CN116808785B - High-efficiency carbon capturing and energy-saving regeneration device based on biphasic ion solution - Google Patents
High-efficiency carbon capturing and energy-saving regeneration device based on biphasic ion solution Download PDFInfo
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- CN116808785B CN116808785B CN202311098948.0A CN202311098948A CN116808785B CN 116808785 B CN116808785 B CN 116808785B CN 202311098948 A CN202311098948 A CN 202311098948A CN 116808785 B CN116808785 B CN 116808785B
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- 230000008929 regeneration Effects 0.000 title claims abstract description 81
- 238000011069 regeneration method Methods 0.000 title claims abstract description 81
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 17
- 230000002051 biphasic effect Effects 0.000 title claims abstract description 14
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 72
- 150000002500 ions Chemical class 0.000 claims abstract description 68
- 238000001816 cooling Methods 0.000 claims abstract description 59
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 36
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 36
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000003546 flue gas Substances 0.000 claims abstract description 35
- 238000010521 absorption reaction Methods 0.000 claims abstract description 32
- 239000000945 filler Substances 0.000 claims abstract description 20
- 230000003197 catalytic effect Effects 0.000 claims abstract description 19
- 239000007788 liquid Substances 0.000 claims description 146
- 239000007921 spray Substances 0.000 claims description 35
- 239000007789 gas Substances 0.000 claims description 16
- 238000003860 storage Methods 0.000 claims description 14
- 239000000498 cooling water Substances 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 229910000510 noble metal Inorganic materials 0.000 claims description 6
- TYJJADVDDVDEDZ-UHFFFAOYSA-M potassium hydrogencarbonate Chemical compound [K+].OC([O-])=O TYJJADVDDVDEDZ-UHFFFAOYSA-M 0.000 claims description 3
- 230000001172 regenerating effect Effects 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 239000000243 solution Substances 0.000 description 122
- 238000001179 sorption measurement Methods 0.000 description 8
- 238000000034 method Methods 0.000 description 7
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 5
- 238000012856 packing Methods 0.000 description 5
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 4
- 239000002250 absorbent Substances 0.000 description 4
- 230000002745 absorbent Effects 0.000 description 4
- 239000003463 adsorbent Substances 0.000 description 4
- 239000000919 ceramic Substances 0.000 description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 238000001354 calcination Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 229910052763 palladium Inorganic materials 0.000 description 2
- GPNDARIEYHPYAY-UHFFFAOYSA-N palladium(ii) nitrate Chemical compound [Pd+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O GPNDARIEYHPYAY-UHFFFAOYSA-N 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- NWAHZABTSDUXMJ-UHFFFAOYSA-N platinum(2+);dinitrate Chemical compound [Pt+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O NWAHZABTSDUXMJ-UHFFFAOYSA-N 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
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- 238000006477 desulfuration reaction Methods 0.000 description 1
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- 238000010438 heat treatment Methods 0.000 description 1
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Abstract
The invention belongs to the technical field of carbon dioxide trapping, and particularly relates to a high-efficiency carbon trapping and energy-saving regeneration device based on a biphasic ion solution. The invention comprises a flue gas heat exchanger, a cooling tower, a carbon dioxide absorption tower, a regeneration tower and a reboiler. According to the invention, heat of high-temperature flue gas is utilized to provide heat for a reboiler, the first ion solution rich solution and the second ion solution rich solution are regenerated, and carbon dioxide is captured by using the two ion solutions successively by utilizing different characteristics of the two ion solutions, so that the carbon dioxide absorption efficiency is improved; for the first ion solution, the catalytic filler is combined, the regeneration temperature of the rich solution of the first ion solution is reduced, the regeneration energy consumption is reduced, the residual heat after the rich solution of the first ion solution is regenerated is utilized to regenerate the rich solution of the second ion solution, the different characteristics of the two solutions and the heat of the flue gas are fully utilized, and the purpose of reducing the operation energy consumption is achieved.
Description
Technical Field
The invention belongs to the technical field of carbon dioxide trapping, and particularly relates to a high-efficiency carbon trapping and energy-saving regeneration device based on a biphasic ion solution.
