CN216457971U - System for synchronously recycling carbon dioxide and nitrogen in flue gas by chemical method and PSA (pressure swing adsorption) method - Google Patents
System for synchronously recycling carbon dioxide and nitrogen in flue gas by chemical method and PSA (pressure swing adsorption) method Download PDFInfo
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 222
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 205
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 203
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 239000003546 flue gas Substances 0.000 title claims abstract description 60
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Abstract
The utility model belongs to the technical field of recycling of boiler flue gas, and particularly relates to a system for synchronously recycling carbon dioxide and nitrogen in flue gas by a chemical method and a PSA (pressure swing adsorption) method. The system for synchronously recovering carbon dioxide and nitrogen in flue gas by a chemical method and a PSA method comprises a carbon dioxide chemical method recovery system, a carbon dioxide refining and liquefying system and a nitrogen PSA concentration and purification system; the carbon dioxide chemical method recovery system comprises a carbon dioxide absorption tower, a carbon dioxide regeneration tower, a heat exchanger and a first cooler. The system for synchronously recovering the carbon dioxide and the nitrogen in the flue gas by the chemical method and the PSA method has good recovery effect on the carbon dioxide and the nitrogen and can effectively save energy.
Description
Technical Field
The utility model belongs to the technical field of recycling of boiler flue gas, and particularly relates to a system for synchronously recycling carbon dioxide and nitrogen in flue gas by a chemical method and a PSA (pressure swing adsorption) method.
Background
The global climate has been severely affected by the greenhouse effect and extreme weather caused by carbon dioxide emissions. In this year, energy sources in many countries are in urgent need. The reduction of emission or recovery of carbon dioxide and the reduction of production energy consumption are very slow. The carbon dioxide is mainly obtained from the combustion of petrochemical fuels (coal, petroleum and natural gas), the production and processing processes of coal and petroleum and the daily production and life of human beings. The capture and reuse of carbon dioxide and nitrogen in the flue gas of the coal-fired boiler is an important measure for realizing the double-carbon target, thereby not only further reducing the carbon emission, but also reducing the energy consumption.
Chinese patent application CN107899376A discloses a combined capturing and recovering device and method for carbon dioxide and nitrogen in flue gas, the device comprises a flue gas treatment system and a first CO2Membrane separation unit, second CO2Membrane separation unit and N2A membrane separation unit. The device belongs to the membrane recovery mode, though can catch carbon dioxide and nitrogen gas simultaneously, but the product purity is low, and the membrane bucket is very high to the air supply cleanliness factor requirement, produces the jam easily in the equipment use, and the life-span is short, and the membrane bucket price is higher, is not suitable for the large-scale production of industrialization.
Chinese patent application CN110498416A discloses a system for synchronously recovering carbon dioxide and nitrogen from boiler flue gas of a coal-fired power plant, which comprises a flue gas pretreatment system, a PSA1 system, a PSA2 system, a carbon dioxide compression and purification system, a carbon dioxide rectification and storage system and a PSA high-purity nitrogen preparation system. The system can trap carbon dioxide and nitrogen to the maximum extent, and has high product purity, but has the problems of inflexible equipment operation, high energy consumption and low carbon dioxide recovery rate. When the nitrogen yield of the later stage is reduced or the capture is not performed, the pressure compression value of the former stage is too high, and the power consumption is large.
Therefore, there is a need to provide an improved solution to the above-mentioned deficiencies of the prior art.
Disclosure of Invention
The utility model aims to provide a system for synchronously recovering carbon dioxide and nitrogen in flue gas by a chemical method and a PSA method, which has good recovery effect on carbon dioxide and nitrogen and can effectively save energy.
In order to achieve the above purpose, the utility model provides the following technical scheme: a system for synchronously recovering carbon dioxide and nitrogen in flue gas by a chemical method and a PSA method comprises a carbon dioxide chemical method recovery system, a carbon dioxide refining and liquefying system and a nitrogen PSA concentration and purification system; the carbon dioxide chemical method recovery system comprises a carbon dioxide absorption tower, a carbon dioxide regeneration tower, a heat exchanger and a first cooler;
a vent gas outlet is formed in the tower top of the carbon dioxide absorption tower, a first spraying device is arranged inside the carbon dioxide absorption tower, a rich liquid outlet is formed in the tower bottom of the carbon dioxide absorption tower, and the vent gas outlet is connected with a gas inlet of the nitrogen PSA concentration and purification system; a desorption gas outlet is formed in the tower top of the carbon dioxide regeneration tower, a second spraying device is arranged inside the carbon dioxide regeneration tower, a lean solution outlet is formed in the tower bottom of the carbon dioxide regeneration tower, and the desorption gas outlet is connected with a liquid inlet of the carbon dioxide refining and liquefying system; the heat exchanger is provided with a high-temperature fluid channel and a low-temperature fluid channel, the rich liquid outlet is connected with the liquid inlet of the low-temperature fluid channel, and the liquid outlet of the low-temperature fluid channel is connected with the liquid inlet of the second spraying device; the liquid outlet of the first cooler is connected with the liquid inlet of the first spraying device, the liquid inlet of the first cooler is connected with the liquid outlet of the high-temperature fluid channel, and the liquid inlet of the high-temperature fluid channel is connected with the lean liquid outlet.
