CN116550090A - Carbon trapping system for low-carbon-dioxide-concentration flue gas and application method thereof - Google Patents
Carbon trapping system for low-carbon-dioxide-concentration flue gas and application method thereof Download PDFInfo
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- CN116550090A CN116550090A CN202310648742.4A CN202310648742A CN116550090A CN 116550090 A CN116550090 A CN 116550090A CN 202310648742 A CN202310648742 A CN 202310648742A CN 116550090 A CN116550090 A CN 116550090A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 77
- 239000003546 flue gas Substances 0.000 title claims abstract description 77
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 24
- 238000000034 method Methods 0.000 title claims abstract description 20
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 390
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 212
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 212
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical group [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 150
- 239000007789 gas Substances 0.000 claims abstract description 146
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 86
- 238000003860 storage Methods 0.000 claims abstract description 54
- 239000012535 impurity Substances 0.000 claims abstract description 32
- 239000003507 refrigerant Substances 0.000 claims abstract description 28
- 239000007787 solid Substances 0.000 claims abstract description 22
- 238000001816 cooling Methods 0.000 claims abstract description 15
- 238000001179 sorption measurement Methods 0.000 claims abstract description 12
- 238000001035 drying Methods 0.000 claims abstract description 7
- 230000005611 electricity Effects 0.000 claims abstract description 4
- 239000002808 molecular sieve Substances 0.000 claims description 94
- 230000001105 regulatory effect Effects 0.000 claims description 37
- 230000018044 dehydration Effects 0.000 claims description 33
- 238000006297 dehydration reaction Methods 0.000 claims description 33
- 239000000779 smoke Substances 0.000 claims description 15
- 230000008929 regeneration Effects 0.000 claims description 8
- 238000011069 regeneration method Methods 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 5
- 238000005265 energy consumption Methods 0.000 abstract description 10
- 238000000926 separation method Methods 0.000 abstract description 3
- 239000003344 environmental pollutant Substances 0.000 abstract description 2
- 231100000719 pollutant Toxicity 0.000 abstract description 2
- 238000000746 purification Methods 0.000 abstract 1
- 238000004146 energy storage Methods 0.000 description 7
- 238000011084 recovery Methods 0.000 description 5
- 238000010248 power generation Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000004083 survival effect Effects 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
- B01D53/02—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
-
- 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
- B01D53/26—Drying gases or vapours
- B01D53/261—Drying gases or vapours by adsorption
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
-
- 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
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Treating Waste Gases (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
A carbon trapping system of low carbon dioxide concentration flue gas and a use method thereof belong to the field of flue gas pollutant purification treatment. The method solves the problems that when the existing flue gas carbon dioxide is trapped, the purity of carbon dioxide products is low, the trapping energy consumption is high, and gaseous carbon dioxide is difficult to transport. The carbon trapping system comprises a flue gas-cold water heat exchanger, a dehydrated molecular sieve group, a carbon dioxide molecular sieve group, a compressor, a refrigerator, a desublimation separator, a compressed gas storage tank, an expansion unit, a carbon dioxide storage tank, a refrigerant heat exchanger, a gas-water separator and an ice storage tank; the method comprises the following steps: 1. flue gas drying treatment and carbon dioxide adsorption enrichment treatment; 2. the mixed gas of carbon dioxide in the carbon dioxide molecular sieve group is subjected to cooling treatment and separation, the separated gas is pressurized and cooled and then enters a desublimation separator, solid carbon dioxide separated by the desublimation separator enters a carbon dioxide storage tank, and high-pressure impurity gas separated by the desublimation separator is heated and then enters a compressed gas storage tank; 3. and doing work to generate electricity.
Description
Technical Field
The invention belongs to the field of purifying treatment of smoke pollutants.
Background
After the world enters an industrialized age, the large amount of fossil fuels is used, so that the emission of carbon dioxide is rapidly increased, various climate changes which are unfavorable for human survival are generated due to the increase of greenhouse gases in the world, and in order to avoid the occurrence of disastrous climate, carbon dioxide emission reduction has become one of the most important environmental problems in the world. The carbon dioxide direct capturing technology is the most widely used carbon capturing technology in industry at present, and can realize large-scale application of industrial grade.
The trapping after combustion is widely used in the existing carbon trapping technology, but the flue gas discharged from industrial production contains moisture and has lower carbon dioxide content, the trapping energy consumption by a chemical absorption method and a physical separation method is larger, and in addition, the moisture also affects the purity of a carbon dioxide product, so that the carbon dioxide product is difficult to use; conventional physical adsorption processes result in gaseous carbon dioxide products that are not readily transportable and utilizable.
Disclosure of Invention
The invention aims to solve the problems that the purity of carbon dioxide products is low, the trapping energy consumption is high and gaseous carbon dioxide is difficult to transport when the carbon dioxide in the existing flue gas is trapped, and further provides a carbon trapping system for flue gas with low carbon dioxide concentration and a use method thereof.