Background
The carbon dioxide in the atmosphere mainly comes from six aspects of power generation, transportation, industry, construction industry and animal and plant respiration. The major sources of artificial carbon dioxide emissions are fossil fuel combustion in energy production and transportation, fossil fuel powered factories and power stations worldwide, and countless motor vehicles, whose exhaust gases are the major sources of atmospheric carbon dioxide.
The harm of carbon dioxide to humans is mainly manifested in climate, most typically by the greenhouse effect, which causes glaciers to melt and sea level to rise. The greenhouse effect also affects the atmospheric circulation, which changes the earth's water circulation and thus changes the global precipitation distribution. Viewed from another aspect, carbon dioxide is a carbon resource. The high-concentration carbon dioxide can be applied to various fields such as medical treatment, food, welding and the like. Capturing and sequestering carbon dioxide is currently the most straightforward measure to control carbon dioxide emissions and carbon dioxide recovery.
At present, the main stream carbon dioxide recovery process at home and abroad is MEA process and pressure swing adsorption process. However, aiming at the working condition of adopting dry desulfurization, denitrification and dedusting, if the flue gas temperature is high and the flue gas directly enters an MEA carbon dioxide absorption system or a pressure swing adsorption system, the carbon dioxide is not easy to capture, and a large amount of energy is wasted.
The MEA process is chemical absorption method, which means that CO is utilized 2 Chemically reacting with the absorbent to form a weakly bound intermediate compound, and then enriching the absorbent with CO by changing the conditions 2 CO in the absorption liquid of (a) 2 Desorbing and regenerating the absorbent. A typical chemical absorbent is Monoethanolamine (MEA). The method has some defects of limited popularization, such as high energy consumption due to heating during solvent regeneration, high running cost for the power industry, pollution to air, easy oxidation and degradation, serious corrosion to equipment and the like.
Conventional pressure swing adsorption utilizes the characteristic that the adsorption capacity of an adsorbent for gas changes with pressure, and the adsorbent is used for pressurizing and adsorbing carbon dioxide components in the gas under the condition of selective adsorption, and desorbing the components under reduced pressure to regenerate the adsorbent. Thereby separating the product gas from the impurity components and regenerating the adsorbent. However, other components contained in the flue gas are not easily desorbed under reduced pressure, and the adsorption efficiency of the adsorption material is affected as the adsorption amount increases.
Disclosure of Invention
In order to solve the technical problems, the invention provides a high-efficiency carbon capturing and energy-saving regeneration device based on a biphasic ion solution, which has high absorption efficiency and low regeneration energy consumption.
The invention relates to a high-efficiency carbon capturing and energy-saving regeneration device based on a biphasic ion solution, which comprises the following components: the device comprises a flue gas heat exchanger, a cooling tower, a carbon dioxide absorption tower, a regeneration tower and a reboiler;
the cooling tower includes: the cooling tower comprises a cooling tower air inlet arranged at the lower part of the cooling tower, a cooling tower air outlet arranged at the upper part of the cooling tower, a cooling tower spray pipe arranged at the inner upper part of the cooling tower and a circulating cooling water outlet arranged at the bottom of the cooling tower, wherein the inlet of the cooling tower spray pipe is connected with the circulating cooling water outlet through a cooling circulating pipe arranged outside the cooling tower, and a cooling water circulating pump is arranged on the cooling circulating pipe;
carbon dioxide absorption tower: the inside absorption tower of carbon dioxide divide the liquid dish by the absorption tower and divide into lower tower and last tower, wherein, the lower tower includes: the first ion solution spray pipe is arranged in the lower tower, the gas inlet is arranged at the lower part of the lower tower, and the first rich solution outlet is arranged at the bottom of the lower tower; the upper tower includes: the second ion solution spray pipe is arranged in the tower, and the exhaust port is arranged at the top of the upper tower;
and (3) a regeneration tower: the inside regeneration tower divide into lower regeneration tower and last regeneration tower by regeneration tower branch liquid dish, and wherein, lower regeneration tower includes: the catalytic filler is arranged in the lower regeneration tower, the first spray pipe is arranged at the upper part of the catalytic filler, the high-temperature ion solution inlet is arranged at the lower part of the catalytic filler, the first ion solution circulating outlet is arranged at the bottom of the lower regeneration tower, and the first lean solution outlet is arranged at the lower part of the lower regeneration tower; the upper regeneration tower comprises: the second spray pipe is arranged in the upper regeneration tower, and the carbon dioxide outlet is arranged at the top of the upper regeneration tower;