Preferably, the first spraying device is arranged at the top of the carbon dioxide absorption tower, the second spraying device is arranged at the top of the carbon dioxide regeneration tower, a rich liquid pump is arranged on a connecting pipeline between the rich liquid outlet and the heat exchanger, and a lean liquid pump is arranged on a connecting pipeline between the lean liquid outlet and the heat exchanger.
Preferably, the carbon dioxide chemical method recovery system further comprises a flue gas pretreatment system, wherein the flue gas pretreatment system comprises an induced draft fan, a desulfurization water washing tower and a first gas-liquid separator; the induced draft fan is connected with the air inlet of the desulfurization water scrubber and is used for conveying the flue gas to the air inlet of the desulfurization water scrubber; the gas outlet of the desulfurization water washing tower is connected with the gas inlet of the first gas-liquid separator, and the desulfurization water washing tower is used for performing desulfurization treatment on the flue gas; and the gas outlet of the first gas-liquid separator is connected with the gas inlet of the carbon dioxide absorption tower, and the first gas-liquid separator is used for carrying out gas-liquid separation on the gas treated by the desulfurization water washing tower.
Preferably, the top of the desulfurization water washing tower is provided with a third spray device, the bottom of the desulfurization water washing tower is provided with a desulfurization liquid outlet, and a pipeline communicating the desulfurization liquid outlet with a liquid inlet of the third spray device is provided with a desulfurization liquid pump.
Preferably, the carbon dioxide chemical method recovery system further comprises a second cooler and a second gas-liquid separator, wherein a gas inlet of the second cooler is connected with a desorption gas outlet of the carbon dioxide regeneration tower, a gas outlet of the second cooler is connected with a gas inlet of the second gas-liquid separator, and a gas outlet of the second gas-liquid separator is connected with a gas inlet of the carbon dioxide refining and liquefying system.
Preferably, the carbon dioxide refining and liquefying system comprises a secondary desulfurization system, a third cooler, a liquefying system and a rectifying tower, wherein an air inlet of the secondary desulfurization system is connected with an air outlet of desorption gas, an air outlet of the secondary desulfurization system is connected with an air inlet of the third cooler, an air outlet of the third cooler is connected with an air inlet of the liquefying system, and a liquid outlet of the liquefying system is connected with the rectifying tower.
Preferably, the carbon dioxide refining and liquefying system further comprises a carbon dioxide storage tank, and the carbon dioxide storage tank is connected with the rectifying tower.
Preferably, the secondary desulfurization system includes first buffer tank, first compressor, desulfurization bed and drying bed, the air inlet of first buffer tank with desorption gas outlet links to each other, the gas outlet of first buffer tank with the air inlet of first compressor links to each other, the gas outlet of first compressor with the air inlet of desulfurization bed links to each other, the gas outlet of desulfurization bed with the air inlet of drying bed links to each other, the gas outlet of drying bed with the air inlet of third cooler links to each other.
Preferably, the desulfurization bed comprises two desulfurization towers connected in parallel, and a desulfurization adsorbent is arranged in each desulfurization tower; the drying bed comprises two drying towers which are connected in parallel, and drying agents are arranged in the drying towers.
Preferably, the nitrogen PSA concentration and purification system comprises a demister, a fourth cooler, a third gas-liquid separator, a second compressor, a dryer, a second buffer tank and a nitrogen adsorption tower, wherein the gas inlet of the demister is connected with the vent gas outlet of the carbon dioxide absorption tower, the gas outlet of the demister is connected with the gas inlet of the fourth cooler, the gas outlet of the fourth cooler is connected with the gas inlet of the third gas-liquid separator, the gas outlet of the third gas-liquid separator is connected with the gas inlet of the second compressor, the gas outlet of the second compressor is connected with the gas inlet of the dryer, the gas outlet of the dryer is connected with the gas inlet of the second buffer tank, and the gas outlet of the second buffer tank is connected with the nitrogen adsorption tower.
Preferably, the nitrogen PSA concentration and purification system further comprises a nitrogen storage tank, and the nitrogen storage tank is connected with a gas outlet at the top of the nitrogen adsorption tower.
Preferably, the nitrogen adsorption towers are at least two.
Preferably, two or more nitrogen adsorption columns are arranged in parallel.