A carbon trapping system of low carbon dioxide concentration flue gas comprises a flue gas-cold water heat exchanger, a dehydrated molecular sieve group, a carbon dioxide molecular sieve group, a compressor, a refrigerator, a desublimation separator, a compressed gas storage tank, an expansion unit, a carbon dioxide storage tank, a refrigerant heat exchanger, a gas-water separator and an ice storage tank;
the dehydration molecular sieve group is formed by parallel connection of a first dehydration molecular sieve device and a second dehydration molecular sieve device;
the carbon dioxide molecular sieve group is formed by parallelly connecting a first carbon dioxide molecular sieve device and a second carbon dioxide molecular sieve device;
the expansion unit is formed by serially connecting a first expansion machine, a second expansion machine and a third expansion machine;
the flue gas inlet pipe is communicated with the inlet of the flue gas-cold water heat exchanger, the outlet of the flue gas-cold water heat exchanger is respectively communicated with the inlets of the first dehydrated molecular sieve device and the second dehydrated molecular sieve device through pipelines, and the dry gas outlets of the first dehydrated molecular sieve device and the second dehydrated molecular sieve device are communicated with the inlet of the first gas heat exchanger through pipelines;
the outlet of the first gas heat exchanger is respectively communicated with the inlets of the first carbon dioxide molecular sieve device and the second carbon dioxide molecular sieve device through pipelines, the carbon dioxide mixed gas outlets of the first carbon dioxide molecular sieve device and the second carbon dioxide molecular sieve device are sequentially communicated with the refrigerant heat exchanger, the gas-water separator, the compressor, the second gas heat exchanger, the refrigerator and the desublimation separator through pipelines, the solid outlet of the gas-water separator is communicated with the ice storage tank through pipelines, the solid carbon dioxide outlet of the desublimation separator is communicated with the carbon dioxide storage tank through pipelines, and the high-pressure impurity gas outlet of the desublimation separator is sequentially communicated with the second gas heat exchanger, the first gas heat exchanger and the compressed gas storage tank through pipelines;
the outlet of the compressed gas storage tank is sequentially communicated with a first hot water heat exchanger, a first expander, a second hot water heat exchanger, a second expander, a third hot water heat exchanger and a third expander through pipelines, and the outlet of the third expander is communicated with a gas discharge pipeline.
The application method of the carbon trapping system for the low-carbon-dioxide-concentration flue gas comprises the following steps:
1. inputting smoke, starting a smoke-cold water heat exchanger, adjusting the outlet temperature of the smoke-cold water heat exchanger to be 25-45 ℃, and enabling the smoke to enter the smoke-cold water heat exchanger for cooling treatment; the operation temperature of the dehydration molecular sieve group is regulated to be 20-40 ℃, and the cooled flue gas enters the dehydration molecular sieve group for drying treatment; adjusting the running temperature of the carbon dioxide molecular sieve group to be 20-30 ℃, cooling the dried flue gas in a first gas heat exchanger, and then, introducing the cooled flue gas into the carbon dioxide molecular sieve group to perform carbon dioxide adsorption enrichment, and discharging impurity gas;
2. after the carbon dioxide molecular sieve group adsorption enrichment process is finished, regulating the operating temperature of the carbon dioxide molecular sieve group to 100-200 ℃, starting a refrigerant heat exchanger, regulating the outlet temperature of the refrigerant heat exchanger to minus 2-10 ℃, starting a compressor, regulating the outlet pressure of the compressor to 0.1-3.1 MPa, starting the refrigerator, regulating the temperature of the refrigerator to minus 100-140 ℃, enabling carbon dioxide mixed gas in the carbon dioxide molecular sieve group to enter the refrigerant heat exchanger for cooling treatment, enabling cooled carbon dioxide mixed gas to enter a gas-water separator, enabling separated water to enter an ice storage tank in a solid form, enabling separated gas to enter a compressor, pressurizing through the compressor, enabling the cooled gas to enter a desublimation separator, enabling solid carbon dioxide separated by the desublimation separator to enter a carbon dioxide storage tank, enabling high-pressure impurity gas separated by the desublimation separator to sequentially pass through a second gas heat exchanger and a first gas heat exchanger for heating, and then entering a compressed gas storage tank;
3. the separated high-pressure impurity gas is discharged from the compressed gas storage tank and sequentially passes through the first expander, the second expander and the third expander to perform work and generate power.
The beneficial effects of the invention are as follows:
the flue gas carbon dioxide trapping system provided by the invention can be used for physically separating carbon dioxide without pollution and with low energy consumption aiming at low-concentration (volume percentage is not more than 10%) carbon dioxide flue gas discharged by industry, can remove water in the flue gas, remove more than 95% of water in the flue gas, and improve the purity of carbon dioxide products to 99% -99.9%, and meanwhile, the invention can obviously reduce the carbon dioxide trapping energy consumption.
The flue gas carbon dioxide trapping system provided by the invention can be used for drying flue gas and recovering moisture in the flue gas; the concentration of carbon dioxide in the flue gas can be improved through the molecular sieve, and finally, the carbon dioxide is separated in a solid form, and the carbon dioxide trapping rate can be more than 90%; the high-pressure impurity gas can complete the energy storage function of the compressed gas, and can generate electricity through the expansion unit, so that the comprehensive treatment of the flue gas is realized.