the hot side inlet of the flue gas heat exchanger is communicated with a high-temperature flue gas source, the hot side outlet of the flue gas heat exchanger is connected with the air inlet of the cooling tower, and the cold side outlet of the flue gas heat exchanger is connected with the hot side inlet of the reboiler;
the gas outlet of the cooling tower is connected with the gas inlet of the lower tower, the first rich solution outlet is connected with the cold side inlet of the first lean-rich solution heat exchanger, the cold side outlet of the first lean-rich solution heat exchanger is connected with the liquid inlet of the first spray pipe, the hot side inlet of the first lean-rich solution heat exchanger is connected with the first lean solution outlet, the hot side outlet of the first lean-rich solution heat exchanger is connected with the hot side inlet of the first lean solution condenser, and the hot side outlet of the first lean solution condenser is connected with the liquid inlet of the first ionic solution spray pipe;
the liquid-separating disc liquid outlet of the absorption tower is connected with the cold side inlet of the second lean-rich liquid heat exchanger, the cold side outlet of the second lean-rich liquid heat exchanger is connected with the liquid inlet of the second spray pipe, the hot side inlet of the second lean-rich liquid heat exchanger is connected with the liquid-separating disc liquid outlet of the regeneration tower, the hot side outlet of the second lean-rich liquid heat exchanger is connected with the hot side inlet of the second lean liquid condenser, and the hot side outlet of the second lean liquid condenser is connected with the liquid inlet of the second ionic solution spray pipe;
the first ionic solution circulation outlet is connected with the cold side inlet of the reboiler, and the cold side outlet of the reboiler is connected with the high-temperature ionic solution inlet.
Preferably, the first ion solution is arranged in the inner cavity of the lower tower, the second ion solution is arranged in the inner cavity of the upper tower, the first ion solution is a solution with the regeneration temperature higher than 120 ℃, the absorption efficiency of carbon dioxide is high, the corrosiveness is low, the regeneration energy consumption is low, and the first ion solution is preferably potassium carbonate solution; the second ion solution is a solution with the regeneration temperature of 100-120 ℃, and DEA solution is preferred for the second ion solution.
Preferably, the catalytic filler is a structured filler with noble metal attached to the surface. Wherein the structured packing is ceramic structured packing; noble metals are platinum and palladium; the adhesion amount of noble metal is 100-800 g/m 2 The method comprises the steps of carrying out a first treatment on the surface of the The preparation method of the catalytic filler comprises the following steps: immersing the ceramic structured packing in a mixed solution of platinum nitrate and palladium nitrate, taking out, and performing anaerobic calcination to obtain the catalyst.
Preferably, the cold side inlet of the flue gas heat exchanger, the cold side inlet of the first lean solution condenser and the cold side inlet of the second lean solution condenser are respectively connected with cold water through pipelines.
Preferably, the lower tower further comprises a first liquid inlet arranged at the lower part of the lower tower, the first liquid inlet is connected with a first ion solution storage tank through a first ion solution delivery pump, and the first ion solution storage tank is filled with a first ion solution.
Preferably, the upper tower further comprises a second liquid inlet arranged at the lower part of the upper tower, the second liquid inlet is connected with a second ion solution storage tank through a second ion solution conveying pump, and the second ion solution storage tank is internally provided with a second ion solution.
Preferably, a first lean liquid pump is arranged between the hot side inlet of the first lean-rich liquid heat exchanger and the first lean liquid outlet.
Preferably, a second lean liquid pump is arranged between the hot side inlet of the second lean-rich liquid heat exchanger and the liquid separating disc liquid outlet of the regeneration tower.
Preferably, a first rich liquid pump is arranged between the first rich liquid outlet and the cold side inlet of the first lean rich liquid heat exchanger.
Preferably, a second rich liquid pump is arranged between the liquid discharge port of the liquid separation disc of the absorption tower and the cold side inlet of the second lean-rich liquid heat exchanger.
