CN116422124B - Carbon trapping pretreatment tower suitable for high-temperature flue gas - Google Patents
Carbon trapping pretreatment tower suitable for high-temperature flue gas Download PDFInfo
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- CN116422124B CN116422124B CN202310457271.9A CN202310457271A CN116422124B CN 116422124 B CN116422124 B CN 116422124B CN 202310457271 A CN202310457271 A CN 202310457271A CN 116422124 B CN116422124 B CN 116422124B
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 61
- 239000003546 flue gas Substances 0.000 title claims abstract description 61
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 40
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 39
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 41
- 238000012856 packing Methods 0.000 claims abstract description 26
- 239000007788 liquid Substances 0.000 claims description 60
- 238000005406 washing Methods 0.000 claims description 56
- 230000007704 transition Effects 0.000 claims description 28
- 239000007789 gas Substances 0.000 claims description 11
- 238000004804 winding Methods 0.000 claims 2
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- 210000000476 body water Anatomy 0.000 abstract description 5
- 230000007246 mechanism Effects 0.000 abstract description 4
- 238000010521 absorption reaction Methods 0.000 description 17
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 14
- 238000000034 method Methods 0.000 description 14
- 238000005516 engineering process Methods 0.000 description 12
- 239000000126 substance Substances 0.000 description 9
- 239000001569 carbon dioxide Substances 0.000 description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 239000000498 cooling water Substances 0.000 description 6
- 239000000945 filler Substances 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 5
- 238000006477 desulfuration reaction Methods 0.000 description 5
- 230000023556 desulfurization Effects 0.000 description 5
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- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
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- 239000003513 alkali Substances 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005202 decontamination Methods 0.000 description 2
- 230000003588 decontaminative effect Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
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- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
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Abstract
The invention discloses a carbon capture pretreatment tower suitable for high-temperature flue gas, which comprises an inlet flue, a heat exchanger, a packing tower and packing, wherein the packing tower is arranged one above the other with the inlet flue, a plurality of tower air inlets and a plurality of tower air outlets are respectively arranged at the outer wall of a tower body and the outer wall of a channel body in a surrounding manner, the heat exchanger comprises a shell, a water inlet main pipe, a heat exchange tube bundle and a water outlet main pipe, the plurality of heat exchangers are respectively wrapped outside the packing tower in a surrounding manner, the inner wall of the shell is respectively provided with a shell air outlet and a shell air inlet which can be correspondingly communicated with the air inlets and the air outlets of the various towers, the heat exchange tube bundle is arranged in the inner cavity of the shell, the outer wall of the tower body of the packing tower is also provided with a tower body water outlet, a tower water inlet and a tower air outlet, and the outer wall of the channel of the inlet flue is also provided with a channel air inlet, and the packing is filled in the inner cavity of the tower body of the packing tower, multiple heat exchange mechanism complementation can be realized, and the cooling and dirt removing functions are integrated.
Description
[ Field of technology ]
The invention relates to the technical field of carbon capture, in particular to the technical field of a carbon capture pretreatment tower suitable for high-temperature flue gas.
[ Background Art ]
Carbon capture technology is being widely focused on by universities and research institutions at home and abroad as an important technical route for achieving carbon peak and carbon neutralization. The carbon trapping technology is mainly classified into a pre-combustion carbon trapping technology, a post-combustion carbon trapping technology and an oxygen-enriched combustion technology. Because of the characteristics of large quantity, large scale and difficult realization of new energy substitution in a short time of the existing coal-fired enterprises in China, especially coal-fired power plants, the carbon capture technology after combustion becomes the most suitable technology for realizing carbon reduction and even zero carbon emission of the coal-fired enterprises in China at the present stage due to the low transformation cost of the existing system. The chemical absorption method carbon trapping technology is based on a solvent absorption technology and is the most mature carbon trapping technology after combustion at present. The principle of the carbon trapping technology by the chemical absorption method is that a chemical solvent reacts with carbon dioxide in flue gas in an absorption tower to form an intermediate compound with weak connectivity so as to realize the absorption of the carbon dioxide, and the carbon dioxide can be desorbed by heating the intermediate compound, so that the continuous trapping of the carbon dioxide is finally completed through the alternation of the absorption and the desorption.