In summary, the system has the following advantages compared with other systems:
1. can remove more than 95% of water in the flue gas.
2. The recovery rate of carbon dioxide is more than 90%, and the purity of the carbon dioxide product is improved to 99% -99.9%.
3. The energy collection device is low in energy consumption and has an energy storage function, and a 100MW unit uses the system to treat smoke, so that the net power consumption is about 20 MW.
Drawings
FIG. 1 is a schematic diagram of a carbon capture system for low carbon dioxide concentration flue gas according to the present invention.
Detailed Description
The first embodiment is as follows: referring to fig. 1, the embodiment is specifically described as a carbon capturing system for low carbon dioxide concentration flue gas, which includes a flue gas-cold water heat exchanger 1, a dehydrated molecular sieve group, a carbon dioxide molecular sieve group, a compressor 6, a refrigerator 7, a desublimation separator 8, a compressed gas storage tank 9, an expansion unit, a carbon dioxide storage tank 12, a refrigerant heat exchanger 13, a gas-water separator 14 and an ice storage tank 15;
the dehydration molecular sieve group is formed by arranging a first dehydration molecular sieve device 4-1 and a second dehydration molecular sieve device 4-2 in parallel;
the carbon dioxide molecular sieve group is formed by arranging a first carbon dioxide molecular sieve device 5-1 and a second carbon dioxide molecular sieve device 5-2 in parallel;
the expansion unit is formed by serially connecting a first expansion machine 10-1, a second expansion machine 10-2 and a third expansion machine 10-3;
the flue gas inlet pipe is communicated with the inlet of the flue gas-cold water heat exchanger 1, the outlet of the flue gas-cold water heat exchanger 1 is respectively communicated with the inlets of the first dehydrated molecular sieve device 4-1 and the second dehydrated molecular sieve device 4-2 through pipelines, and the dry gas outlets of the first dehydrated molecular sieve device 4-1 and the second dehydrated molecular sieve device 4-2 are communicated with the inlet of the first gas heat exchanger 3-1 through pipelines;
the outlet of the first gas heat exchanger 3-1 is respectively communicated with the inlets of the first carbon dioxide molecular sieve device 5-1 and the second carbon dioxide molecular sieve device 5-2 through pipelines, the carbon dioxide mixed gas outlets of the first carbon dioxide molecular sieve device 5-1 and the second carbon dioxide molecular sieve device 5-2 are sequentially communicated with the refrigerant heat exchanger 13, the gas-water separator 14, the compressor 6, the second gas heat exchanger 3-2, the refrigerator 7 and the desublimation separator 8 through pipelines, the solid outlet of the gas-water separator 14 is communicated with the ice storage tank 15 through pipelines, the solid carbon dioxide outlet of the desublimation separator 8 is communicated with the carbon dioxide storage tank 12 through pipelines, and the high-pressure impurity gas outlet of the desublimation separator 8 is sequentially communicated with the second gas heat exchanger 3-2, the first gas heat exchanger 3-1 and the compressed gas storage tank 9 through pipelines;
the outlet of the compressed gas storage tank 9 is communicated with the first hot water heat exchanger 11-1, the first expansion machine 10-1, the second hot water heat exchanger 11-2, the second expansion machine 10-2, the third hot water heat exchanger 11-3 and the third expansion machine 10-3 in sequence through pipelines, and the outlet of the third expansion machine 10-3 is communicated with a gas discharge pipeline.
The air inlet of the flue gas-cold water heat exchanger 1 is used for receiving low carbon dioxide concentration flue gas;
the low-temperature flue gas output by the flue gas-cold water heat exchanger 1 in the specific embodiment is separated from water through a dehydration molecular sieve group;
the dry flue gas output by the dehydration molecular sieve group in the specific embodiment sequentially enters the first gas heat exchanger 3-1 and the carbon dioxide molecular sieve group;
the carbon dioxide molecular sieve group in the specific embodiment is used for adsorbing and enriching carbon dioxide in the flue gas and outputting high-concentration carbon dioxide mixed gas and impurity mixed gas;
the mixed gas with high carbon dioxide concentration output by the carbon dioxide molecular sieve group in the specific embodiment enters a refrigerant heat exchanger 13 for cooling, a gas-water separator 14 separates out solid water, a compressor 6 carries out pressurization, a second gas heat exchanger 3-2 cools down and then enters a refrigerator 7;
the refrigerator 7 of the specific embodiment cools the mixed gas with high carbon dioxide concentration and then enters the desublimation separator 8 to separate solid carbon dioxide and high-pressure impurity gas;
the solid carbon dioxide output from the desublimation separator 8 enters a carbon dioxide storage tank 12.
The compressed gas energy storage unit comprises a high-pressure gas storage tank 9, which is used for storing high-pressure impurity gas output by the desublimation separator 8;
the power generation unit of the specific embodiment comprises an expansion unit and a hot water heat exchanger group, wherein the air outlet of the third expansion machine 10-3 is used for discharging impurity gas after acting;
in the specific embodiment, the carbon dioxide trapping system is additionally provided with the compressed gas energy storage unit and the power generation unit to recover impurity gases except carbon dioxide in the flue gas, and because the impurity gases have higher pressure, the recovery of the impurity gases is used for acting power generation, so that the recovery, storage and recycling of energy sources are realized.