Compared with the prior art, the invention has the beneficial effects that:
1. the heat of the high-temperature flue gas is utilized to provide heat for a reboiler, and the first ion solution rich liquid and the second ion solution rich liquid are regenerated;
2. the first ion solution has high absorption efficiency, the second ion solution has low absorption efficiency and low regeneration energy consumption, and the carbon dioxide is captured by using the two ion solutions sequentially by utilizing the different characteristics of the two ion solutions, so that the carbon dioxide absorption efficiency is improved;
3. according to the invention, the two ion solutions are respectively regenerated, and for the first ion solution, the catalytic filler is combined, so that the regeneration temperature of the rich solution of the first ion solution is reduced, the regeneration energy consumption is reduced, the residual heat after the rich solution of the first ion solution is regenerated is utilized to regenerate the rich solution of the second ion solution, the different characteristics of the two solutions and the heat of the flue gas are fully utilized, and the purpose of reducing the operation energy consumption is achieved;
4. the invention has wide application range and can be applied to industries such as iron and steel, metallurgy, building materials, cement and the like.
Drawings
FIG. 1 is a schematic diagram of the structure of the device of the present invention;
in the figure, 1, a flue gas heat exchanger;
2. a cooling tower; 21. an air inlet of the cooling tower; 22. a cooling tower air outlet; 23. a cooling tower spray pipe; 24. a circulating cooling water outlet; 25. a cooling circulation pipe; 26. a cooling water circulation pump;
3. a carbon dioxide absorption tower; 31. a liquid separation disc of the absorption tower; 32. lower tower; 33. loading on a tower; 321. a first ionic solution shower; 322. a gas inlet; 323. a first rich liquid outlet; 324. a first liquid inlet; 325. a first ionic solution delivery pump; 326. a first ionic solution storage tank; 331. a second ionic solution spray pipe; 332. an exhaust port; 333. a second liquid inlet; 334. a second ionic solution delivery pump; 335. a second ionic solution storage tank;
4. a regeneration tower; 41. a liquid separating disc of the regeneration tower; 42. a lower regeneration tower; 43. feeding the waste water to a regeneration tower; 421. catalytic packing; 422. a first shower; 423. a high temperature ionic solution inlet; 424. a first ionic solution circulation outlet; 425. a first lean liquid outlet; 431. a second shower; 432. a carbon dioxide outlet;
5. a reboiler;
6. a first lean-rich liquid heat exchanger; 61. a first lean liquid pump; 62. a first rich liquid pump;
7. a first lean liquid condenser;
8. a second lean-rich liquid heat exchanger; 81. a second lean liquid pump; 82. a second rich liquid pump;
9. a second lean liquid condenser.
Detailed Description
The technical scheme of the present invention will be clearly and completely described in the following with reference to the accompanying drawings and examples.
It should be noted that: relational terms such as first and second, and the like may be used solely to distinguish one entity or action from another entity or action without necessarily representing a sequential relationship.
Example 1
As shown in fig. 1, the efficient carbon capturing and energy-saving regeneration device based on the biphasic ion solution comprises: a flue gas heat exchanger 1, a cooling tower 2, a carbon dioxide absorption tower 3, a regeneration tower 4 and a reboiler 5;
the cooling tower 2 includes: the cooling tower comprises a cooling tower air inlet 21 arranged at the lower part of a cooling tower 2, a cooling tower air outlet 22 arranged at the upper part of the cooling tower 2, a cooling tower spray pipe 23 arranged at the upper part of the cooling tower 2, and a circulating cooling water outlet 24 arranged at the bottom of the cooling tower 2, wherein the inlet of the cooling tower spray pipe 23 is connected with the circulating cooling water outlet 24 through a cooling circulating pipe 25 arranged outside the cooling tower 2, and a cooling water circulating pump 26 is arranged on the cooling circulating pipe 25;
carbon dioxide absorption tower 3: the inside of the carbon dioxide absorption tower 3 is divided into a lower tower 32 and an upper tower 33 by an absorption tower liquid separation tray 31, wherein the lower tower 32 comprises: a first ionic solution spray pipe 321 arranged in the lower tower 32, a gas inlet 322 arranged at the lower part of the lower tower 32, and a first rich solution outlet 323 arranged at the bottom of the lower tower 32; the upper tower 33 includes: a second ion solution shower 331 provided inside, and an exhaust port 332 provided at the top of the upper tower 33;
