LU504005B1 - System and method for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and psa method - Google Patents
System and method for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and psa method Download PDFInfo
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- LU504005B1 LU504005B1 LU504005A LU504005A LU504005B1 LU 504005 B1 LU504005 B1 LU 504005B1 LU 504005 A LU504005 A LU 504005A LU 504005 A LU504005 A LU 504005A LU 504005 B1 LU504005 B1 LU 504005B1
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- carbon dioxide
- gas
- column
- liquid
- nitrogen gas
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 376
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 193
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 193
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 117
- 229910001873 dinitrogen Inorganic materials 0.000 title claims abstract description 98
- 238000000034 method Methods 0.000 title claims abstract description 89
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 239000003546 flue gas Substances 0.000 title claims abstract description 65
- 238000011084 recovery Methods 0.000 title claims abstract description 64
- 239000000126 substance Substances 0.000 title claims abstract description 49
- 230000001360 synchronised effect Effects 0.000 title claims abstract description 34
- 238000010521 absorption reaction Methods 0.000 claims abstract description 39
- 230000008929 regeneration Effects 0.000 claims abstract description 35
- 238000011069 regeneration method Methods 0.000 claims abstract description 35
- 238000000746 purification Methods 0.000 claims abstract description 21
- 238000007670 refining Methods 0.000 claims abstract description 19
- 239000007788 liquid Substances 0.000 claims description 137
- 239000007789 gas Substances 0.000 claims description 67
- 238000006477 desulfuration reaction Methods 0.000 claims description 61
- 230000023556 desulfurization Effects 0.000 claims description 58
- 238000003795 desorption Methods 0.000 claims description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 24
- 239000012530 fluid Substances 0.000 claims description 22
- 238000005406 washing Methods 0.000 claims description 18
- 238000001179 sorption measurement Methods 0.000 claims description 17
- 238000001035 drying Methods 0.000 claims description 16
- 238000003860 storage Methods 0.000 claims description 13
- 238000000926 separation method Methods 0.000 claims description 9
- 239000003463 adsorbent Substances 0.000 claims description 3
- 230000003009 desulfurizing effect Effects 0.000 claims description 3
- 239000002274 desiccant Substances 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 11
- 239000002904 solvent Substances 0.000 description 8
- 238000007906 compression Methods 0.000 description 6
- 230000006835 compression Effects 0.000 description 6
- 239000012528 membrane Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 101150107050 PSA2 gene Proteins 0.000 description 1
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 description 1
- 230000003749 cleanliness Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 238000011070 membrane recovery Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/343—Heat recovery
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/10—Nitrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Sustainable Development (AREA)
- Life Sciences & Earth Sciences (AREA)
- Treating Waste Gases (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
A system and method for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method. This system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method comprises a carbon dioxide chemical method recovery system, a carbon dioxide refining liquefaction system a nitrogen gas PSA concentration and purification system; the carbon dioxide chemical method recovery system comprises a carbon dioxide absorption column, a carbon dioxide regeneration column, a heat exchanger and a first congealer. This system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method has a good recovery effect of carbon dioxide and nitrogen gas, and can effectively save energy.
Description
BL-5662
LU504005
SYSTEM AND METHOD FOR SYNCHRONOUS RECOVERY OF CARBON
DIOXIDE AND NITROGEN GAS FROM FLUE GAS BY CHEMICAL METHOD AND
PSA METHOD
The present invention belongs to the technical field of recovery and utilization of boiler flue gas, and particularly relates to a system and method for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method.
Background Information
Greenhouse effects and extreme weather caused by carbon dioxide emission have seriously affected the global climate. Capture and reuse of carbon dioxide and nitrogen gas of coal-fired boiler flue gas is an important measure to achieve double-carbon target, which can not only further reduce carbon emission, but also reduce energy consumption.
Chinese patent application CN107899376A discloses a "combined capture and recovery device and method for carbon dioxide and nitrogen gas from flue gas", the device comprises a flue gas treatment system, a first CO, membrane separation unit, a second CO, membrane separation unit and an N, membrane separation unit. This device belongs to the membrane recovery mode, although it can capture carbon dioxide and nitrogen gas at the same time, the product purity is low, the membrane barrel has a high requirement for air source cleanliness, the equipment is easily blocked during use, the service life is short, and the membrane barrel has a high price, which is not suitable for industrial large-scale production.
Chinese patent application CN110498416A discloses a "system for synchronous recovery of carbon dioxide and nitrogen gas from boiler flue gas in coal-fired power plant”, comprising a flue gas pipeline pretreatment system, a PSAI 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. This system can capture carbon dioxide and nitrogen gas to the maximum extent, and the product purity is high, but there are some problems such as inflexible equipment operation, high energy consumption and low recovery rate of carbon dioxide. When the nitrogen gas production of the later stage is reduced or the capture 1s not performed, the pressure compression value of the earlier stage is too high and the power consumption is large. 1
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Accordingly, there is a need to provide an improved solution to the above-mentioned deficiencies of the prior art.