The beneficial effects of this concrete implementation are:
the flue gas carbon dioxide trapping system provided by the embodiment can carry out pollution-free and low-energy-consumption physical separation on low-concentration (volume percentage is not more than 10%) carbon dioxide flue gas discharged by industry, can remove water in the flue gas, remove more than 95% of water in the flue gas, improves the purity of carbon dioxide products to 99% -99.9%, and can obviously reduce the carbon dioxide trapping energy consumption.
The flue gas carbon dioxide trapping system provided by the embodiment can be used for drying flue gas and recovering moisture in the flue gas; the concentration of carbon dioxide in the flue gas can be improved through the molecular sieve, and finally, the carbon dioxide is separated in a solid form, and the carbon dioxide trapping rate can be more than 90%; the high-pressure impurity gas can complete the energy storage function of the compressed gas, and can generate electricity through the expansion unit, so that the comprehensive treatment of the flue gas is realized.
In summary, the system has the following advantages compared with other systems:
1. can remove more than 95% of water in the flue gas.
2. The recovery rate of carbon dioxide is more than 90%, and the purity of the carbon dioxide product is improved to 99% -99.9%.
3. The energy collection device is low in energy consumption and has an energy storage function, and a 100MW unit uses the system to treat smoke, so that the net power consumption is about 20 MW.
The second embodiment is as follows: the first difference between this embodiment and the specific embodiment is that: a first smoke regulating valve 2-5 is arranged on a moisture regeneration outlet of the first dehydration molecular sieve device 4-1; the second smoke regulating valve 2-6 is arranged on the moisture regeneration outlet of the second dehydrating molecular sieve device 4-2. The other is the same as in the first embodiment.
And a third specific embodiment: this embodiment differs from one or both of the embodiments in that: a first dehydrated molecular sieve device inlet valve 2-1 is arranged on a pipeline between the flue gas-cold water heat exchanger 1 and the first dehydrated molecular sieve device 4-1, and a second dehydrated molecular sieve device inlet valve 2-2 is arranged on a pipeline between the flue gas-cold water heat exchanger 1 and the second dehydrated molecular sieve device 4-2; the pipeline between the first dehydrated molecular sieve device 4-1 and the first gas heat exchanger 3-1 is provided with a first dehydrated molecular sieve device outlet valve 2-3, and the pipeline between the second dehydrated molecular sieve device 4-2 and the first gas heat exchanger 3-1 is provided with a second dehydrated molecular sieve device outlet valve 2-4. The other is the same as the first or second embodiment.
The specific embodiment IV is as follows: this embodiment differs from one of the first to third embodiments in that: a first carbon dioxide molecular sieve device inlet valve 2-7 is arranged on a pipeline between the first gas heat exchanger 3-1 and the first carbon dioxide molecular sieve device 5-1, and a second carbon dioxide molecular sieve device inlet valve 2-8 is arranged on a pipeline between the first gas heat exchanger 3-1 and the second carbon dioxide molecular sieve device 5-2; a first carbon dioxide outlet regulating valve 2-11 is arranged on a pipeline between the first carbon dioxide molecular sieve device 5-1 and the refrigerant heat exchanger 13; and a second carbon dioxide outlet regulating valve 2-12 is arranged on a pipeline between the second carbon dioxide molecular sieve device 5-2 and the refrigerant heat exchanger 13. The other embodiments are the same as those of the first to third embodiments.
Fifth embodiment: this embodiment differs from one to four embodiments in that: the impurity gas outlet of the first carbon dioxide molecular sieve device 5-1 is provided with a first carbon dioxide molecular sieve device outlet valve 2-9; the impurity gas outlet of the second carbon dioxide molecular sieve device 5-2 is provided with a second carbon dioxide molecular sieve device outlet valve 2-10. The other embodiments are the same as those of the first to fourth embodiments.
Specific embodiment six: this embodiment differs from one of the first to fifth embodiments in that: the pipeline between the compressed gas storage tank 9 and the first hot water heat exchanger 11-1 is provided with a high-pressure gas outlet regulating valve 2-13. The other embodiments are the same as those of the first to fifth embodiments.
Seventh embodiment: this embodiment differs from one of the first to sixth embodiments in that: the operating temperature range of the first dehydrating molecular sieve device 4-1 and the second dehydrating molecular sieve device 4-2 is 10 ℃ to 100 ℃; the operating temperature of the first carbon dioxide molecular sieve device 5-1 and the second carbon dioxide molecular sieve device 5-2 ranges from 10 ℃ to 120 ℃. The other embodiments are the same as those of the first to sixth embodiments.
Eighth embodiment: this embodiment differs from one of the first to seventh embodiments in that: the operation pressure range of the desublimation separator 8 is 0.1MPa to 3MPa, and the operation temperature range is-80 ℃ to-140 ℃. The others are the same as those of the seventh embodiment.