regeneration tower 4: the inside of the regeneration tower 4 is divided into a lower regeneration tower 42 and an upper regeneration tower 43 by a regeneration tower liquid separation disc 41, wherein the lower regeneration tower 42 comprises: a catalytic filler 421 arranged inside, a first spray pipe 422 arranged at the upper part of the catalytic filler 421, a high-temperature ion solution inlet 423 arranged at the lower part of the catalytic filler 421, a first ion solution circulating outlet 424 arranged at the bottom of the lower regeneration tower 42, and a first lean solution outlet 425 arranged at the lower part of the lower regeneration tower 42; the upper regeneration tower 43 includes: a second spray pipe 431 arranged in the upper regeneration tower 43 and a carbon dioxide gas outlet 432 arranged at the top of the upper regeneration tower 43;
the hot side inlet of the flue gas heat exchanger 1 is communicated with a high-temperature flue gas source, the hot side outlet of the flue gas heat exchanger 1 is connected with the air inlet 21 of the cooling tower, and the cold side outlet of the flue gas heat exchanger 1 is connected with the hot side inlet of the reboiler 5;
the cooling tower air outlet 22 is connected with the air inlet of the lower tower 32, the first rich liquid outlet 323 is connected with the cold side inlet of the first lean-rich liquid heat exchanger 6, the cold side outlet of the first lean-rich liquid heat exchanger 6 is connected with the liquid inlet of the first spray pipe 422, the hot side inlet of the first lean-rich liquid heat exchanger 6 is connected with the first lean liquid outlet 425, the hot side outlet of the first lean-rich liquid heat exchanger 6 is connected with the hot side inlet of the first lean liquid condenser 7, and the hot side outlet of the first lean liquid condenser 7 is connected with the liquid inlet of the first ionic solution spray pipe 321;
the liquid outlet of the liquid separation disc 31 of the absorption tower is connected with the cold side inlet of the second lean-rich liquid heat exchanger 8, the cold side outlet of the second lean-rich liquid heat exchanger 8 is connected with the liquid inlet of the second spray pipe 431, the hot side inlet of the second lean-rich liquid heat exchanger 8 is connected with the liquid outlet of the liquid separation disc 41 of the regeneration tower, the hot side outlet of the second lean-rich liquid heat exchanger 8 is connected with the hot side inlet of the second lean liquid condenser 9, and the hot side outlet of the second lean liquid condenser 9 is connected with the liquid inlet of the second ionic solution spray pipe 331;
the first ionic solution circulation outlet 424 is connected to the cold side inlet of the reboiler 5, and the cold side outlet of the reboiler 5 is connected to the high temperature ionic solution inlet 423.
The inner cavity of the lower tower 32 is filled with a first ionic solution, the inner cavity of the upper tower 33 is filled with a second ionic solution, and the first ionic solution is potassium carbonate solution; the second ion solution is DEA solution;
the catalytic filler 421 is a ceramic structured filler with noble metals platinum and palladium attached to the surface, and the attached amount of the noble metals is 100-800 g/m 2 . The preparation method of the catalytic filler comprises the following steps: immersing the ceramic structured packing in a mixed solution of platinum nitrate and palladium nitrate, taking out, and performing anaerobic calcination to obtain the catalyst.
The cold side inlet of the flue gas heat exchanger 1, the cold side inlet of the first lean solution condenser 7 and the cold side inlet of the second lean solution condenser 9 are respectively connected with cold water through pipelines.
A first lean liquid pump 61 is provided between the hot side inlet of the first lean-rich liquid heat exchanger 6 and the first lean liquid outlet 425.
A second lean liquid pump 81 is arranged between the hot side inlet of the second lean-rich liquid heat exchanger 8 and the liquid outlet of the liquid separating disc 41 of the regeneration tower.
A first rich liquid pump 62 is arranged between the first rich liquid outlet 323 and the cold side inlet of the first lean rich liquid heat exchanger 6.
A second rich liquid pump 82 is arranged between the liquid outlet of the liquid separating disc 31 of the absorption tower and the cold side inlet of the second lean-rich liquid heat exchanger 8.