Has the advantages that: the utility model can recover carbon dioxide and nitrogen to the maximum extent without generating three wastes; the carbon dioxide is recovered by a chemical method (a solvent absorption method), the purity of the carbon dioxide in the gas flowing out of a gas outlet at the top of the carbon dioxide regeneration tower is high (the volume concentration of the carbon dioxide can reach 92-95 percent), and the recovery rate is high; the tower top vent gas generated by the chemical method (solvent absorption method) is nitrogen-rich gas, the content of the nitrogen is about 90-92%, and the nitrogen-rich gas has larger gas quantity than that when the PSA method is adopted to realize the separation of the carbon dioxide in the flue gas.
The nitrogen PSA concentration and purification system comprises the second compressor, so that a secondary pressure increasing process is realized, and the compressor and the compression pressure can be selected according to the requirements of users, thereby achieving the purpose of energy conservation.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the utility model and, together with the description, serve to explain the utility model and not to limit the utility model. Wherein:
FIG. 1 is a schematic diagram of the overall structure of a system for synchronously recovering nitrogen and carbon dioxide in flue gas by a chemical method and a PSA method provided by an embodiment of the utility model;
FIG. 2 is a schematic structural diagram of a carbon dioxide chemical recovery system according to an embodiment of the present invention;
FIG. 3 is a schematic structural diagram of a carbon dioxide refining and liquefying system provided by an embodiment of the utility model;
FIG. 4 is a schematic diagram of a nitrogen PSA concentration and purification system according to an embodiment of the present invention;
reference numerals:
1-a carbon dioxide chemical recovery system; 2-a carbon dioxide refining liquefaction system; 3-nitrogen PSA concentration purification system;
101-an induced draft fan; 102-a desulfurization liquid pump; 103-a desulfurization water washing tower; 103 a-a third spray device; 104-a first gas-liquid separator; 105-a carbon dioxide absorber; 105 a-a first spray device; 106-a first cooler; 107-rich liquid pump; 108-a heat exchanger; 109-barren liquor pump; 110-a carbon dioxide regenerator; 110 a-a second spray device; 111-a second cooler; 112-a second gas-liquid separator;
201-a first buffer tank; 202-a first compressor; 203-a desulfurization bed; 204-dry bed, 205-third cooler; 206-a liquefaction system; 207-rectifying column; 208-a carbon dioxide storage tank;
301-a demister; 302-a fourth cooler; 303-a third gas-liquid separator; 304-a second compressor; 305-a dryer; 306-a second buffer tank; 307-nitrogen adsorption tower; 308-nitrogen storage tank.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments that can be derived by one of ordinary skill in the art from the embodiments given herein are intended to be within the scope of the present invention.
The present invention will be described in detail with reference to examples. It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
The utility model aims at the problems existing in the capture and reuse of carbon dioxide and nitrogen in flue gas at present, and provides a system for synchronously recovering carbon dioxide and nitrogen in flue gas by a chemical method and a PSA method, as shown in figure 1-2, the system for synchronously recovering carbon dioxide and nitrogen in flue gas by the chemical method and the PSA method comprises a carbon dioxide chemical method recovery system 1, a carbon dioxide refining and liquefying system 2 and a nitrogen PSA concentration and purification system 3; the carbon dioxide chemical recovery system 1 includes a carbon dioxide absorption tower 105, a carbon dioxide regeneration tower 110, a heat exchanger 108, and a first cooler 106; an air vent gas outlet is formed in the top of the carbon dioxide absorption tower 105, a first spraying device 105a is arranged inside the carbon dioxide absorption tower 105, a rich liquid outlet is formed in the bottom of the carbon dioxide absorption tower 105, and the air vent gas outlet is connected with a gas inlet of the nitrogen PSA concentration and purification system 3; a desorption gas outlet is arranged at the top of the carbon dioxide regeneration tower 110, a second spraying device 110a is arranged inside the carbon dioxide regeneration tower 110, a lean solution outlet and a tower bottom reboiler (not shown in the figure) are arranged at the bottom of the carbon dioxide regeneration tower 110, and the desorption gas outlet is connected with a liquid inlet of the carbon dioxide refining and liquefying system 2; the heat exchanger 108 is provided with a high-temperature fluid channel and a low-temperature fluid channel, a rich liquid outlet is connected with a liquid inlet of the low-temperature fluid channel, and a liquid outlet of the low-temperature fluid channel is connected with a liquid inlet of the second spraying device 110 a; the liquid outlet of the first cooler 106 is connected with the liquid inlet of the first spraying device 105a, the liquid inlet of the first cooler 106 is connected with the liquid outlet of the high-temperature fluid channel, and the liquid inlet of the high-temperature fluid channel is connected with the lean liquid outlet.