Therefore, an improved technical solution needs to be provided against the shortcomings of the above prior art.
It is an object of the present invention to provide a system and for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method, which has a good recovery effect of carbon dioxide and nitrogen gas, and can effectively save energy.
In order to achieve the above object, the present invention provides the following technical solutions: a system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method, comprising a carbon dioxide chemical method recovery system, a carbon dioxide refining liquefaction system and a nitrogen gas PSA concentration and purification system; the carbon dioxide chemical method recovery system comprises a carbon dioxide absorption column, a carbon dioxide regeneration column, a heat exchanger and a first congealer; the column top of the carbon dioxide absorption column is provided with an air outlet of vent gas, the interior of the carbon dioxide absorption column is provided with a first sprinkler, the column bottom of the carbon dioxide absorption column is provided with a liquid outlet of rich liquid, and the air outlet of the vent gas is connected to the air inlet of the nitrogen gas PSA concentration and purification system; the column top of the carbon dioxide regeneration column is provided with an air outlet of desorption gas, the interior of the carbon dioxide regeneration column is provided with a second sprinkler, the column bottom of the carbon dioxide regeneration column is provided with a liquid outlet of lean liquid, and the air outlet of the desorption gas is connected to the liquid inlet of the carbon dioxide refining liquefaction system; the heat exchanger has a high temperature fluid channel and a low temperature fluid channel, the liquid outlet of rich liquid is connected to the liquid inlet of the low temperature fluid channel, and the liquid outlet of the low temperature fluid channel 1s connected to the liquid inlet of the second sprinkler; the liquid outlet of the first congealer is connected to the liquid inlet of the first sprinkler, the liquid inlet of the first congealer is connected to the liquid outlet of the high temperature fluid channel, and the liquid inlet of the high temperature fluid channel is connected to the liquid outlet of lean liquid.
The present invention also provides a method for synchronous recovery of carbon dioxide and 2
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LU504005 nitrogen gas from flue gas, and the method for synchronous recovery of carbon dioxide and nitrogen gas from flue gas of the present invention adopts the following technical solution: the system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method as described above 1s used for synchronous recovery of carbon dioxide and nitrogen gas from flue gas.
The present invention can recover carbon dioxide and nitrogen gas to the maximum extent, and no three wastes are generated; chemical method (solvent absorption method) 1s used to recover carbon dioxide, and the gas flowed out from column top air outlet of carbon dioxide regeneration column has high purity of carbon dioxide (the volume concentration of carbon dioxide can reach 92-95%) and high recovery rate; the column top vent gas produced by chemical method (solvent absorption method) 1s nitrogen-rich gas and the content of nitrogen gas is about 90-92%, and the gas volume of nitrogen-rich gas is more than that of carbon dioxide separation in flue gas by PSA method.
The second compressor is comprised in the nitrogen gas PSA concentration and purification system of the present invention, and there is a secondary pressure-raising process, the compressor and compression pressure can be selected according to the user's needs, so as to achieve the purpose of energy saving.
Fig. 1 is a schematic diagram of the overall structure of a system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method;
Fig. 2 is a schematic diagram of the structure of the carbon dioxide chemical method recovery system.
Fig. 3 is a schematic diagram of the structure of the carbon dioxide refining liquefaction system.
Fig. 4 is a schematic diagram of the structure of the nitrogen gas PSA concentration and purification system.
In the drawings: 1-carbon dioxide chemical method recovery system; 2-carbon dioxide refining liquefaction system; 3-nitrogen gas PSA concentration and purification system; 101-draught fan; 102-desulfurization liquid pump; 103-desulfurization water washing column; 3
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LU504005 103a-third sprinkler; 104-first gas-liquid separator; 105-carbon dioxide absorption column; 105a-first sprinkler; 106-first congealer; 107-rich solution pump; 108-heat exchanger; 109-lean solution pump; 110-carbon dioxide regeneration column; 110a-second sprinkler; 111-second congealer; 112-second gas-liquid separator; 201-first buffer tank; 202-first compressor; 203-desulfurization bed; 204-drying bed, 205-third congealer; 206-liquefaction system; 207-rectifying column; 208-carbon dioxide storage tank; 301-demister; 302-fourth congealer; 303-third gas-liquid separator; 304-second compressor; 305-dryer; 306-second buffer tank; 307-nitrogen gas adsorption column; 308-nitrogen gas storage tank.