The working process of the invention is as follows:
high-temperature flue gas enters from a hot side inlet of the flue gas heat exchanger 1, indirectly exchanges heat with cold water to be cooled to 90-100 ℃, enters into a cooling tower 2 from a hot side outlet of the flue gas heat exchanger 1, reversely contacts with circulating cooling water sprayed by a cooling tower spray pipe 23, and is cooled to 40 ℃; the flue gas enters the gas inlet 322 from the cooling tower gas outlet 22, thus entering the lower tower 32, flows from bottom to top, contacts with the first ionic solution first and causes most of CO to flow 2 After being absorbed, the residual flue gas passes through the liquid separation disc 31 of the absorption tower and enters the upper tower 33 to contact with the second ion solution, so as to lead the residual CO in the flue gas 2 Absorbed and then discharged from the exhaust port 332;
the first ion solution rich liquid at the bottom of the lower tower 32 passes through the first rich liquid outlet 323The first rich liquid pump 62 enters the cold side inlet of the first lean-rich liquid heat exchanger 6, exchanges heat with the first ion solution lean liquid and heats up, and enters the lower regeneration tower 42 through the first spray pipe 422 through the cold side outlet of the first lean-rich liquid heat exchanger 6; the first ionic solution in the lower regeneration tower 42 enters the cold side inlet of the reboiler 5 through the first ionic solution circulation outlet 424, indirectly exchanges heat with hot water (90-100 ℃) provided by the cold side outlet of the flue gas heat exchanger 1, then enters the flue gas heat exchanger through the high-temperature ionic solution inlet 423, heats the first ionic solution rich solution in the lower regeneration tower 42, and simultaneously under the action of the catalytic filler 421, the CO in the first ionic solution rich solution 2 The gas is separated and continuously rises, enters the upper regeneration tower 43 to be in reverse contact with the second ion solution rich liquid after passing through the absorption tower liquid separation disc 31, heats the second ion solution rich liquid and CO 2 The gas is separated and discharged from the carbon dioxide outlet 432;
the first ionic solution lean solution in the lower regeneration tower 42 enters the hot side inlet of the first lean-rich solution heat exchanger 6 from the first lean solution outlet 425 through the first lean solution pump 61, indirectly exchanges heat with cold water for cooling, and enters the first ionic solution spray pipe 321 from the hot side outlet of the first lean-rich solution heat exchanger 6; the second ionic solution lean solution in the upper regeneration tower 43 enters a hot side inlet of the second lean-rich solution heat exchanger 8 from a liquid outlet of a liquid separating disc 41 of the regeneration tower through a second lean liquid pump 81, indirectly exchanges heat with cold water for cooling, and enters a second ionic solution spray pipe 331 from a hot side outlet of the second lean-rich solution heat exchanger 8; both ionic solutions complete the regeneration cycle.
Example 2
As shown in fig. 1, on the basis of embodiment 1, the lower tower 32 further includes a first liquid inlet 324 disposed at a lower portion of the lower tower 32, the first liquid inlet 324 is connected to a first ionic solution storage tank 326 through a first ionic solution delivery pump 325, and the first ionic solution storage tank 326 is filled with a first ionic solution;
the upper tower 33 further comprises a second liquid inlet 333 arranged at the lower part of the upper tower 33, the second liquid inlet 333 is connected with a second ion solution storage tank 335 through a second ion solution delivery pump 334, and the second ion solution storage tank 335 is filled with a second ion solution.
The first ionic solution in the first ionic solution tank 326 is fed into the lower column 32 by the first ionic solution delivery pump 325 and the second ionic solution in the second ionic solution tank 335 is fed into the upper column 33 by the second ionic solution delivery pump 334.