Because the tail end flue gas temperature is lower after the flue gas in most industries is subjected to purification procedures such as dust removal and desulfurization, when the chemical absorption method carbon capture is carried out, the factory can meet the requirements of the flue gas chemical absorption reaction only by arranging a pretreatment tower at the upstream of the carbon capture absorption tower to carry out pretreatment such as deep desulfurization, dehydration, water supplementing and the like on the flue gas. In addition, the existing carbon capture device by chemical absorption method is further provided with a temperature monitoring device to monitor whether the temperature of the flue gas is low enough in real time to ensure sufficient adsorption of carbon dioxide, such as a carbon capture system stable absorption control system and method disclosed in the utility model patent with publication number of CN115581994A and a water balance adjusting device for wet desulfurization flue gas double-alkali carbon capture disclosed in the utility model patent with publication number of CN 216630312U.
However, the flue gas in part of industries has the problem of higher temperature of the tail end flue gas, such as high-temperature flue gas discharged in certain working sections in the industries of metallurgy and the like, because the flue gas has no strict ultralow emission index on one hand and the wet desulfurization treatment on the other hand is not needed. When the high-temperature flue gas is subjected to carbon capture by a chemical absorption method, the flue gas cannot be cooled to the optimal reaction temperature for carbon dioxide absorption through a single pretreatment tower, and a flue gas cooler is generally arranged on a flue at the upstream of the pretreatment tower. That is, when carbon capturing is performed on high temperature flue gas, the pretreatment device needs to include both an upstream flue gas cooler and a downstream pretreatment tower. The flue gas cooler is mainly used for primarily cooling high-temperature flue gas. However, the conventional carbon capture system by chemical absorption method comprises a pretreatment tower, an absorption tower, a regeneration tower and other equipment, so that the investment cost is high, and if a flue gas cooler is arranged independently, the project cost is increased remarkably, so that the aim of high technical economy is not achieved. In addition, the existing flue gas cooler is generally arranged on a flue, so that the problems of high installation requirement and difficult maintenance exist, and the manufacturing, installation and debugging quality is difficult to ensure. Therefore, if such a design is adopted, once the flue gas cooler has burst problems during operation, the problem of reduced pretreatment efficiency is caused, and further a series of adverse effects are caused on the subsequent absorption of carbon dioxide. I.e. such a design places stringent demands on the reliability of the flue gas cooler.
[ Invention ]
The invention aims to solve the problems in the prior art, provides a carbon capture pretreatment tower suitable for high-temperature flue gas, can realize complementation of multiple heat exchange mechanisms, integrates the functions of cooling and decontamination, and can perform efficient pretreatment on the high-temperature flue gas in the industries of metallurgy and the like.
In order to achieve the above purpose, the invention provides a carbon capture pretreatment tower suitable for high-temperature flue gas, which comprises an inlet flue, a heat exchanger, a filler tower and a filler, wherein the filler tower is arranged one by one with the inlet flue, a plurality of tower air inlets and tower air outlets are respectively arranged at the positions of the outer wall of the tower body and the outer wall of the channel body in a surrounding manner, the heat exchanger comprises a shell, a water inlet main pipe, a heat exchange tube bundle and a water outlet main pipe, a plurality of heat exchangers are respectively wrapped outside the filler tower in a surrounding manner, shell air outlets and shell air inlets which can be correspondingly communicated with the air inlets and the air outlets of the tower bodies are respectively arranged at the inner wall of the shell, the heat exchange tube bundle is arranged in the shell inner cavity of the shell, one end of the water inlet main pipe and one end of the water outlet main pipe extend into the shell inner cavity of the shell and are respectively communicated with the heat exchange tube bundle, a tower body water outlet, a tower body water inlet and a tower air inlet are respectively arranged at the outer wall of the channel of the inlet, and the filler is arranged in the tower inner cavity of the filler tower.