When the flue gas is treated by the system for synchronously recovering carbon dioxide and nitrogen in the flue gas by adopting the chemical method and the PSA method, after the flue gas enters the carbon dioxide absorption tower 105, the carbon dioxide in the flue gas can be absorbed by a chemical solvent in the carbon dioxide absorption tower 105 to obtain a rich solution rich in carbon dioxide, the rich solution is conveyed to the carbon dioxide regeneration tower 110 through a rich solution outlet, a low-temperature fluid channel of the heat exchanger 108 and a second spraying device 110a, the carbon dioxide in the rich solution is desorbed at a high temperature under the action of a tower bottom reboiler at the tower bottom of the carbon dioxide regeneration tower 110, the desorbed gas comes out from a desorbed gas outlet at the tower top of the carbon dioxide regeneration tower 110 and enters the carbon dioxide refining and liquefying system 2 (the volume concentration of the carbon dioxide in the desorbed gas can reach 92-95 percent), and the carbon dioxide is further purified; the unabsorbed components (vent gas) in the flue gas flow out of a vent gas outlet at the top of the carbon dioxide absorption tower 105 and then enter a nitrogen PSA concentration and purification system 3 (the volume concentration of the nitrogen in the vent gas can reach 90-92%, and the content of the nitrogen in the vent gas is significantly higher compared with air, and the production efficiency of nitrogen preparation is improved and the cost is saved by adopting the vent gas to prepare the nitrogen), and the nitrogen in the vent gas is concentrated and purified to prepare high-purity nitrogen; in the carbon dioxide regeneration tower 110, the rich solution is sprayed out from the second spraying device 110a, and carbon dioxide is desorbed under the action of a reboiler at the tower bottom to form a lean solution (with low content of carbon dioxide), and the lean solution flows out from a lean solution outlet at the tower bottom of the carbon dioxide regeneration tower 110, sequentially passes through a high-temperature fluid channel of the heat exchanger 108, the first cooler 106 and the first spraying device 105a, enters the carbon dioxide absorption tower 105, and is used for absorbing carbon dioxide in the flue gas again; the heat exchange can be performed in the heat exchanger 108 by passing the rich liquid in the low-temperature fluid channel and the lean liquid in the high-temperature fluid channel through the heat exchanger 108 at the same time, so as to help recover the heat in the lean liquid, reduce the workload of the first cooler 106, and save energy.
Compared with the prior art, the system for synchronously recovering the carbon dioxide and the nitrogen in the flue gas by the chemical method and the PSA method has the following advantages: (1) the utility model can recover carbon dioxide and nitrogen to the maximum extent without generating three wastes; (2) the carbon dioxide is recovered by a chemical method (a solvent absorption method), and the purity and the recovery rate of the carbon dioxide in the gas flowing out of the gas outlet at the top of the carbon dioxide regeneration tower are high; (3) the tower top vent gas generated by the chemical method (solvent absorption method) is nitrogen-rich gas, the content of the nitrogen is about 90-92%, and the nitrogen-rich gas has larger gas quantity than that when the PSA method is adopted to realize the separation of the carbon dioxide in the flue gas.
In a preferred embodiment of the present invention, the first spraying device 105a is disposed on the top of the carbon dioxide absorption tower 105, the second spraying device 110a is disposed on the top of the carbon dioxide regeneration tower 110, a rich liquid pump 107 is disposed on a connection pipeline between the rich liquid outlet and the heat exchanger 108, and a lean liquid pump 109 is disposed on a connection pipeline between the lean liquid outlet and the heat exchanger 108. The arrangement of the first spraying device 105a on the top of the carbon dioxide absorption tower 105 contributes to improving the contact between the flue gas and the solvent for absorbing carbon dioxide, improving the efficiency of absorbing carbon dioxide by a chemical method, and further contributing to improving the recovery efficiency of carbon dioxide in the flue gas; the second spraying device 110a is arranged at the top of the carbon dioxide regeneration tower 110, which is beneficial to improving the efficiency of carbon dioxide desorption in the rich liquid; the rich liquid pump 107 and the lean liquid pump 109 are arranged, so that the transfer of rich liquid and lean liquid can be conveniently realized, the normal operation of the carbon dioxide absorption tower 105 and the carbon dioxide regeneration tower 110 is ensured, and the production efficiency is improved.
In a preferred embodiment of the present invention, the carbon dioxide chemical recovery system 1 further comprises a flue gas pretreatment system, wherein the flue gas pretreatment system comprises an induced draft fan 101, a desulfurization water scrubber 103 and a first gas-liquid separator 104; the induced draft fan 101 is connected with the air inlet of the desulfurization water scrubber 103 and is used for conveying the flue gas to the air inlet of the desulfurization water scrubber 103; the gas outlet of the desulfurization water scrubber 103 is connected with the gas inlet of the first gas-liquid separator 104, and the desulfurization water scrubber 103 is used for performing desulfurization treatment on the flue gas; the gas outlet of the first gas-liquid separator 104 is connected to the gas inlet of the carbon dioxide absorption tower 105, and the first gas-liquid separator 104 is used for gas-liquid separation of the gas treated by the desulfurization water washing tower 103. The flue gas pretreatment system is helpful for removing the sulfide in the flue gas in advance, and the influence of the sulfide on the subsequent recovery of carbon dioxide is avoided.