In view of the problems existing in the current capture and reuse of carbon dioxide and nitrogen gas in flue gas, the present invention provides a system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method, as shown in Figs 1-2, the system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method comprises a carbon dioxide chemical method recovery system 1, a carbon dioxide refining liquefaction system 2 and a nitrogen gas PSA concentration and purification system 3; the carbon dioxide chemical method recovery system 1 comprises a carbon dioxide absorption column 105, a carbon dioxide regeneration column 110, a heat exchanger 108 and a first congealer 106; the column top of the carbon dioxide absorption column 105 is provided with an air outlet of vent gas, the interior of the carbon dioxide absorption column 105 is provided with a first sprinkler 105a, the column bottom of the carbon dioxide absorption column 105 is provided with a liquid outlet of rich liquid, and the air outlet of the vent gas is connected to the air inlet of the nitrogen gas PSA concentration and purification system 3; the column top of the carbon dioxide regeneration column 110 is provided with an air outlet of desorption gas, the mterior of the carbon dioxide regeneration column 110 is provided with a second sprinkler 110a, the column bottom of the carbon dioxide regeneration column 110 is provided with a liquid outlet of lean liquid and a column bottom reboiler (not shown in the figure), and the air outlet of the desorption gas is connected to the liquid inlet of the carbon dioxide refining liquefaction system 2; the heat exchanger 108 has a high temperature fluid channel and a low temperature fluid channel, the liquid outlet of rich liquid is connected to the liquid inlet of the low temperature fluid channel, 4
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LU504005 and the liquid outlet of the low temperature fluid channel is connected to the liquid inlet of the second sprinkler 110a; the liquid outlet of the first congealer 106 is connected to the liquid inlet of the first sprinkler 105a, the liquid inlet of the first congealer 106 is connected to the liquid outlet of the high temperature fluid channel, and the liquid inlet of the high temperature fluid channel is connected to the liquid outlet of lean liquid.
When the flue gas is treated by the above-mentioned system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method, after the flue gas being entered into the carbon dioxide absorption column 105, the carbon dioxide in the flue gas can be absorbed by the chemical solvent in the carbon dioxide absorption column 105 to obtain the rich liquid rich in carbon dioxide, and the rich liquid is sent to carbon dioxide regeneration column 110 via the liquid outlet of rich liquid, the low temperature fluid channel of heat exchanger 108 and second sprinkler 110a, under the action of column bottom reboiler in the column bottom of the carbon dioxide regeneration column 110, the carbon dioxide in the rich liquid is desorbed at the high temperature, and the desorption gas, which exits from the air outlet of desorption gas of the column top of the carbon dioxide regeneration column 110, enters into the carbon dioxide refining liquefaction system 2 (the volume concentration of carbon dioxide in desorption gas can reach 92-95%), so as to further purify the carbon dioxide; the unabsorbed component (the vent gas) in the flue gas, which has flowed out from the air outlet of the vent gas of the column top of the carbon dioxide absorption column 105, enters into the nitrogen gas PSA concentration and purification system 3 (the volume concentration of the nitrogen gas in the vent gas can reach 90-92%, and the content of nitrogen gas in the vent gas is significantly higher than that in air, this vent gas is used to prepare the nitrogen gas can improve the production efficiency of the nitrogen gas preparation and save costs), and the nitrogen gas in the vent gas is concentrated and purified to prepare high-purity nitrogen gas; in the carbon dioxide regeneration column 110, the rich liquid is sprayed out from the second sprinkler 110a, and after desorbing the carbon dioxide by the action of the column bottom reboiler, a lean liquid (the content of the carbon dioxide is low) 1s formed, and the lean liquid, which has flowed out through the liquid outlet of lean liquid of the column bottom of the carbon dioxide regeneration column 110, successively passes through the high temperature fluid channel of the heat exchanger 108, the first congealer 106 and the first sprinkler 105a, enters the carbon dioxide absorption column 105, and is used
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LU504005 again for the absorption of the carbon dioxide in the flue gas; the heat exchange may be performed within 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 simultaneously through the heat exchanger 108 to facilitate the heat recovery from the lean liquid, reduce the workload on the first congealer 106 and save energy.
The system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method of the present invention has the following advantages over the prior art: (1) the present invention can recover carbon dioxide and nitrogen gas to the maximum extent, and no three wastes are generated; (2) chemical method (solvent absorption method) 1s used to recover carbon dioxide, and the gas flowed out from column top air outlet of carbon dioxide regeneration column has high purity of carbon dioxide and high recovery rate; (3) the column top vent gas produced by chemical method (solvent absorption method) 1s nitrogen-rich gas and the content of nitrogen gas is about 90-92%, and the gas volume of nitrogen-rich gas is more than that of carbon dioxide separation in flue gas by PSA method.