Preferably, the heat exchanger further comprises a skirt seat barrel, wherein the skirt seat barrel is positioned below the packed tower, a plurality of notches are formed in the top surface of the skirt seat barrel in a surrounding mode, and the bottom ends of the heat exchangers are respectively arranged in the notches.
Preferably, the inlet flue comprises an inlet section and a transition zone, the transition zone is funnel-shaped and is positioned in the inner cavity of the barrel of the skirt barrel, the inlet section is horizontally arranged, a passage air inlet is formed in the passage outer wall of one end of the inlet section, the other end of the inlet section firstly extends into the inner cavity of the barrel of the skirt barrel and then is bent upwards and connected with the transition zone, and each passage outlet is positioned at the passage outer wall of the transition zone.
Preferably, the packed tower comprises a washing liquid area and a washing area, wherein the washing area and the washing liquid area are arranged one above the other, and the washing liquid area is funnel-shaped and sinks into a transition inner cavity of the transition area.
Preferably, a plurality of reinforcing plates are arranged in the transition inner cavity of the transition zone in a surrounding mode, and the washing liquid zone is supported by the reinforcing plates.
Preferably, the water inlet of the tower body is positioned at the side part of the washing area, the air outlet of the tower body is positioned at the top of the washing area, the water outlet of the tower body is positioned at the side part of the washing liquid area, and a drain pipe extending out of the inner cavity of the barrel body of the skirt seat barrel is further arranged at the bottom of the washing liquid area.
Preferably, the heat exchanger further comprises a baffle plate, and a plurality of baffle plates are respectively arranged on each heat exchange branch pipe of the heat exchange pipe bundle and form an S-shaped path for enabling cooling water to flow in a meandering manner.
Preferably, a guide plate is further arranged at the air inlet of the tower body, and the guide plate is inclined gradually descending from the fixed end to the free end.
Preferably, the tower also comprises a gas distributor and a liquid distributor, wherein the gas distributor is arranged close to each heat exchanger and enables the flue gas to flow upwards through the gas distributor and then along the inner cavity of the tower, and the liquid distributor is arranged close to the water inlet of the tower and enables the washing liquid to flow downwards through the liquid distributor and then along the inner cavity of the tower.
Preferably, a demister is further arranged in the inner cavity of the tower body and between the liquid distributor and the air outlet of the tower body.
The invention has the beneficial effects that:
The invention forms triple convection through the flue gas-tower external cooling water in the heat exchanger, the side washing liquid in the flue gas-washing liquid area in the heat exchanger and the bottom washing liquid in the flue gas-washing liquid area in the inlet flue, and on the other hand, the invention utilizes the conduction heat exchange mechanism and the gas-liquid mass transfer heat exchange in the packed tower, so that the temperature regulation of high-temperature flue gas is multiple enhanced, the material consumption and the energy consumption required by cooling can be reduced on the premise of ensuring the outlet index, the whole structure is simple and reliable, the integration of the flue gas cooler and the pretreatment tower which are originally independently arranged can be realized, the operation and maintenance are convenient, the structure is stable and reliable, the occupied area is greatly saved, the requirements of the double-carbon policy are met, the CCUS layout and development are quickened, and the invention is very suitable for the carbon capture pretreatment tower with the flue gas temperature of more than 80 ℃.
As the chemical absorption method is integrally demonstrated in industry in terms of technical maturity, the method can be used as a technical reserve for meeting policy requirements, technical deepening and application expansion.
The features and advantages of the present invention will be described in detail by way of example with reference to the accompanying drawings.