Claims (9)
1. The utility model provides a high-efficient carbon entrapment and energy-conserving regenerating unit based on diphase ion solution which characterized in that includes: a flue gas heat exchanger (1), a cooling tower (2), a carbon dioxide absorption tower (3), a regeneration tower (4) and a reboiler (5);
the cooling tower (2) comprises: the cooling tower comprises a cooling tower air inlet (21) arranged at the lower part of a cooling tower (2), a cooling tower air outlet (22) arranged at the upper part of the cooling tower (2), a cooling tower spray pipe (23) arranged at the inner upper part of the cooling tower (2) and a circulating cooling water outlet (24) arranged at the bottom of the cooling tower (2), wherein the inlet of the cooling tower spray pipe (23) is connected with the circulating cooling water outlet (24) through a cooling circulation pipe (25) arranged outside the cooling tower (2), and a cooling water circulation pump (26) is arranged on the cooling circulation pipe (25);
carbon dioxide absorption tower (3): the inside of the carbon dioxide absorption tower (3) is divided into a lower tower (32) and an upper tower (33) by an absorption tower liquid separation disc (31), wherein the lower tower (32) comprises: a first ion solution spray pipe (321) arranged in the lower tower (32), a gas inlet (322) arranged at the lower part of the lower tower (32), and a first rich solution outlet (323) arranged at the bottom of the lower tower (32); the upper tower (33) comprises: a second ion solution spray pipe (331) arranged in the tower, and an exhaust port (332) arranged at the top of the upper tower (33);
regeneration tower (4): the interior of the regeneration tower (4) is divided into a lower regeneration tower (42) and an upper regeneration tower (43) by a regeneration tower liquid separation disc (41), wherein the lower regeneration tower (42) comprises: the catalytic device comprises a catalytic filler (421) arranged inside, a first spray pipe (422) arranged at the upper part of the catalytic filler (421), a high-temperature ion solution inlet (423) arranged at the lower part of the catalytic filler (421), a first ion solution circulation outlet (424) arranged at the bottom of a lower regeneration tower (42), and a first lean solution outlet (425) arranged at the lower part of the lower regeneration tower (42); the upper regeneration tower (43) comprises: a second spray pipe (431) arranged in the upper regeneration tower (43) and a carbon dioxide gas outlet (432) arranged at the top of the upper regeneration tower (43);
the hot side inlet of the flue gas heat exchanger (1) is communicated with a high-temperature flue gas source, the hot side outlet of the flue gas heat exchanger (1) is connected with the air inlet (21) of the cooling tower, and the cold side outlet of the flue gas heat exchanger (1) is connected with the hot side inlet of the reboiler (5);
the cooling tower air outlet (22) is connected with the air inlet (322) of the lower tower (32), the first rich liquid outlet (323) is connected with the cold side inlet of the first lean-rich liquid heat exchanger (6), the cold side outlet of the first lean-rich liquid heat exchanger (6) is connected with the liquid inlet of the first spray pipe (422), the hot side inlet of the first lean-rich liquid heat exchanger (6) is connected with the first lean liquid outlet (425), the hot side outlet of the first lean-rich liquid heat exchanger (6) is connected with the hot side inlet of the first lean liquid condenser (7), and the hot side outlet of the first lean liquid condenser (7) is connected with the liquid inlet of the first ionic solution spray pipe (321);
the liquid outlet of the liquid separating disc (31) of the absorption tower is connected with the cold side inlet of the second lean-rich liquid heat exchanger (8), the cold side outlet of the second lean-rich liquid heat exchanger (8) is connected with the liquid inlet of the second spray pipe (431), the hot side inlet of the second lean-rich liquid heat exchanger (8) is connected with the liquid outlet of the liquid separating disc (41) of the regeneration tower, the hot side outlet of the second lean-rich liquid heat exchanger (8) is connected with the hot side inlet of the second lean liquid condenser (9), and the hot side outlet of the second lean liquid condenser (9) is connected with the liquid inlet of the second ionic solution spray pipe (331);
the first ionic solution circulation outlet (424) is connected with the cold side inlet of the reboiler (5), and the cold side outlet of the reboiler (5) is connected with the high-temperature ionic solution inlet (423);
the inner cavity of the lower tower (32) is filled with a first ion solution, the inner cavity of the upper tower (33) is filled with a second ion solution, the first ion solution is a potassium carbonate solution, and the second ion solution is a DEA solution.
2. The efficient carbon capture and energy-saving regeneration device based on the biphasic ionic solution according to claim 1, wherein the catalytic filler (421) is a structured filler with noble metal attached to the surface.
3. The efficient carbon capturing and energy-saving regeneration device based on the biphasic ion solution according to claim 1, wherein a cold side inlet of the flue gas heat exchanger (1), a cold side inlet of the first lean solution condenser (7) and a cold side inlet of the second lean solution condenser (9) are respectively connected with cold water through pipelines.