In the preferred embodiment of the present invention, the top of the desulfurization water washing tower 103 is provided with a third spraying device 103a, the bottom of the desulfurization water washing tower 103 is provided with a desulfurization liquid outlet, and a pipeline communicating the desulfurization liquid outlet with the liquid inlet of the third spraying device 103a is provided with a desulfurization liquid pump 102. The third spraying device 103a and the desulphurization liquid pump 102 are arranged to improve the desulphurization effect and conveniently realize the reuse of the desulphurization liquid.
In a preferred embodiment of the present invention, the carbon dioxide chemical recovery system 1 further comprises a second cooler 111 and a second gas-liquid separator 112, wherein a gas inlet of the second cooler 111 is connected to a gas outlet of the carbon dioxide regeneration tower 110, a gas outlet of the second cooler 111 is connected to a gas inlet of the second gas-liquid separator 112, and a gas outlet of the second gas-liquid separator 112 is connected to a gas inlet of the carbon dioxide refining and liquefying system 2. The arrangement of the second cooler 111 and the second gas-liquid separator 112 helps to further remove water from the desorbed gas at the top of the carbon dioxide regeneration tower 110, thereby improving the efficiency of carbon dioxide purification.
In a preferred embodiment of the present invention, as shown in fig. 3, the carbon dioxide refining and liquefying system 2 includes a secondary desulfurization system, a third cooler 205, a liquefying system 206 and a rectifying tower 207, wherein an air inlet of the secondary desulfurization system is connected to an outlet of the desorption gas (in the case where the carbon dioxide chemical recovery system 1 includes the second cooler 111 and the second gas-liquid separator 112, an air inlet of the secondary desulfurization system is connected to an outlet of the second gas-liquid separator 112), an outlet of the secondary desulfurization system is connected to an air inlet of the third cooler 205, an air outlet of the third cooler 205 is connected to an air inlet of the liquefying system 206, and an outlet of the liquefying system 206 is connected to the rectifying tower 207. The carbon dioxide in the desorbed gas is further purified by adopting a secondary desulfurization system, a third cooler 205, a liquefaction system 206 and a rectifying tower 207 in the carbon dioxide refining and liquefying system 2, so that the finished carbon dioxide (the volume concentration is more than or equal to 99.9%) with higher purity and meeting the requirement can be obtained.
In the preferred embodiment of the present invention, the carbon dioxide refining liquefaction system 2 further comprises a carbon dioxide storage tank 208, and the carbon dioxide storage tank 208 is connected to the rectifying tower 207. The carbon dioxide storage tank 208 is arranged to store the refined high-purity carbon dioxide (the volume concentration is more than or equal to 99.9%) in the carbon dioxide storage tank 208, so that the carbon dioxide purification device is convenient to use.
In a preferred embodiment of the present invention, the secondary desulfurization system includes a first buffer tank 201, a first compressor 202, a desulfurization bed 203, and a desiccant bed 204, wherein an air inlet of the first buffer tank 201 is connected to a desorption gas outlet (in the case where the carbon dioxide chemical recovery system 1 includes the second cooler 111 and the second gas-liquid separator 112, an air inlet of the first buffer tank 201 is connected to an air outlet of the second gas-liquid separator 112), an air outlet of the first buffer tank 201 is connected to an air inlet of the first compressor 202, an air outlet of the first compressor 202 is connected to an air inlet of the desulfurization bed 203, an air outlet of the desulfurization bed 203 is connected to an air inlet of the desiccant bed 204, and an air outlet of the desiccant bed 204 is connected to an air inlet of the third cooler 205. The purity of carbon dioxide is further improved by further desulfurization and drying treatment of the desorbed gas from the carbon dioxide regeneration tower 110 using the desulfurization bed 203 and the drying bed 204. The first compressor 202 compresses the carbon dioxide desorption gas (e.g., the desorption gas may be compressed to 2.5MPa), thereby facilitating desulfurization and drying of the desorption gas through the desulfurization bed 203 and the drying bed 204.
In the preferred embodiment of the present invention, the desulfurization bed 203 comprises two desulfurization towers connected in parallel, and a desulfurization adsorbent is arranged in each desulfurization tower; the desiccant bed 204 includes two parallel desiccant towers with desiccant disposed therein.