[ Description of the drawings ]
FIG. 1 is a front view of a carbon capture pretreatment tower suitable for use with high temperature flue gas of the present invention;
FIG. 2 is a schematic perspective view of an inlet flue of a carbon capture pretreatment tower for high temperature flue gas according to the present invention;
FIG. 3 is a schematic perspective view of a skirt of a carbon capture pretreatment tower for high temperature flue gas according to the present invention;
FIG. 4 is a schematic perspective view of a heat exchanger of a carbon capture pretreatment tower for high temperature flue gas according to the present invention;
FIG. 5 is a schematic view showing the internal structure of a heat exchanger of a carbon capture pretreatment tower suitable for high temperature flue gas according to the present invention;
FIG. 6 is a diagram of the position of the column air inlet of the packed column of the carbon capture pretreatment column of the present invention for high temperature flue gas.
In the figure: 1-inlet flue, 11-inlet section, 12-transition zone, 13-channel air outlet, 2-skirt seat cylinder, 21-skirt seat straight section, 22-notch, 23-raised part, 3-heat exchanger, 31-shell, 32-shell air inlet, 33-shell air outlet, 34-water inlet main pipe, 35-heat exchange tube bundle, 36-baffle plate, 37-water outlet main pipe, 4-packed tower, 41-washing liquid zone, 42-washing zone, 43-blow-down pipe, 44-tower water outlet, 45-tower air inlet, 46-tower water inlet, 47-tower air outlet, 5-gas distributor, 6-packing, 7-liquid distributor and 8-demister.
[ Detailed description ] of the invention
Referring to fig. 1 to 6, the carbon capture pretreatment tower suitable for high temperature flue gas according to the present invention comprises an inlet flue 1, a heat exchanger 3, a packing tower 4 and a packing 6, wherein the packing tower 4 is disposed above and below the inlet flue 1, a plurality of tower air inlets 45 and a plurality of channel air outlets 13 are respectively disposed at the outer wall of the tower body and the outer wall of the channel, the heat exchanger 3 comprises a shell 31, a water inlet manifold 34, a heat exchange tube bundle 35 and a water outlet manifold 37, the plurality of heat exchangers 3 are respectively disposed outside the packing tower 4 in a surrounding manner, a shell air outlet 33 and a shell air inlet 32 which can be correspondingly communicated with the respective tower air inlets 45 and flue outlets 13 are respectively disposed at the inner wall of the shell 31, the heat exchange tube bundle 35 is disposed in the shell cavity of the shell 31, the water inlet manifold 34 and the water outlet manifold 37 are disposed above and below, one end of each of the heat exchange tube bundle 35 is respectively extended into the shell cavity of the shell 31 and is communicated with the heat exchange tube bundle 35, a tower water outlet 44, a tower water inlet 46 and a tower air outlet 47 are respectively disposed at the outer wall of the packing tower 4, and the channel air inlet 4 is disposed in the channel 4. The casing 31 is in an arc plate shape as a whole, and has a flat bottom surface and an inclined top surface. The opening angle of the housing air inlet 32 is 110-130 deg. and the opening height is 500-1400 mm, and the opening angle of the housing air outlet 33 is 110-130 deg.. The packing 6 has a material separation function and can strengthen the effect of gas-liquid mass transfer in the tower, can be arranged in 2-3 layers, and adopts low-pressure-drop bulk or structured packing.
The heat exchanger further comprises a skirt seat barrel 2, wherein the skirt seat barrel 2 is positioned below the packed tower 4, a plurality of notches 22 are formed in the top surface in a surrounding mode, and the bottom ends of the heat exchangers 3 are respectively arranged in the notches 22. Wherein each heat exchanger 3 can be welded in the corresponding recess 22. In addition, each notch 22 forms a plurality of raised portions 23 on the top surface of the skirt barrel 2, and the outer wall of the packed tower 4 above each raised portion 23 (i.e. the outer wall of the packed tower 4 between two adjacent heat exchangers 3) can be used for providing components such as meters and pipeline interfaces. The above-mentioned components are preferably installed in a region of 25 to 35 ° between two adjacent heat exchangers 3. The difference in height between the bottom surface of the notch 22 and the top surface of the raised portion 23 is 500 to 1400mm, and the height of the notch is equal to the opening height of the duct air outlet 13.