4. The two-phase ionic solution-based efficient carbon capture and energy-saving regeneration device according to claim 1, wherein the lower tower (32) further comprises a first liquid inlet (324) arranged at the lower part of the lower tower (32), the first liquid inlet (324) is connected with a first ionic solution storage tank (326) through a first ionic solution delivery pump (325), and the first ionic solution storage tank (326) is filled with a first ionic solution.
5. The efficient carbon capturing and energy-saving regeneration device based on the biphasic ionic solution according to claim 1, wherein the upper tower (33) further comprises a second liquid inlet (333) arranged at the lower part of the upper tower (33), the second liquid inlet (333) is connected with a second ionic solution storage tank (335) through a second ionic solution delivery pump (334), and the second ionic solution storage tank (335) is filled with a second ionic solution.
6. The efficient carbon capturing and energy-saving regeneration device based on the biphasic ionic solution according to claim 1, wherein a first lean liquid pump (61) is arranged between the hot side inlet of the first lean-rich liquid heat exchanger (6) and the first lean liquid outlet (425).
7. The efficient carbon capturing and energy-saving regeneration device based on the biphasic ionic solution according to claim 1, wherein a second lean liquid pump (81) is arranged between a hot side inlet of the second lean-rich liquid heat exchanger (8) and a liquid outlet of a liquid separating disc (41) of the regeneration tower.
8. The efficient carbon capturing and energy-saving regeneration device based on the biphasic ion solution according to claim 1, wherein a first rich liquid pump (62) is arranged between the first rich liquid outlet (323) and the cold side inlet of the first lean rich liquid heat exchanger (6).
9. The efficient carbon capturing and energy-saving regeneration device based on the biphasic ion solution according to claim 1, wherein a second rich liquid pump (82) is arranged between a liquid outlet of a liquid separation disc (31) of the absorption tower and a cold side inlet of a second lean-rich liquid heat exchanger (8).
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102596364A (en) * | 2009-09-15 | 2012-07-18 | 阿尔斯通技术有限公司 | Method and system for removal of carbon dioxide from a process gas |
| CN105503732A (en) * | 2015-11-25 | 2016-04-20 | 河北科技大学 | Ether-based bis-imidazole ionic liquid used for absorbing SO2, preparation method and application method thereof |
| CN105521696A (en) * | 2015-11-26 | 2016-04-27 | 南京大学 | Room-temperature liquid-phase Claus process taking ionic liquid as media |
| CN109193009A (en) * | 2018-09-19 | 2019-01-11 | 中国科学院上海高等研究院 | Solid oxide fuel cell composite system and application method |
| CN114210176A (en) * | 2021-12-15 | 2022-03-22 | 北京民利储能技术有限公司 | Carbon dioxide capture process and simulation method coupled with heat recovery |
| CN116078138A (en) * | 2022-12-05 | 2023-05-09 | 安徽威达环保科技股份有限公司 | Device and process for removing carbon dioxide in flue gas by using hot potash method |
| CN116139660A (en) * | 2023-01-16 | 2023-05-23 | 中国能源建设集团广东省电力设计研究院有限公司 | Carbon dioxide trapping system |
-
2023
- 2023-08-30 CN CN202311098948.0A patent/CN116808785B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102596364A (en) * | 2009-09-15 | 2012-07-18 | 阿尔斯通技术有限公司 | Method and system for removal of carbon dioxide from a process gas |
| CN105503732A (en) * | 2015-11-25 | 2016-04-20 | 河北科技大学 | Ether-based bis-imidazole ionic liquid used for absorbing SO2, preparation method and application method thereof |
| CN105521696A (en) * | 2015-11-26 | 2016-04-27 | 南京大学 | Room-temperature liquid-phase Claus process taking ionic liquid as media |
| CN109193009A (en) * | 2018-09-19 | 2019-01-11 | 中国科学院上海高等研究院 | Solid oxide fuel cell composite system and application method |
| CN114210176A (en) * | 2021-12-15 | 2022-03-22 | 北京民利储能技术有限公司 | Carbon dioxide capture process and simulation method coupled with heat recovery |
| CN116078138A (en) * | 2022-12-05 | 2023-05-09 | 安徽威达环保科技股份有限公司 | Device and process for removing carbon dioxide in flue gas by using hot potash method |
| CN116139660A (en) * | 2023-01-16 | 2023-05-23 | 中国能源建设集团广东省电力设计研究院有限公司 | Carbon dioxide trapping system |
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