Detailed description nine: the application method of the carbon trapping system for the low-carbon-dioxide-concentration flue gas in the embodiment comprises the following steps of:
1. inputting smoke, starting the smoke-cold water heat exchanger 1, adjusting the outlet temperature of the smoke-cold water heat exchanger 1 to be 25-45 ℃, and enabling the smoke to enter the smoke-cold water heat exchanger 1 for cooling treatment; the operation temperature of the dehydration molecular sieve group is regulated to be 20-40 ℃, and the cooled flue gas enters the dehydration molecular sieve group for drying treatment; adjusting the running temperature of the carbon dioxide molecular sieve group to be 20-30 ℃, cooling the dried flue gas in a first gas heat exchanger 3-1, and then, introducing the cooled flue gas into the carbon dioxide molecular sieve group for carbon dioxide adsorption enrichment, and discharging impurity gas;
2. after the carbon dioxide molecular sieve group adsorption enrichment process is finished, regulating the operating temperature of the carbon dioxide molecular sieve group to 100-200 ℃, starting a refrigerant heat exchanger 13, regulating the outlet temperature of the refrigerant heat exchanger 13 to minus 2-minus 10 ℃, starting a compressor 6, regulating the outlet pressure of the compressor 6 to 0.1-3.1 MPa, starting a refrigerator 7, regulating the temperature of the refrigerator 7 to minus 100-minus 140 ℃, enabling carbon dioxide mixed gas in the carbon dioxide molecular sieve group to enter the refrigerant heat exchanger 13 for cooling treatment, enabling the cooled carbon dioxide mixed gas to enter a gas-water separator 14, enabling separated water to enter an ice storage tank 15 in a solid form, enabling the separated gas to enter a desublimation separator 8 after being pressurized by the compressor 6 and cooled by the second gas heat exchanger 3-2, enabling solid carbon dioxide separated by the desublimation separator 8 to enter a carbon dioxide storage tank 12, enabling high-pressure impurity gas separated by the desublimation separator 8 to sequentially pass through the second gas heat exchanger 3-2 and the first gas heat exchanger 3-1 for heating, and then entering a compressed gas storage tank 9;
3. the separated high-pressure impurity gas is discharged from the compressed gas storage tank 9 and sequentially passes through the first expander 10-1, the second expander 10-2 and the third expander 10-3 to perform work and generate power.
Detailed description ten: this embodiment differs from the ninth embodiment in that: the volume percentage of carbon dioxide in the flue gas in the first step is not more than 10%, and the volume percentage of the water content is 5% -20%. The other is the same as in the ninth embodiment.
The following examples are used to verify the benefits of the present invention:
in the first embodiment, taking the flue gas treatment of a 100MW unit as an example:
a carbon trapping system of low carbon dioxide concentration flue gas comprises a flue gas-cold water heat exchanger 1, a dehydrated molecular sieve group, a carbon dioxide molecular sieve group, a compressor 6, a refrigerator 7, a desublimation separator 8, a compressed gas storage tank 9, an expansion unit, a carbon dioxide storage tank 12, a refrigerant heat exchanger 13, a gas-water separator 14 and an ice storage tank 15;
the dehydration molecular sieve group is formed by arranging a first dehydration molecular sieve device 4-1 and a second dehydration molecular sieve device 4-2 in parallel;
the carbon dioxide molecular sieve group is formed by arranging a first carbon dioxide molecular sieve device 5-1 and a second carbon dioxide molecular sieve device 5-2 in parallel;
the expansion unit is formed by serially connecting a first expansion machine 10-1, a second expansion machine 10-2 and a third expansion machine 10-3;
the flue gas inlet pipe is communicated with the inlet of the flue gas-cold water heat exchanger 1, the outlet of the flue gas-cold water heat exchanger 1 is respectively communicated with the inlets of the first dehydrated molecular sieve device 4-1 and the second dehydrated molecular sieve device 4-2 through pipelines, and the dry gas outlets of the first dehydrated molecular sieve device 4-1 and the second dehydrated molecular sieve device 4-2 are communicated with the inlet of the first gas heat exchanger 3-1 through pipelines;
the outlet of the first gas heat exchanger 3-1 is respectively communicated with the inlets of the first carbon dioxide molecular sieve device 5-1 and the second carbon dioxide molecular sieve device 5-2 through pipelines, the carbon dioxide mixed gas outlets of the first carbon dioxide molecular sieve device 5-1 and the second carbon dioxide molecular sieve device 5-2 are sequentially communicated with the refrigerant heat exchanger 13, the gas-water separator 14, the compressor 6, the second gas heat exchanger 3-2, the refrigerator 7 and the desublimation separator 8 through pipelines, the solid outlet of the gas-water separator 14 is communicated with the ice storage tank 15 through pipelines, the solid carbon dioxide outlet of the desublimation separator 8 is communicated with the carbon dioxide storage tank 12 through pipelines, and the high-pressure impurity gas outlet of the desublimation separator 8 is sequentially communicated with the second gas heat exchanger 3-2, the first gas heat exchanger 3-1 and the compressed gas storage tank 9 through pipelines;
the outlet of the compressed gas storage tank 9 is communicated with the first hot water heat exchanger 11-1, the first expansion machine 10-1, the second hot water heat exchanger 11-2, the second expansion machine 10-2, the third hot water heat exchanger 11-3 and the third expansion machine 10-3 in sequence through pipelines, and the outlet of the third expansion machine 10-3 is communicated with a gas discharge pipeline.