In a preferred embodiment of the present invention, as shown in fig. 4, the nitrogen PSA concentration and purification system 3 includes a demister 301, a fourth cooler 302, a third gas-liquid separator 303, a second compressor 304, a dryer 305, a second buffer tank 306, and a nitrogen adsorption tower 307 (the nitrogen adsorption tower 307 is filled with an adsorbent for purifying nitrogen and has a high recovery rate for a vent gas having a complicated composition), an air inlet of the demister 301 is connected to an air outlet of the vent gas of the carbon dioxide absorption tower 105, an air outlet of the demister 301 is connected to an air inlet of the fourth cooler 302, an air outlet of the fourth cooler 302 is connected to an air inlet of the third gas-liquid separator 303, an air outlet of the third gas-liquid separator 303 is connected to an air inlet of the second compressor 304, an air outlet of the second compressor 304 is connected to an air inlet of the dryer 305, an air outlet of the dryer 305 is connected to an air inlet of the second buffer tank 306, the outlet of the second buffer tank 306 is connected to a nitrogen adsorption tower 307. The desorption gas obtained after being treated by the carbon dioxide regeneration tower 110 sequentially enters a demister 301 and a third gas-liquid separator 303, large-particle free water is removed, the desorption gas enters a second compressor 304, an air outlet of the second compressor 304 is connected with an air inlet of a dryer 305, the desorption gas is dried by the dryer 305, the desorption gas enters a nitrogen adsorption tower 307 after passing through a second buffer tank 306, and the product nitrogen (the volume concentration can reach 99-99.999%) is obtained after pressure swing adsorption. The nitrogen PSA concentration and purification system comprises a second compressor 304, and has a secondary pressure increasing process, and the compressor and the compression pressure can be selected according to the needs of users, so that the aim of saving energy is fulfilled.
In the preferred embodiment of the present invention, the nitrogen PSA concentration and purification system 3 further includes a nitrogen storage tank 308, and the nitrogen storage tank 308 is connected to the outlet of the nitrogen adsorption tower 307 at the top of the tower, so as to facilitate storage of the recovered nitrogen.
In a preferred embodiment of the present invention, at least two nitrogen adsorption towers 307 are provided, and two or more nitrogen adsorption towers 307 are provided in parallel.
In the preferred embodiment of the present invention, two nitrogen adsorption towers 307 are arranged in parallel.
In the preferred embodiment of the present invention, the method for synchronously recovering carbon dioxide and nitrogen in flue gas of the present invention is specifically exemplified as follows:
the utility model is used for recovering carbon dioxide and nitrogen in flue gas of a certain coal power plant. Carbon dioxide gas is used for increasing the income of intelligent agriculture, and nitrogen gas is used for replacement and purging in the chemical workshop of the factory. The smoke composition is shown in table 1 below:
TABLE 1
| Composition (I) | Sulfur dioxide | Nitrogen oxides | Carbon monoxide | Carbon dioxide | Oxygen gas | Water (W) |
| Measured value | 20mg/m3 | 31mg/m3 | Not detected out | 13％ | 6.20％ | 12.50％ |
| Detection limit | 2mg/m3 | 2mg/m3 | 20mg/m3 | 0.03％ | —— | —— |
The required flue gas is led out from a flue gas emission chimney after desulfurization and denitrification, enters a desulfurization washing tower 103 for desulfurization and dust removal, enters a first gas-liquid separator 104 for gas-liquid separation, then enters a carbon dioxide absorption tower 105, carbon dioxide in the flue gas is absorbed by a solvent, the solvent forms a rich solution, and nitrogen-rich gas (the content of nitrogen is 90-92%) which is not absorbed flows out through an air discharge gas outlet at the top of the carbon dioxide absorption tower 105.
The rich solution and the lean solution (the solution obtained by desorbing the rich solution in the carbon dioxide regeneration tower 110 to remove the carbon dioxide) are subjected to heat exchange in the heat exchanger 108 through the rich solution pump 107, and then enter the carbon dioxide regeneration tower 110 (enter the second spraying device 110a inside the carbon dioxide regeneration tower 110), carbon dioxide is desorbed under the heating action of the reboiler at the bottom of the tower, and the crude carbon dioxide gas (desorbed gas) with the carbon dioxide content of 95% flows out from the desorbed gas outlet at the top of the tower, and further undergoes water removal through the second cooler 111 and the second gas-liquid separator 112, and then enters the carbon dioxide refining liquefaction system 2.
After the rich solution desorbs carbon dioxide in the carbon dioxide regeneration tower 110, a lean solution is formed at the bottom of the tower, and after the lean solution exchanges heat with the rich solution in the heat exchanger 108 through the lean solution pump 109, the lean solution enters the first cooler 106 (which may be a water cooler) for further cooling, and then enters the carbon dioxide absorption tower 105 (which enters the first spraying device 105a inside the carbon dioxide absorption tower 105), so that a working cycle is completed.
Desorption gas (containing 95 percent of crude carbon dioxide gas) obtained after cooling and dewatering through the second cooler 111 and the second gas-liquid separator 112 enters the first compressor 202 after passing through the first buffer tank 201, the pressure is increased to 2.5MPa, and then enters the desulfurization bed 203 and the drying bed 204 for desulfurization and impurity removal, the temperature of the desorption gas enters the third cooler 205 for cooling, the desorption gas enters the liquefaction system 206 for cooling to-18 ℃ to obtain liquid carbon dioxide, the liquid carbon dioxide enters the rectifying tower 207 for refining and purification, food-grade carbon dioxide with the purity of 99.9 percent can be obtained at the bottom of the tower, and the food-grade carbon dioxide enters the carbon dioxide storage tank 208 for storage. Furthermore, the vent gas at the top of the rectifying tower can also be used as a regeneration gas source of the desulfurizing bed 203 and the drying bed 204, so that the product gas is saved, and the energy consumption is reduced.
