toshiba Corp | Carbon dioxide recovering system |
| CN104399356A (en) * | 2014-11-05 | 2015-03-11 | 中国华能集团清洁能源技术研究院有限公司 | Carbon dioxide capture system |
| CN212166984U (en) * | 2020-03-31 | 2020-12-18 | 国家能源投资集团有限责任公司 | CO2Trapping system |
| CN113144836A (en) * | 2021-05-20 | 2021-07-23 | 中国华电科工集团有限公司 | Carbon dioxide capture rich solution flash evaporation regeneration waste heat recovery system |
| CN115212709A (en) * | 2022-07-16 | 2022-10-21 | 碳索(杭州)能源环境科技有限公司 | Chemical method flue gas carbon dioxide capture system and capture method thereof |
-
2023
- 2023-07-12 CN CN202310851249.2A patent/CN116747696A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010088982A (en) * | 2008-10-06 | 2010-04-22 | Toshiba Corp | Carbon dioxide recovering system |
| CN104399356A (en) * | 2014-11-05 | 2015-03-11 | 中国华能集团清洁能源技术研究院有限公司 | Carbon dioxide capture system |
| CN212166984U (en) * | 2020-03-31 | 2020-12-18 | 国家能源投资集团有限责任公司 | CO2Trapping system |
| CN113144836A (en) * | 2021-05-20 | 2021-07-23 | 中国华电科工集团有限公司 | Carbon dioxide capture rich solution flash evaporation regeneration waste heat recovery system |
| CN115212709A (en) * | 2022-07-16 | 2022-10-21 | 碳索(杭州)能源环境科技有限公司 | Chemical method flue gas carbon dioxide capture system and capture method thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA2670395C (en) | Improved absorbent regeneration | |
| CN102895860B (en) | Method and system for reducing consumption in capturing process of CO2 through chemical absorption | |
| CN103961979B (en) | A kind of carbon dioxide capture system of multi-stage diffluence regeneration and technique | |
| CN110152489B (en) | Carbon dioxide capture system and method based on steam turbine exhaust waste heat recovery | |
| CN104399356B (en) | A kind of carbon dioxide capture system | |
| EA035832B1 (en) | Method and plant for cocapture | |
| CN212166984U (en) | CO2Trapping system | |
| CN108236831B (en) | Carbon dioxide trapping system based on waste heat utilization | |
| CN107859539A (en) | A kind of double Brayton cycle electricity generation systems of carbon dioxide of integrated carbon trapping | |
| CN101703880A (en) | Power plant flue gas desulphurization and decarbonization integrated purification system | |
| CN203803335U (en) | Multistage split regeneration carbon dioxide trapping system | |
| CN105749728B (en) | Method and apparatus for capturing carbon dioxide | |
| CN106076073A (en) | A kind of solar energy and the energy utility system of geothermal energy united power plant low-carbon emission | |
| CN109027994B (en) | Coal-fired power generation system utilizing boiler flue gas waste heat, decarbonizing waste heat and absorption heat pump | |
| CN106693614B (en) | Compact ammonia-method carbon capture system driven by ammonia-water second-class absorption heat pump | |
| CN111744328A (en) | Low-energy-consumption carbon dioxide capturing method and system for low-concentration carbon dioxide-containing tail gas | |
| CN116747696A (en) | Carbon trapping system with waste heat recovery device | |
| CN204582900U (en) | A kind of decarbonization system utilizing solar energy to assist reboiler to heat | |
| CN111054187A (en) | Recovery system and gas recovery method | |
| CN114272735B (en) | Flue gas waste heat utilization and carbon capture integrated system | |
| CN106669372B (en) | Coal-fired power plant carbon capture system driven by solar heating absorption heat pump | |
| CN114788992A (en) | Carbon capture system and power plant boiler steam turbine system coupled with carbon capture system | |
| CN206889109U (en) | A kind of calcium base decarburization integrated system based on Combined cycle gas-steam turbine | |
| CN114768488B (en) | Coal-fired unit flue gas carbon dioxide entrapment system | |
| CN219630976U (en) | Carbon dioxide collecting system |
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 |