A first flue gas regulating valve 2-5 is arranged on a moisture regeneration outlet of the first dehydration molecular sieve device 4-1; the second smoke regulating valve 2-6 is arranged on the moisture regeneration outlet of the second dehydrating molecular sieve device 4-2.
A first dehydrated molecular sieve device inlet valve 2-1 is arranged on a pipeline between the flue gas-cold water heat exchanger 1 and the first dehydrated molecular sieve device 4-1, and a second dehydrated molecular sieve device inlet valve 2-2 is arranged on a pipeline between the flue gas-cold water heat exchanger 1 and the second dehydrated molecular sieve device 4-2; the pipeline between the first dehydrated molecular sieve device 4-1 and the first gas heat exchanger 3-1 is provided with a first dehydrated molecular sieve device outlet valve 2-3, and the pipeline between the second dehydrated molecular sieve device 4-2 and the first gas heat exchanger 3-1 is provided with a second dehydrated molecular sieve device outlet valve 2-4.
A first carbon dioxide molecular sieve device inlet valve 2-7 is arranged on a pipeline between the first gas heat exchanger 3-1 and the first carbon dioxide molecular sieve device 5-1, and a second carbon dioxide molecular sieve device inlet valve 2-8 is arranged on a pipeline between the first gas heat exchanger 3-1 and the second carbon dioxide molecular sieve device 5-2; a first carbon dioxide outlet regulating valve 2-11 is arranged on a pipeline between the first carbon dioxide molecular sieve device 5-1 and the refrigerant heat exchanger 13; and a second carbon dioxide outlet regulating valve 2-12 is arranged on a pipeline between the second carbon dioxide molecular sieve device 5-2 and the refrigerant heat exchanger 13.
The impurity gas outlet of the first carbon dioxide molecular sieve device 5-1 is provided with a first carbon dioxide molecular sieve device outlet valve 2-9; the impurity gas outlet of the second carbon dioxide molecular sieve device 5-2 is provided with a second carbon dioxide molecular sieve device outlet valve 2-10.
The pipeline between the compressed gas storage tank 9 and the first hot water heat exchanger 11-1 is provided with a high-pressure gas outlet regulating valve 2-13.
The first dehydration molecular sieve device 4-1 and the second dehydration molecular sieve device 4-2 are internally provided with ZSM-5 molecular sieves, and the operating temperature ranges from 10 ℃ to 100 ℃; the first carbon dioxide molecular sieve device 5-1 and the second carbon dioxide molecular sieve device 5-2 are internally provided with 4A molecular sieves, and the operating temperature ranges from 10 ℃ to 120 ℃.
The operation pressure range of the desublimation separator 8 is 0.1MPa to 3MPa, and the operation temperature range is-80 ℃ to-140 ℃.
The application method of the carbon trapping system for the low-carbon-dioxide-concentration flue gas comprises the following steps:
1. inputting smoke, starting the smoke-cold water heat exchanger 1, adjusting the outlet temperature of the smoke-cold water heat exchanger 1 to be 30 ℃, and enabling the smoke to enter the smoke-cold water heat exchanger 1 for cooling treatment; the operation temperature of the dehydration molecular sieve group is regulated to be 20 ℃, and the cooled flue gas enters the dehydration molecular sieve group for drying treatment; adjusting the running temperature of the carbon dioxide molecular sieve group to 25 ℃, cooling the dried flue gas to 25 ℃ in a first gas heat exchanger 3-1, and then, introducing the flue gas into the carbon dioxide molecular sieve group to perform carbon dioxide adsorption enrichment, and discharging impurity gas;
2. after the carbon dioxide molecular sieve group adsorption enrichment process is finished, regulating the operating temperature of the carbon dioxide molecular sieve group to 120 ℃, starting a refrigerant heat exchanger 13, regulating the outlet temperature of the refrigerant heat exchanger 13 to-2 ℃, starting a compressor 6, regulating the outlet pressure of the compressor 6 to 0.3MPa, starting a refrigerator 7, regulating the temperature of the refrigerator 7 to-120 ℃, regulating the operating pressure of a desublimation separator 8 to 0.12MPa, regulating the operating temperature to-120 ℃, introducing carbon dioxide mixed gas in the carbon dioxide molecular sieve group into the refrigerant heat exchanger 13 for cooling treatment, introducing cooled carbon dioxide mixed gas into a gas-water separator 14, introducing separated water into an ice storage tank 15 in a solid form, introducing separated gas into the compressor 6, pressurizing and cooling by the compressor 6 and introducing the cooled gas into a desublimation separator 8, introducing solid carbon dioxide separated by the desublimation separator 8 into a carbon dioxide storage tank 12, introducing high-pressure impurity gas separated by the desublimation separator 8 into a compressed gas storage tank 9 after being sequentially heated to 15 ℃ through a second gas heat exchanger 3-2 and a first gas heat exchanger 3-1;
3. the separated high-pressure impurity gas is discharged from the compressed gas storage tank 9 and sequentially passes through the first expander 10-1, the second expander 10-2 and the third expander 10-3 to perform work and power generation, and the gas discharge pressure is 0.1MPa.