Preferably, the first sprinkler 105a is provided in the column top of the carbon dioxide absorption column 103, the second sprinkler 110a is provided in the column top of the carbon dioxide regeneration column 110, the rich solution pump 107 is provided on the connecting line of the liquid outlet of rich liquid and the heat exchanger 108, and lean solution pump 109 1s provided on the connecting line of the liquid outlet of lean liquid and the heat exchanger 108. The first sprinkler 105a is provided in the column top of the carbon dioxide absorption column 105, which contributes to improve the contact of the flue gas with the solvent that absorbs the carbon dioxide, and improves the efficiency of chemical method absorption of the carbon dioxide, so as to further contribute to improve the recovery efficiency of the carbon dioxide in the flue gas; the second sprinkler 110a is provided in the column top of the carbon dioxide regeneration column 110, which contributes to improve the efficiency of carbon dioxide desorption in the rich liquid; the arrangement of the rich solution pump 107 and the lean solution pump 109 allows easy transfer of the rich liquid and the lean liquid, so as to ensure proper operation of the carbon dioxide absorption column 105 and the carbon dioxide regeneration column 110, and improve production efficiency.
Preferably, the carbon dioxide chemical method recovery system 1 further comprises a flue gas 6
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LU504005 pipeline pretreatment system, and the flue gas pipeline pretreatment system comprises a draught fan 101, a desulfurization water washing column 103 and a first gas-liquid separator 104; the draught fan 101 is connected to the air inlet of the desulfurization water washing column 103 for transporting the flue gas to the air inlet of the desulfurization water washing column 103; the air outlet of the desulfurization water washing column 103 is connected to the air inlet of the first gas-liquid separator 104, and the desulfurization water washing column 103 is used for desulfurizing the flue gas; the air outlet of the first gas-liquid separator 104 is connected to the air inlet of the carbon dioxide absorption column 105, and the first gas-liquid separator 104 is used for performing gas-liquid separation on the gas treated by the desulfurization water washing column 103. The flue gas pipeline pretreatment system contributes to remove the sulfide from the flue gas in advance, and avoids the effect of sulfide on the subsequent recovery of the carbon dioxide.
Preferably, the column top of the desulfurization water washing column 103 is provided with a third sprinkler 103a, the column bottom of the desulfurization water washing column 103 is provided with a liquid outlet of desulfurization liquid, and a desulfurization liquid pump 102 is provided on a pipeline connecting the liquid outlet of the desulfurization liquid and the liquid inlet of the third sprinkler 103a. The arrangement of the third sprinkler 103a and the desulfurization liquid pump 102 contributes to the improvement of the desulfurization effect, and easily realize the reuse of the desulfurization liquid.
Preferably, the carbon dioxide chemical method recovery system 1 further comprises a second congealer 111 and a second gas-liquid separator 112, the air inlet of the second congealer 111 is connected to the air outlet of the carbon dioxide regeneration column 110, the air outlet of the second congealer 111 is connected to the air inlet of the second gas-liquid separator 112, and the air outlet of the second gas-liquid separator 112 is connected to the air inlet of the carbon dioxide refining liquefaction system 2. The arrangement of the second congealer 111 and the second gas-liquid separator 112 contributes to further remove water from the column top desorption gas of the carbon dioxide regeneration column 110 to improve the efficiency of carbon dioxide purification.
Preferably, as shown in Fig. 3, the carbon dioxide refining liquefaction system 2 comprises a secondary desulfurization system, a third congealer 205, a liquefaction system 206 and a 7
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LU504005 rectifying column 207, the air inlet of the secondary desulfurization system is connected to the air outlet of desorption gas (in the case where the carbon dioxide chemical method recovery system 1 comprises the second congealer 111 and the second gas-liquid separator 112, the air outlet of the secondary desulfurization system is connected to the air outlet of the second gas-liquid separator 112), the air outlet of the secondary desulfurization system is connected to the air inlet of the third congealer 205, the air outlet of the third congealer 205 is connected to the air inlet of the liquefaction system 206, and the liquid outlet of the liquefaction system 206 is connected to the rectifying column 207. By further purification of the carbon dioxide in desorption gas using the secondary desulfurization system, third congealer 205, liquefaction system 206 and rectifying column 207 in the carbon dioxide refining liquefaction system 2, it is possible to obtain more pure and satisfactory of finished product carbon dioxide (volume concentration: > 99.9%).