The method comprises the steps of enabling vent gas (nitrogen-rich gas and nitrogen content of 90-92%) produced at the top of a carbon dioxide absorption tower 105 to enter a demister 301, a fourth cooler 302 and a third gas-liquid separator 303, removing free water, enabling the vent gas to enter a second compressor 304, increasing pressure to 0.8-1.0 MPa, enabling the vent gas to enter a second buffer tank 306 after being dried by a dryer 305, enabling the vent gas to enter a nitrogen adsorption tower 307 for pressure swing adsorption to obtain finished nitrogen, enabling the finished nitrogen to enter a nitrogen storage tank 308, and enabling the nitrogen purity to be different from 99% -99.999%.
In the embodiment, the carbon and nitrogen separation in the flue gas adopts a chemical absorption mode, the carbon dioxide recovery effect is good, the carbon dioxide with the content of about 95 percent can be prepared, and the recovery rate of the carbon dioxide is high; and the nitrogen content in the vent gas (the vent gas of the carbon dioxide absorption tower 105) can reach 92 percent and is far higher than 78 percent of the nitrogen content in the air, so the nitrogen-containing gas is a high-quality nitrogen raw material. The nitrogen PSA concentration and purification system 3 utilizes nitrogen-rich gas containing 92% of nitrogen as raw material gas, adopts a secondary compression mode, improves the pressure from 3KPa to 0.8-1.0 MPa, fully recovers compression energy, and saves energy by more than 20% compared with the nitrogen prepared from air.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A system for synchronously recovering carbon dioxide and nitrogen in flue gas by a chemical method and a PSA method is characterized by comprising a carbon dioxide chemical method recovery system, a carbon dioxide refining and liquefying system and a nitrogen PSA concentration and purification system;
the carbon dioxide chemical method recovery system comprises a carbon dioxide absorption tower, a carbon dioxide regeneration tower, a heat exchanger and a first cooler;
a vent gas outlet is formed in the tower top of the carbon dioxide absorption tower, a first spraying device is arranged inside the carbon dioxide absorption tower, a rich liquid outlet is formed in the tower bottom of the carbon dioxide absorption tower, and the vent gas outlet is connected with a gas inlet of the nitrogen PSA concentration and purification system;
a desorption gas outlet is formed in the tower top of the carbon dioxide regeneration tower, a second spraying device is arranged inside the carbon dioxide regeneration tower, a lean solution outlet is formed in the tower bottom of the carbon dioxide regeneration tower, and the desorption gas outlet is connected with a liquid inlet of the carbon dioxide refining and liquefying system;
the heat exchanger is provided with a high-temperature fluid channel and a low-temperature fluid channel, the rich liquid outlet is connected with the liquid inlet of the low-temperature fluid channel, and the liquid outlet of the low-temperature fluid channel is connected with the liquid inlet of the second spraying device;
the liquid outlet of the first cooler is connected with the liquid inlet of the first spraying device, the liquid inlet of the first cooler is connected with the liquid outlet of the high-temperature fluid channel, and the liquid inlet of the high-temperature fluid channel is connected with the lean liquid outlet.
2. The system for synchronously recycling carbon dioxide and nitrogen in flue gas by a chemical method and a PSA method according to claim 1, wherein the first spraying device is arranged at the top of the carbon dioxide absorption tower, the second spraying device is arranged at the top of the carbon dioxide regeneration tower, a rich liquid pump is arranged on a connecting pipeline between the rich liquid outlet and the heat exchanger, and a lean liquid pump is arranged on a connecting pipeline between the lean liquid outlet and the heat exchanger.
3. The system for synchronously recovering carbon dioxide and nitrogen from flue gas by a chemical method and a PSA method according to claim 1, wherein the carbon dioxide chemical method recovery system further comprises a flue gas pretreatment system, and the flue gas pretreatment system comprises an induced draft fan, a desulfurization water washing tower and a first gas-liquid separator;
the induced draft fan is connected with the air inlet of the desulfurization water scrubber and is used for conveying the flue gas to the air inlet of the desulfurization water scrubber;
the gas outlet of the desulfurization water washing tower is connected with the gas inlet of the first gas-liquid separator, and the desulfurization water washing tower is used for performing desulfurization treatment on the flue gas;
and the gas outlet of the first gas-liquid separator is connected with the gas inlet of the carbon dioxide absorption tower, and the first gas-liquid separator is used for carrying out gas-liquid separation on the gas treated by the desulfurization water washing tower.