In the dehydration process, the first dehydration molecular sieve device 4-1 or the second dehydration molecular sieve device 4-2 is selected for dehydration, and the rest dehydration molecular sieve devices are used for molecular sieve regeneration; in the carbon dioxide adsorption enrichment process, the first carbon dioxide molecular sieve device 5-1 or the second carbon dioxide molecular sieve device 5-2 is selected from the carbon dioxide molecular sieve group for carbon dioxide adsorption enrichment, and the rest carbon dioxide molecular sieve devices are used for molecular sieve regeneration.
The volume percentage of carbon dioxide in the flue gas in the first step is 10%, and the volume percentage of the water content is 16%.
The first hot water heat exchanger 11-1, the second hot water heat exchanger 11-2 and the third hot water heat exchanger 11-3 are used for heating, and enter an expansion unit after being heated.
A simulation experiment is carried out on the system in the embodiment I, a 100MW gas turbine unit is simulated, the simulated flue gas flow is 110kg/s, the inlet flue gas temperature is 110 ℃, the carbon dioxide concentration in the flue gas is 10%, and under the condition that the volume percentage of the water content is 16%, the carbon dioxide capture rate and the carbon dioxide recovery rate are 90.2%, the dehydration rate is 99%, and the carbon dioxide purity is 99.92%.
The embodiment has lower energy consumption and energy storage function, and the 100MW unit uses the system to treat the flue gas, so that the net power consumption is about 20 MW.
Claims (10)
1. The carbon trapping system for the low-carbon-dioxide-concentration flue gas is characterized by comprising a flue gas-cold water heat exchanger (1), a dehydrated molecular sieve group, a carbon dioxide molecular sieve group, a compressor (6), a refrigerator (7), a desublimation separator (8), a compressed gas storage tank (9), an expansion unit, a carbon dioxide storage tank (12), a refrigerant heat exchanger (13), a gas-water separator (14) and an ice storage tank (15);
the dehydration molecular sieve group is formed by parallel connection of a first dehydration molecular sieve device (4-1) and a second dehydration molecular sieve device (4-2);
the carbon dioxide molecular sieve group is formed by arranging a first carbon dioxide molecular sieve device (5-1) and a second carbon dioxide molecular sieve device (5-2) in parallel;
the expansion unit is formed by connecting a first expansion machine (10-1), a second expansion machine (10-2) and a third expansion machine (10-3) in series;
the flue gas inlet pipe is communicated with the inlet of the flue gas-cold water heat exchanger (1), the outlet of the flue gas-cold water heat exchanger (1) is respectively communicated with the inlets of the first dehydrating molecular sieve device (4-1) and the second dehydrating molecular sieve device (4-2) through pipelines, and the dry gas outlets of the first dehydrating molecular sieve device (4-1) and the second dehydrating molecular sieve device (4-2) are communicated with the inlet of the first gas heat exchanger (3-1) through pipelines;
the outlet of the first gas heat exchanger (3-1) is respectively communicated with the inlets of the first carbon dioxide molecular sieve device (5-1) and the second carbon dioxide molecular sieve device (5-2) through pipelines, the carbon dioxide mixed gas outlets of the first carbon dioxide molecular sieve device (5-1) and the second carbon dioxide molecular sieve device (5-2) are sequentially communicated with the refrigerant heat exchanger (13), the gas-water separator (14), the compressor (6), the second gas heat exchanger (3-2), the refrigerator (7) and the desublimation separator (8) through pipelines, the solid outlet of the gas-water separator (14) is communicated with the ice storage tank (15) through pipelines, the solid carbon dioxide outlet of the desublimation separator (8) is communicated with the carbon dioxide storage tank (12) through pipelines, and the high-pressure impurity gas outlet of the desublimation separator (8) is sequentially communicated with the second gas heat exchanger (3-2), the first gas heat exchanger (3-1) and the compressed gas storage tank (9) through pipelines;
the outlet of the compressed gas storage tank (9) is communicated with the first hot water heat exchanger (11-1), the first expander (10-1), the second hot water heat exchanger (11-2), the second expander (10-2), the third hot water heat exchanger (11-3) and the third expander (10-3) in sequence through pipelines, and the outlet of the third expander (10-3) is communicated with a gas discharge pipeline.
2. The carbon capturing system of low carbon dioxide concentration flue gas according to claim 1, wherein a first flue gas regulating valve (2-5) is arranged on a moisture regeneration outlet of the first dehydrating molecular sieve device (4-1); and a second smoke regulating valve (2-6) is arranged on a moisture regeneration outlet of the second dehydration molecular sieve device (4-2).