Preferably, the carbon dioxide refining liquefaction system 2 further comprises a carbon dioxide storage tank 208 being connected to the rectifying column 207. By providing the carbon dioxide storage tank 208, the purified high-purity carbon dioxide (volume concentration: > 99.9%) can be stored in the carbon dioxide storage tank 208 for use.
Preferably, the secondary desulfurization system comprises a first buffer tank 201, a first compressor 202, a desulfurization bed 203 and a drying bed 204, the air inlet of the first buffer tank 201 is connected to the air outlet of the desorption gas (in the case where the carbon dioxide chemical method recovery system 1 comprises the second congealer 111 and the second gas-liquid separator 112, the air outlet of the first buffer tank 201 is connected to the air outlet of the second gas-liquid separator 112), the air outlet of the first buffer tank 201 is connected to the air inlet of the first compressor 202, the air outlet of the first compressor 202 1s connected to the air inlet of the desulfurization bed 203, the air outlet of the desulfurization bed 203 1s connected to the air inlet of the drying bed 204, and the air outlet of the drying bed 204 is connected to the air inlet of the third congealer 205. The purity of carbon dioxide is further improved by further desulfurizing and drying the desorption gas from the carbon dioxide regeneration column 110 using the desulfurization bed 203 and the drying bed 204. After the carbon dioxide desorption gas is compressed by the first compressor 202 (e.g. desorption gas can be compressed to 2.5MPa) to facilitate desulfurization and drying of the desorption gas via desulfurization bed 203 and drying bed 204. 8
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LU504005
Preferably, the desulfurization bed 203 comprises two parallel desulfurization columns, and the desulfurization column 1s provided with a desulfurization adsorbent therein; the drying bed 204 comprises two parallel dry columns, and the dry column is provided with a desiccant therein.
Preferably, as shown in Fig. 4, the nitrogen gas PSA concentration and purification system 3 comprises a demister 301, a fourth congealer 302, a third gas-liquid separator 303, a second compressor 304, a dryer 305, a second buffer tank 306 and a nitrogen gas adsorption column 307 (the nitrogen gas adsorption column 307 is filled with an adsorbent for purifying nitrogen, and has a high recovery rate for the vent gas having the complicated composition), the air inlet of the demister 301 is connected to the air outlet of the vent gas of the carbon dioxide absorption column 105, the air outlet of the demister 301 1s connected to the air inlet of the fourth congealer 302, the air outlet of the fourth congealer 302 1s connected to the air inlet of the third gas-liquid separator 303, the air outlet of the third gas-liquid separator 303 1s connected to the air inlet of the second compressor 304, the air outlet of the second compressor 304 is connected to the air inlet of the dryer 305, the air outlet of the dryer 305 is connected to the air inlet of the second buffer tank 306, and the air outlet of the second buffer tank 306 is connected to the nitrogen gas adsorption column 307. The desorption gas obtained after the treatment by the carbon dioxide regeneration column 110 successively enters the demister 301 and the third gas-liquid separator 303, and after removing the large particles of free water, it enters the second compressor 304; the air outlet of the second compressor 304 is connected to the air inlet of the dryer 305, and after drying by dryer 305, the gas enters nitrogen gas adsorption column 307 after passing through second buffer tank 306, and after pressure swing adsorption, the product nitrogen gas can be obtained (the volume concentration can reach 99-99.999%). The nitrogen gas PSA concentration and purification system comprises the second compressor 304, will have a secondary pressurization process, which can select compressor and compression pressure according to the user's needs, so as to achieve the purpose of energy saving.
Preferably, the nitrogen gas PSA concentration and purification system 3 further comprises a nitrogen gas storage tank 308 being connected to column top air outlet of the nitrogen gas adsorption column 307 to facilitate storage of the recovered nitrogen gas.
Preferably, the nitrogen gas adsorption column 307 is provided with at least two; two or more of the nitrogen gas adsorption columns 307 are arranged in parallel. 9
BL-5662
LU504005
Preferably, two nitrogen gas adsorption columns 307 are used in parallel.
The method for synchronous recovery of carbon dioxide and nitrogen gas from flue gas of the present invention, wherein the above-mentioned the system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method is used for synchronous recovery of carbon dioxide and nitrogen gas from flue gas.
Preferably, the method for synchronous recovery of carbon dioxide and nitrogen gas from flue gas of the present invention is specifically exemplified as follows:
The present invention is used for recovery of carbon dioxide and nitrogen gas from flue gas of a coal power plant. The carbon dioxide gas is used to increase the income of smart agriculture, and the nitrogen gas is used to replace and purge the chemical plant of the factory. The flue gas composition is shown in Table 1 as below:
Table 1 dioxide oxide monoxide dioxide detected _ Detection limit | 2mg/m’ | 2mg/m? | 20mgm’ | 003% | — | —
The required flue gas is extracted from the flue gas blow-down stack after desulfurization and denitration, and enters desulfurization water washing column 103 for desulfurization and dust removal, then enters the first gas-liquid separator 104 for gas-liquid separation, and then enters the carbon dioxide absorption column 105, the carbon dioxide in the flue gas is absorbed by the solvent, and the solvent forms a rich liquid, the unabsorbed nitrogen-rich gas (nitrogen gas content: 90-92%) flows out through the air outlet of the vent gas of the column top of the carbon dioxide absorption column 105.