The inlet flue 1 comprises an inlet section 11 and a transition zone 12, the transition zone 12 is funnel-shaped and is positioned in the inner cavity of the skirt barrel 2, the inlet section 11 is horizontally arranged, a passage air inlet is arranged at the passage outer wall of one end of the inlet section, the other end of the inlet section firstly extends into the inner cavity of the skirt barrel 2 and then is bent upwards and connected with the transition zone 12, and each passage outlet 13 is positioned at the passage outer wall of the transition zone 12. Wherein the slope of the funnel-shaped top of the transition zone 12 is 10-15 degrees, the opening angle of the channel body outlet 13 is 110-130 degrees, and the opening height is 500-1400 mm.
The packed column 4 comprises a washing liquid zone 41 and a washing zone 42, wherein the washing zone 42 and the washing liquid zone 41 are arranged one above the other, and the washing liquid zone 41 is funnel-shaped and sinks into the transition inner cavity of the transition zone 12. Wherein the side surface of the washing liquid region 41 is attached to each heat exchanger 3, so that the washing liquid accumulated in the washing cavity of the washing liquid region 41 is used for conducting heat exchange with the flue gas flowing through each heat exchanger 3 from the side. Furthermore, it is possible to provide a device for the treatment of a disease. The funnel-shaped profile of the wash liquor zone 41 and the transition zone 12 also allows for partial heat transfer from the bottom of the wash liquor accumulated in the wash chamber of the wash liquor zone 41 to the flue gas located in the transition chamber of the transition zone 12. The funnel-shaped bottom slope of the washing liquid area 41 is 10-15 degrees, the opening angle of the tower air inlet 45 is 110-130 degrees, and the opening height is 500-1400 mm.
A plurality of reinforcing plates are also arranged in the transition inner cavity of the transition zone 12 in a surrounding manner, and the washing liquid zone 41 is supported by the reinforcing plates.
The tower water inlet 46 is positioned at the side part of the washing area 42, the tower air outlet 47 is positioned at the top part of the washing area 42, the tower water outlet 44 is positioned at the side part of the washing liquid area 41, and the bottom part of the washing liquid area 41 is also provided with a drain pipe 43 extending out of the inner cavity of the cylinder body of the skirt seat cylinder 2. In operation, the scrubbing liquid is injected into the tower body cavity of the packed tower 4 along the tower body water inlet 46 and is discharged from the tower body water outlet 44, thereby forming water balance in the tower. Further, the washed sewage may be discharged through the drain pipe 43 as necessary. The flue gas after decontamination and temperature reduction is finally discharged through the tower air outlet 47 and enters the subsequent process. The washing liquid can be industrial water or NaOH alkali liquor according to the contents of SO 2 and NO x in the flue gas, and the pH range is 6-8.
The heat exchanger 3 further comprises a baffle plate 36, and a plurality of baffle plates 36 are respectively arranged on each heat exchange branch pipe of the heat exchange tube bundle 35 and form an S-shaped path for enabling cooling water to flow in a meandering manner. Wherein, each baffle 36 may be arranged in staggered layers, and the adjacent upper and lower baffles 36 may be welded at the inner side wall and the outer side wall of the casing 31, respectively.
And each tower air inlet 45 is also provided with a guide plate, and the guide plates are inclined gradually descending from the fixed end to the free end. Wherein, the inclination angle of the guide plate is 45 degrees downwards, and the guide plate can be used as a flow blocking eave to prevent the washing liquid from entering the inner cavity of the shell 31.
The gas distributor 5 is arranged close to each heat exchanger 3, and enables flue gas to flow upwards through the gas distributor 5 and then along the inner cavity of the tower body, and the liquid distributor 7 is arranged close to the water inlet 46 of the tower body, and enables washing liquid to flow downwards through the liquid distributor 7 and then along the inner cavity of the tower body. The liquid distributor 7 can adopt a porous liquid distributor and an overflow liquid distributor, so that the washing liquid injected through the tower water inlet 46 is uniformly distributed above the packing 6, and the efficiency of the packing 6 is helped to be exerted. In addition, the gas distributor 5 is communicated with the tower air outlet 47 to assist in achieving uniform gas flow distribution.