3. The carbon capturing system of the low carbon dioxide concentration flue gas according to claim 1, wherein a first dehydrated molecular sieve device inlet valve (2-1) is arranged on a pipeline between the flue gas-cold water heat exchanger (1) and the first dehydrated molecular sieve device (4-1), and a second dehydrated molecular sieve device inlet valve (2-2) is arranged on a pipeline between the flue gas-cold water heat exchanger (1) and the second dehydrated molecular sieve device (4-2); the pipeline between the first dehydrated molecular sieve device (4-1) and the first gas heat exchanger (3-1) is provided with a first dehydrated molecular sieve device outlet valve (2-3), and the pipeline between the second dehydrated molecular sieve device (4-2) and the first gas heat exchanger (3-1) is provided with a second dehydrated molecular sieve device outlet valve (2-4).
4. The carbon capturing system of the low carbon dioxide concentration flue gas according to claim 1, wherein a first carbon dioxide molecular sieve device inlet valve (2-7) is arranged on a pipeline between the first gas heat exchanger (3-1) and the first carbon dioxide molecular sieve device (5-1), and a second carbon dioxide molecular sieve device inlet valve (2-8) is arranged on a pipeline between the first gas heat exchanger (3-1) and the second carbon dioxide molecular sieve device (5-2); a first carbon dioxide outlet regulating valve (2-11) is arranged on a pipeline between the first carbon dioxide molecular sieve device (5-1) and the refrigerant heat exchanger (13); and a second carbon dioxide outlet regulating valve (2-12) is arranged on a pipeline between the second carbon dioxide molecular sieve device (5-2) and the refrigerant heat exchanger (13).
5. The carbon capturing system of the low carbon dioxide concentration flue gas according to claim 1, wherein the impurity gas outlet of the first carbon dioxide molecular sieve device (5-1) is provided with a first carbon dioxide molecular sieve device outlet valve (2-9); the impurity gas outlet of the second carbon dioxide molecular sieve device (5-2) is provided with a second carbon dioxide molecular sieve device outlet valve (2-10).
6. The carbon capturing system of low carbon dioxide concentration flue gas according to claim 1, wherein a high pressure gas outlet regulating valve (2-13) is arranged on a pipeline between the compressed gas storage tank (9) and the first hot water heat exchanger (11-1).
7. The carbon capture system of low carbon dioxide concentration flue gas according to claim 1, wherein the operating temperature of the first (4-1) and second (4-2) dehydrated molecular sieve devices is in the range of 10 ℃ to 100 ℃; the operating temperature range of the first carbon dioxide molecular sieve device (5-1) and the second carbon dioxide molecular sieve device (5-2) is 10 ℃ to 120 ℃.
8. A carbon capture system for low carbon dioxide concentration flue gas according to claim 1, characterized in that the desublimation separator (8) operates at a pressure ranging from 0.1MPa to 3MPa and at a temperature ranging from-80 ℃ to-140 ℃.
9. The method of using a carbon capture system for low carbon dioxide concentration flue gas according to claim 1, wherein the method comprises the steps of:
1. inputting smoke, starting a smoke-cold water heat exchanger (1), adjusting the outlet temperature of the smoke-cold water heat exchanger (1) to be 25-45 ℃, and enabling the smoke to enter the smoke-cold water heat exchanger (1) for cooling treatment; the operation temperature of the dehydration molecular sieve group is regulated to be 20-40 ℃, and the cooled flue gas enters the dehydration molecular sieve group for drying treatment; adjusting the running temperature of the carbon dioxide molecular sieve group to be 20-30 ℃, cooling the dried flue gas in a first gas heat exchanger (3-1), and then, introducing the cooled flue gas into the carbon dioxide molecular sieve group for carbon dioxide adsorption enrichment, and discharging impurity gas;
2. after the carbon dioxide molecular sieve group adsorption enrichment process is finished, regulating the operation temperature of the carbon dioxide molecular sieve group to be 100-200 ℃, starting a refrigerant heat exchanger (13), regulating the outlet temperature of the refrigerant heat exchanger (13) to be minus 2-minus 10 ℃, starting a compressor (6), regulating the outlet pressure of the compressor (6) to be 0.1-3.1 MPa, starting a refrigerator (7), regulating the temperature of the refrigerator (7) to be minus 100-minus 140 ℃, enabling carbon dioxide mixed gas in the carbon dioxide molecular sieve group to enter the refrigerant heat exchanger (13) for cooling treatment, enabling cooled carbon dioxide mixed gas to enter a gas-water separator (14), enabling separated water to enter an ice storage tank (15) in a solid form, enabling separated gas to enter the compressor (6), pressurizing through the compressor (6) and enabling the cooled gas to enter a desublimation separator (8), enabling solid carbon dioxide separated by the desublimation separator (8) to enter a carbon dioxide storage tank (12), and enabling high-pressure impurity gas separated by the desublimation separator (8) to sequentially enter the second gas heat exchanger (3-2) and the first gas heat exchanger (3-1) for compressing the gas;
3. the separated high-pressure impurity gas is discharged from a compressed gas storage tank (9) and sequentially passes through a first expander (10-1), a second expander (10-2) and a third expander (10-3) to do work and generate electricity.
10. The method for using a carbon capture system for low carbon dioxide concentration flue gas according to claim 9, wherein the carbon dioxide content in the flue gas in the first step is not more than 10% by volume, and the water content is 5% -20% by volume.
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