The rich liquid is subjected to heat exchange with the lean liquid (the liquid where the rich liquid have been desorbed and removed from the carbon dioxide in the carbon dioxide regeneration column 110) via the rich solution pump 107 in the heat exchanger 108, and then enters the carbon dioxide regeneration column 110 (enters the second sprinkler 110a inside the carbon dioxide regeneration column 110), under the heating action of the bottom reboiler, the carbon dioxide is desorbed, the crude carbon dioxide gas (desorption gas) with a carbon dioxide
BL-5662
LU504005 content of 95% flows out from the gas outlet of desorption gas at the column top, after further removing water via the second congealer 111 and second gas-liquid separator 112, 1t enters the carbon dioxide refining liquefaction system 2.
After desorbing the carbon dioxide from the carbon dioxide regeneration column 110, the rich liquid forms a lean liquid at the column bottom, it is subjected to heat exchange with the rich solution in the heat exchanger 108 via the lean solution pump 109, and then enters the first congealer 106 (optionally a water cooler) for further cooling, and then enters the carbon dioxide absorption column 105 (entering the first sprinkler 105a inside the carbon dioxide absorption column 105) to complete one working cycle.
The desorption gas (containing 95% of crude carbon dioxide gas), obtained after cooling and removing water by the second congealer 111 and the second gas-liquid separator 112, enters the first compressor 202 after through the first buffer tank 201, increases the pressure to 2.5 MPa, then enters the desulfurization bed 203 and the drying bed 204 for desulfurization and impurity removal, enters the third congealer 205 for temperature reduction, and enters the liquefaction system 206, and after temperature reduction to -18°C to obtain carbon dioxide in a liquid state, after the liquid carbon dioxide enters the rectifying column 207 for refining and purification, the food-grade carbon dioxide with a purity of up to 99.9% can be obtained at the column bottom, and enters the carbon dioxide storage tank 208 for storage. Further, the vent gas of column top of the rectifying column can also be used as a regeneration gas source for the desulfurization bed 203 and the drying bed 204, so as to save product gas and reduce energy consumption.
The vent gas produced by the column top of the carbon dioxide absorption column 105 (a nitrogen-rich gas, with a nitrogen content of 90-92%) enters demister 301, fourth congealer 302 and third gas-liquid separator 303, after removing free water, it enters second compressor 304, increases the pressure to 0.8-1.0 MPa, and after being dried by a dryer 305, enters a second buffer tank 306, and then enters a nitrogen gas adsorption column 307 for pressure swing adsorption to obtain finished product nitrogen gas, and the finished product nitrogen gas enters nitrogen gas storage tank 308, with the nitrogen purity varying from 99%-99.999%.
In this example, the carbon-nitrogen separation in flue gas adopts a chemical absorption mode, and the recovery effect of carbon dioxide is good, and carbon dioxide with a content of about 95% can be obtained, the recovery rate of carbon dioxide is high; the nitrogen gas content in the vent 11
BL-5662
LU504005 gas (the vent gas of the carbon dioxide absorption column 105) is up to 92%, much higher than 78% in air, which is a high-quality nitrogen gas raw material. With regard to the nitrogen gas PSA concentration and purification system 3, nitrogen-containing 92% nitrogen-rich gas is used as the raw material gas, the secondary compression mode 1s adopted, the pressure is increased from 3
KPa to 0.8-1.0 MPa, the compression energy is fully recovered, and more than 20% energy is saved compared with preparing nitrogen gas from air. 12
Claims (10)
1. À system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method, characterized in that, comprising a carbon dioxide chemical method recovery system, a carbon dioxide refining liquefaction system and a nitrogen gas PSA concentration and purification system; the carbon dioxide chemical method recovery system comprises a carbon dioxide absorption column, a carbon dioxide regeneration column, a heat exchanger and a first congealer; the column top of the carbon dioxide absorption column is provided with an air outlet of vent gas, the interior of the carbon dioxide absorption column is provided with a first sprinkler, the column bottom of the carbon dioxide absorption column is provided with a liquid outlet of rich liquid, and the air outlet of the vent gas is connected to the air inlet of the nitrogen gas PSA concentration and purification system; the column top of the carbon dioxide regeneration column is provided with an air outlet of desorption gas, the interior of the carbon dioxide regeneration column is provided with a second sprinkler, the column bottom of the carbon dioxide regeneration column is provided with a liquid outlet of lean liquid, and the air outlet of the desorption gas is connected to the liquid inlet of the carbon dioxide refining liquefaction system; the heat exchanger has a high temperature fluid channel and a low temperature fluid channel, the liquid outlet of rich liquid is connected to the liquid inlet of the low temperature fluid channel, and the liquid outlet of the low temperature fluid channel is connected to the liquid inlet of the second sprinkler; the liquid outlet of the first congealer is connected to the liquid inlet of the first sprinkler, the liquid inlet of the first congealer is connected to the liquid outlet of the high temperature fluid channel, and the liquid inlet of the high temperature fluid channel is connected to the liquid outlet of lean liquid.