A demister 8 is arranged in the tower body cavity and between the liquid distributor 7 and the tower body air outlet 47. Wherein, defroster 8 installs in the 4 tops of packing tower for liquid droplet in the separation flue gas can adopt wire mesh defroster, baffling board defroster or above-mentioned defroster's combination, still can dispose defroster washing unit simultaneously in order to further improve the defogging effect.
Regarding the material, the heat exchanger 31 is entirely made of stainless steel and is welded with the skirt 2 and the packing tower 4 respectively, while the packing tower 4 and the inner member welded with the packing tower are made of carbon steel, the other inner members are made of materials with good corrosion resistance, and the inner lining of the packing tower 4 is also made of corrosion resistant materials.
The working process of the invention comprises the following steps:
flow route of flue gas: the flue gas flows into the transition cavity of the transition zone 12 along the channel air inlet, and then enters the shell cavity of the shell 31 after passing through the channel air outlet 13, the notch 22 and the shell air inlet 32. The flue gas then passes through the shell air outlet 33 and the tower air inlet 45 before entering the tower interior of the packed tower 4. Finally, the flue gas is discharged through the tower air outlet 47 after passing through the gas distributor 5, the packing 6, the liquid distributor 7 and the demister 8 in this order upward.
Flow route of cooling water: the cooling water is externally connected to the water inlet manifold 34 and is discharged from the water outlet manifold 37 after flowing through the heat exchange tube bundle 35, and heat exchange with the flue gas is completed in the process. I.e. water inlet header 34 and water outlet header 37 are the parent tubes of heat exchange tube bundle 35.
The flow route of the washing liquid: the washing liquid is connected into the tower water inlet 46 from the outside, is uniformly sprayed by the liquid distributor 7, is accumulated in the washing cavity of the washing liquid area 41, and is finally discharged through the drain pipe 43 or the tower water outlet 44.
In normal operation, the convection effect of the flue gas in the inner cavity of the housing 31 and the external cooling water is a primary heat exchange process, and the heat conduction effect between the flue gas in the inner cavity of the housing 31 and the side and bottom of the washing liquid area 41 is an auxiliary process of primary heat exchange. In addition, the gas-liquid mass transfer heat exchange of the second step can be completed between the flue gas and the washing liquid in the tower body cavity of the packed tower 4, and finally the complementary reinforcement of the heat exchange mechanism of the invention is realized, thereby achieving the purposes of removing dirt and cooling high-temperature flue gas.
In summary, the invention can realize the primary cooling of the high-temperature flue gas in the inlet flue 1, the heat exchanger 3 and the washing liquid area 41 through the integration of the heat exchanger 3 and the packed tower 4, and then finish the secondary cooling, deep desulfurization and dehydration/water supplementing in the washing area 42.
The above embodiments are illustrative of the present invention, and not limiting, and any simple modifications of the present invention fall within the scope of the present invention.