4. The system for synchronously recycling carbon dioxide and nitrogen in flue gas by a chemical method and a PSA method according to claim 3, wherein a third spraying device is arranged at the top of the desulfurization water washing tower, a desulfurization liquid outlet is arranged at the bottom of the desulfurization water washing tower, and a desulfurization liquid pump is arranged on a pipeline which communicates the desulfurization liquid outlet with a liquid inlet of the third spraying device.
5. The system for synchronously recovering carbon dioxide and nitrogen from flue gas by the chemical method and the PSA method according to claim 1, wherein the system for chemically recovering carbon dioxide by the chemical method further comprises a second cooler and a second gas-liquid separator, wherein a gas inlet of the second cooler is connected with a desorption gas outlet of the carbon dioxide regeneration tower, a gas outlet of the second cooler is connected with a gas inlet of the second gas-liquid separator, and a gas outlet of the second gas-liquid separator is connected with a gas inlet of the carbon dioxide refining and liquefying system.
6. The system for synchronously recovering carbon dioxide and nitrogen from flue gas by a chemical method and a PSA method according to claim 1, wherein the carbon dioxide refining and liquefying system comprises a secondary desulfurization system, a third cooler, a liquefying system and a rectifying tower, wherein a gas inlet of the secondary desulfurization system is connected with a desorption gas outlet, a gas outlet of the secondary desulfurization system is connected with a gas inlet of the third cooler, a gas outlet of the third cooler is connected with a gas inlet of the liquefying system, and a liquid outlet of the liquefying system is connected with the rectifying tower;
the carbon dioxide refining and liquefying system also comprises a carbon dioxide storage tank, and the carbon dioxide storage tank is connected with the rectifying tower.
7. The system for synchronously recovering carbon dioxide and nitrogen from flue gas by a chemical process and a PSA process according to claim 6, wherein the secondary desulfurization system comprises a first buffer tank, a first compressor, a desulfurization bed and a drying bed, wherein a gas inlet of the first buffer tank is connected with a gas outlet of the desorption gas, a gas outlet of the first buffer tank is connected with a gas inlet of the first compressor, a gas outlet of the first compressor is connected with a gas inlet of the desulfurization bed, a gas outlet of the desulfurization bed is connected with a gas inlet of the drying bed, and a gas outlet of the drying bed is connected with a gas inlet of the third cooler;
the desulfurization bed comprises two desulfurization towers connected in parallel, and a desulfurization adsorbent is arranged in each desulfurization tower; the drying bed comprises two drying towers which are connected in parallel, and drying agents are arranged in the drying towers.
8. The system for synchronously recovering carbon dioxide and nitrogen in flue gas by a chemical method and a PSA method according to claim 1, it is characterized in that the nitrogen PSA concentration and purification system comprises a demister, a fourth cooler, a third gas-liquid separator, a second compressor, a dryer, a second buffer tank and a nitrogen adsorption tower, the air inlet of the demister is connected with the vent air outlet of the carbon dioxide absorption tower, the air outlet of the demister is connected with the air inlet of the fourth cooler, the air outlet of the fourth cooler is connected with the air inlet of the third gas-liquid separator, the air outlet of the third gas-liquid separator is connected with the air inlet of the second compressor, the gas outlet of the second compressor is connected with the gas inlet of the dryer, the gas outlet of the dryer is connected with the gas inlet of the second buffer tank, and the gas outlet of the second buffer tank is connected with the nitrogen adsorption tower.
9. The system for synchronously recovering carbon dioxide and nitrogen from flue gas by using the chemical method and the PSA method as claimed in claim 8, wherein the nitrogen PSA concentration and purification system further comprises a nitrogen storage tank, and the nitrogen storage tank is connected with the top gas outlet of the nitrogen adsorption tower.
10. The system for synchronously recovering carbon dioxide and nitrogen from flue gas by using the chemical method and the PSA method as claimed in claim 8 or 9, wherein the number of the nitrogen adsorption towers is at least two;
and more than two nitrogen adsorption towers are arranged in parallel.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113975950A (en) * | 2021-11-04 | 2022-01-28 | 大连理工大学 | System and method for synchronously recovering carbon dioxide and nitrogen in flue gas by chemical method and PSA (pressure swing adsorption) method |
| CN113975950B (en) * | 2021-11-04 | 2024-07-05 | 大连理工大学 | System and method for synchronously recycling carbon dioxide and nitrogen in flue gas by chemical method and PSA method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113975950A (en) * | 2021-11-04 | 2022-01-28 | 大连理工大学 | System and method for synchronously recovering carbon dioxide and nitrogen in flue gas by chemical method and PSA (pressure swing adsorption) method |
| WO2023061507A1 (en) * | 2021-11-04 | 2023-04-20 | 碳和科技(北京)有限公司 | System and method for synchronously recovering carbon dioxide and nitrogen in flue gas by means of chemical method and psa method |
| CN113975950B (en) * | 2021-11-04 | 2024-07-05 | 大连理工大学 | System and method for synchronously recycling carbon dioxide and nitrogen in flue gas by chemical method and PSA method |
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