2. The system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method according to claim 1, characterized in that, the first sprinkler is provided in the column top of the carbon dioxide absorption column, the second sprinkler is provided in the column top of the carbon dioxide regeneration column, the rich solution pump is 13
BL-5662 LU504005 provided on the connecting line of the liquid outlet of rich liquid and the heat exchanger, and lean solution pump is provided on the connecting line of the liquid outlet of lean liquid and the heat exchanger.
3. The system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method according to claim 1, characterized in that, the carbon dioxide chemical method recovery system further comprises a flue gas pipeline pretreatment system, and the flue gas pipeline pretreatment system comprises a draught fan, a desulfurization water washing column and a first gas-liquid separator; the draught fan is connected to the air inlet of the desulfurization water washing column for transporting the flue gas to the air inlet of the desulfurization water washing column; the air outlet of the desulfurization water washing column is connected to the air inlet of the first gas-liquid separator, and the desulfurization water washing column is used for desulfurizing the flue gas; the air outlet of the first gas-liquid separator is connected to the air inlet of the carbon dioxide absorption column, and the first gas-liquid separator is used for performing gas-liquid separation on the gas treated by the desulfurization water washing column; the column top of the desulfurization water washing column is provided with a third sprinkler, the column bottom of the desulfurization water washing column is provided with a liquid outlet of desulfurization liquid, and a desulfurization liquid pump is provided on a pipeline connecting the liquid outlet of the desulfurization liquid and the liquid inlet of the third sprinkler.
4. The system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method according to claim 1, characterized in that, the carbon dioxide chemical method recovery system further comprises a second congealer and a second gas-liquid separator, the air inlet of the second congealer is connected to the air outlet of the desorption gas of the carbon dioxide regeneration column, the air outlet of the second congealer is connected to the air inlet of the second gas-liquid separator, and the air outlet of the second gas-liquid separator 1s connected to the air inlet of the carbon dioxide refining liquefaction system. 14
BL-5662 LU504005
5. The system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method according to claim 1, characterized in that, the carbon dioxide refining liquefaction system comprises a secondary desulfurization system, a third congealer, a liquefaction system and a rectifying column, the air inlet of the secondary desulfurization system is connected to the air outlet of desorption gas, the air outlet of the secondary desulfurization system is connected to the air inlet of the third congealer, the air outlet of the third congealer is connected to the air inlet of the liquefaction system, and the liquid outlet of the liquefaction system is connected to the rectifying column; the carbon dioxide refining liquefaction system further comprises a carbon dioxide storage tank being connected to the rectifying column.
6. The system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method according to claim 5, characterized in that, the secondary desulfurization system comprises a first buffer tank, a first compressor, a desulfurization bed and a drying bed, the air inlet of the first buffer tank is connected to the air outlet of the desorption gas, the air outlet of the first buffer tank is connected to the air inlet of the first compressor, the air outlet of the first compressor is connected to the air inlet of the desulfurization bed, the air outlet of the desulfurization bed is connected to the air inlet of the drying bed, and the air outlet of the drying bed is connected to the air inlet of the third congealer; the desulfurization bed comprises two parallel desulfurization columns, and the desulfurization column is provided with a desulfurization adsorbent therein; the drying bed comprises two parallel dry columns, and the dry column is provided with a desiccant therein.
7. The system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method according to claim 1, characterized in that, the nitrogen gas PSA concentration and purification system comprises a demister, a fourth congealer, a third gas-liquid separator, a second compressor, a dryer, a second buffer tank and a nitrogen gas adsorption column, the air inlet of the demister is connected to the air outlet of the vent gas of the carbon dioxide absorption column, the air outlet of the demister is connected to the air inlet of the fourth congealer, the air outlet of the fourth congealer is connected to the air inlet of the third
BL-5662 LU504005 gas-liquid separator, the air outlet of the third gas-liquid separator is connected to the air inlet of the second compressor, the air outlet of the second compressor is connected to the air inlet of the dryer, the air outlet of the dryer is connected to the air inlet of the second buffer tank, and the air outlet of the second buffer tank is connected to the nitrogen gas adsorption column.