Claims (4)
1. Carbon entrapment pretreatment column suitable for high temperature flue gas, its characterized in that: comprises an inlet flue (1), a heat exchanger (3), a packed tower (4) and a packing (6), wherein the packed tower (4) is arranged up and down with the inlet flue (1) and is provided with a plurality of tower air inlets (45) and a channel air outlet (13) in a surrounding manner, the heat exchanger (3) comprises a shell (31), a water inlet main pipe (34), a heat exchange tube bundle (35) and a water outlet main pipe (37), the plurality of heat exchangers (3) are respectively wrapped outside the packed tower (4) in a surrounding manner, the inner wall of the shell (31) is respectively provided with a shell air outlet (33) and a shell air inlet (32) which can be correspondingly communicated with each tower air inlet (45) and flue outlet (13), the heat exchange tube bundle (35) is arranged in the inner cavity of the shell (31), one end of the water inlet main pipe (34) and one end of the water outlet main pipe (37) are respectively extended into the inner cavity of the shell (31) and are communicated with the heat exchange tube bundle (35), the outer wall of the packed tower (4) is respectively provided with a shell air inlet (44) and a channel air inlet (47) which is arranged in the tower (4) and the outer wall of the packed tower, the heat exchanger further comprises a skirt seat cylinder (2), the skirt seat cylinder (2) is positioned below the packing tower (4) and the top surface is provided with a plurality of notches (22) in a surrounding mode, the bottom end of each heat exchanger (3) is respectively arranged in each notch (22), the inlet flue (1) comprises an inlet section (11) and a transition area (12), the transition area (12) is funnel-shaped and is positioned in the inner cavity of the cylinder body of the skirt seat cylinder (2), the inlet section (11) is horizontally arranged, the outer wall of the channel at one end is provided with a channel air inlet, the other end firstly extends into the inner cavity of the cylinder body of the skirt seat cylinder (2) and then bends upwards and is connected with the transition area (12), each channel outlet (13) is positioned at the outer wall of the channel of the transition area (12), the packing tower (4) comprises a washing liquid area (41) and a washing area (42), the washing liquid area (42) and the washing liquid area (41) are arranged one above the other, the washing liquid area (41) is funnel-shaped and is sunk into the inner cavity of the transition area (12), the transition area (12) is provided with a plurality of heat exchanger baffles (36) which are arranged in a winding mode, each heat exchanger (36) is formed by a plurality of heat exchanger baffles (35) and each heat exchanger tube bundle (36) is arranged in a winding mode, and each tower air inlet (45) is also provided with a guide plate, and the guide plates are inclined gradually descending from the fixed end to the free end.
2. The carbon capture pretreatment tower for high temperature flue gas of claim 1, wherein: the washing device is characterized in that the tower water inlet (46) is positioned at the side part of the washing area (42), the tower air outlet (47) is positioned at the top of the washing area (42), the tower water outlet (44) is positioned at the side part of the washing liquid area (41), and a drain pipe (43) extending out of the inner cavity of the barrel body of the skirt seat barrel (2) is further arranged at the bottom of the washing liquid area (41).
3. The carbon capture pretreatment tower for high temperature flue gas according to claim 1 or 2, wherein: the gas distributor (5) is close to each heat exchanger (3) and enables flue gas to flow upwards through the gas distributor (5) and then along the inner cavity of the tower body, the liquid distributor (7) is close to the water inlet (46) of the tower body and enables washing liquid to flow downwards through the liquid distributor (7) and then along the inner cavity of the tower body.
4. A carbon capture pretreatment tower for high temperature flue gas according to claim 3, wherein: a demister (8) is arranged in the inner cavity of the tower body and between the liquid distributor (7) and the tower body air outlet (47).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310457271.9A CN116422124B (en) | 2023-04-26 | Carbon trapping pretreatment tower suitable for high-temperature flue gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310457271.9A CN116422124B (en) | 2023-04-26 | Carbon trapping pretreatment tower suitable for high-temperature flue gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN116422124A CN116422124A (en) | 2023-07-14 |
| CN116422124B true CN116422124B (en) | 2024-07-05 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105536394A (en) * | 2016-01-29 | 2016-05-04 | 北京神雾环境能源科技集团股份有限公司 | Spray tower, lignite drying flue gas treatment system provided with spray tower and method of lignite drying flue gas treatment system |
| CN217829407U (en) * | 2022-03-09 | 2022-11-18 | 中国矿业大学 | Flue gas CO 2 Gathering pretreatment tower |
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105536394A (en) * | 2016-01-29 | 2016-05-04 | 北京神雾环境能源科技集团股份有限公司 | Spray tower, lignite drying flue gas treatment system provided with spray tower and method of lignite drying flue gas treatment system |
| CN217829407U (en) * | 2022-03-09 | 2022-11-18 | 中国矿业大学 | Flue gas CO 2 Gathering pretreatment tower |
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