8. The system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method according to claim 1, characterized in that, the nitrogen gas PSA concentration and purification system further comprises a nitrogen gas storage tank being connected to column top air outlet of the nitrogen gas adsorption column.
9. The system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method according to any one of claim 7 or 8, characterized in that, the nitrogen gas adsorption column is provided with at least two; two or more of the nitrogen gas adsorption columns are arranged in parallel.
10. A method for synchronous recovery of carbon dioxide and nitrogen gas from flue gas, characterized in that, the system for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and PSA method according to any one of claim 1-9 is used for synchronous recovery of carbon dioxide and nitrogen gas from flue gas. 16
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111302095.9A CN113975950B (en) | 2021-11-04 | 2021-11-04 | System and method for synchronously recycling carbon dioxide and nitrogen in flue gas by chemical method and PSA method |
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| LU504005A1 LU504005A1 (en) | 2023-05-05 |
| LU504005B1 true LU504005B1 (en) | 2023-08-21 |
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| LU504005A LU504005B1 (en) | 2021-11-04 | 2022-11-02 | System and method for synchronous recovery of carbon dioxide and nitrogen gas from flue gas by chemical method and psa method |
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| Country | Link |
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| CN (1) | CN113975950B (en) |
| LU (1) | LU504005B1 (en) |
| SE (1) | SE2350521A1 (en) |
| WO (1) | WO2023061507A1 (en) |
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| CN113998677B (en) * | 2021-10-19 | 2023-10-24 | 碳和科技(北京)有限公司 | CO recovery from chemical process 2 System and method for preparing nitrogen from waste gas of (a) a reactor |
| 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 |
| CN114713008A (en) * | 2022-03-08 | 2022-07-08 | 山东保蓝环保工程有限公司 | Tail gas treatment device suitable for domestic waste schizolysis produces |
| CN114917723A (en) * | 2022-03-16 | 2022-08-19 | 四川天采科技有限责任公司 | CO recovery from flue gas 2 Full temperature range pressure swing adsorption process |
| CN114852973A (en) * | 2022-06-02 | 2022-08-05 | 西安本清化学技术有限公司 | Method and system for synchronously preparing nitrogen and carbon dioxide from oil field boiler flue gas |
| CN115159524B (en) * | 2022-07-06 | 2023-04-07 | 重庆朗福环保科技有限公司 | Carbon dioxide recovery and liquefaction process and system thereof |
| CN115350574B (en) * | 2022-08-03 | 2023-08-04 | 大连理工大学 | Gas heat function recovery and carbon capture comprehensive utilization method and device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2008123337A1 (en) * | 2007-03-29 | 2008-10-16 | Nippon Oil Corporation | Method of hydrogen production and carbon dioxide recovery and apparatus therefor |
| CN103143249B (en) * | 2013-03-06 | 2015-02-18 | 上海锅炉厂有限公司 | Method and device for capturing carbon dioxide in flue gas of power station boiler |
| JP6575050B2 (en) * | 2014-08-12 | 2019-09-18 | 株式会社Ihi | Carbon dioxide recovery method and recovery apparatus |
| CN110498416A (en) * | 2019-08-14 | 2019-11-26 | 东营市港城热力有限公司 | A kind of system that coal-fired plant boiler flue gas synchronizes recycling carbon dioxide and nitrogen |
| CN113310063A (en) * | 2021-02-10 | 2021-08-27 | 上海凯盛节能工程技术有限公司 | Device and method for capturing and purifying carbon dioxide in glass kiln flue gas |
| 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 |
| CN216457971U (en) * | 2021-11-04 | 2022-05-10 | 大连理工大学 | System for synchronously recycling carbon dioxide and nitrogen in flue gas by chemical method and PSA (pressure swing adsorption) method |
-
2021
- 2021-11-04 CN CN202111302095.9A patent/CN113975950B/en active Active
-
2022
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- 2022-11-02 LU LU504005A patent/LU504005B1/en active IP Right Grant
- 2022-11-02 WO PCT/CN2022/129313 patent/WO2023061507A1/en unknown
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| Publication number | Publication date |
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| CN113975950B (en) | 2024-07-05 |
| WO2023061507A1 (en) | 2023-04-20 |
| LU504005A1 (en) | 2023-05-05 |
| CN113975950A (en) | 2022-01-28 |
| SE2350521A1 (en) | 2023-04-28 |
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