CN117180928A - Gas trapping and storing system and method - Google Patents
Gas trapping and storing system and method Download PDFInfo
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- CN117180928A CN117180928A CN202311284358.7A CN202311284358A CN117180928A CN 117180928 A CN117180928 A CN 117180928A CN 202311284358 A CN202311284358 A CN 202311284358A CN 117180928 A CN117180928 A CN 117180928A
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- 238000000034 method Methods 0.000 title claims abstract description 19
- 238000003795 desorption Methods 0.000 claims abstract description 135
- 239000007789 gas Substances 0.000 claims abstract description 121
- 238000010521 absorption reaction Methods 0.000 claims abstract description 89
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 66
- 239000007788 liquid Substances 0.000 claims abstract description 40
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 38
- 239000003546 flue gas Substances 0.000 claims abstract description 38
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 34
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 34
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 33
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 33
- 239000012528 membrane Substances 0.000 claims description 27
- 238000004891 communication Methods 0.000 claims description 24
- 238000001926 trapping method Methods 0.000 claims description 5
- 229910021386 carbon form Inorganic materials 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 16
- 230000005540 biological transmission Effects 0.000 abstract description 4
- 230000008929 regeneration Effects 0.000 abstract description 4
- 238000011069 regeneration method Methods 0.000 abstract description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 37
- 229910052757 nitrogen Inorganic materials 0.000 description 16
- 239000000047 product Substances 0.000 description 10
- 238000006243 chemical reaction Methods 0.000 description 8
- 239000006096 absorbing agent Substances 0.000 description 6
- 150000001412 amines Chemical class 0.000 description 5
- 229910001873 dinitrogen Inorganic materials 0.000 description 5
- 238000012856 packing Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 239000012071 phase Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 230000005501 phase interface Effects 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 description 1
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
Classifications
-
- 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
Landscapes
- Treating Waste Gases (AREA)
Abstract
The application discloses a gas trapping and storing system and a gas trapping and storing method. The gas trapping and storing system of the present application comprises: the absorption unit is provided with a first inlet and a first outlet, carbon-containing flue gas is sent into the absorption unit from the first inlet, carbon dioxide is contained in the carbon-containing flue gas, the carbon-containing flue gas contacts with absorption liquid in the absorption unit to form a first solution, and the first solution is sent out from the first outlet; the desorption unit is provided with a second inlet, and the first solution sent out from the first outlet is sent into the desorption unit from the second inlet; and the gas transmission unit is used for feeding desorption gas into the desorption unit, and the desorption gas contacts with the first solution to finish desorption of at least part of carbon dioxide to form a second solution, and the second solution is fed into the absorption unit from the desorption unit. The gas trapping and storing system reduces the partial pressure of carbon dioxide by utilizing the desorption gas, promotes desorption, reduces the regeneration energy consumption of the desorption system and reduces the running cost of the system.
Description
Technical Field
The application relates to the field of ship tail gas purification, in particular to a gas trapping and storing system and a gas trapping and storing method.
Background
The ship carbon capture and sealing post-treatment technology has become an important technical route for ship emission due to the advantages of high emission reduction strength, good matching performance for the ship operation condition, economy and the like. Although the technology can realize large-scale carbon emission reduction, the problem of high energy consumption for system desorption exists, and the application requirements of actual ships are difficult to meet.
Disclosure of Invention
The application aims to provide a gas trapping and storing system and a gas trapping and storing method, which can solve the technical problems.
The embodiment of the application provides a gas trapping and storing system, which comprises:
the absorption unit is provided with a first inlet and a first outlet, carbon-containing flue gas is sent into the absorption unit from the first inlet, the carbon-containing flue gas contains carbon dioxide, the carbon-containing flue gas contacts with absorption liquid in the absorption unit to form a first solution, and the first solution is sent out from the first outlet;
a desorption unit, wherein the desorption unit is provided with a second inlet, and the first solution sent out from the first outlet is sent into the desorption unit from the second inlet;
and the gas transmission unit is used for feeding desorption gas into the desorption unit, the desorption gas is contacted with the first solution, desorption of at least part of the carbon dioxide is completed, a second solution is formed, and the second solution is fed into the absorption unit from the desorption unit.
In some embodiments, the circulation unit further comprises a first circulation pump, an inlet of the first circulation pump being in communication with the first outlet, an outlet of the first circulation pump being in communication with the second inlet.
In some embodiments, the circulation unit includes a second circulation pump, the absorption unit has a third inlet, the desorption unit has a second outlet, the inlet of the second circulation pump is in communication with the second outlet, and the outlet of the second circulation pump is in communication with the third inlet.
In some embodiments, the circulation unit comprises a heat exchanger in communication with the outlet of the first circulation pump and the outlet of the second circulation pump, respectively.
In some embodiments, the heat exchanger has a first heat exchange outlet in communication with the second inlet; the heat exchanger has a second heat exchange outlet in communication with the third inlet.
In some embodiments, the circulation unit includes a first heater disposed between the first heat exchange outlet and the second inlet.
In some embodiments, the circulation unit comprises a cooler disposed between the second heat exchange outlet and the third inlet.
In some embodiments, the gas transfer unit comprises a membrane separator, the desorption unit having a third outlet, an inlet of the membrane separator being in communication with the third outlet.
In some embodiments, the gas transfer unit includes a condenser disposed between the membrane separator and the third outlet.
In some embodiments, the gas transfer unit includes a second heater, the desorption unit having a fourth inlet, the second heater disposed between the membrane separator and the fourth inlet.
In some embodiments, the gas transfer unit has a fifth inlet for feeding a desorption gas.
Correspondingly, the application provides a gas trapping method, which comprises the following steps:
the method comprises the steps that carbon-containing flue gas is sent to an absorption unit, an absorption liquid is arranged in the absorption unit, the carbon-containing flue gas comprises carbon dioxide, and a first solution is formed after the absorption liquid is contacted with the carbon-containing flue gas;
the first solution is sent to a desorption unit, and a gas delivery unit sends desorption gas to the desorption unit for desorbing carbon dioxide in the first solution;
the desorbed first solution forms a second solution, which is fed from the desorption unit to the absorption unit.
In some embodiments, the absorption unit has a first gas pressure in the range of 0.8 to 1.2bar.
In some embodiments, the absorption unit has a first temperature in the range of 30-40 ℃.
In some embodiments, the desorption unit has a second gas pressure in the range of 0.8 to 1.2bar.
In some embodiments, the desorption unit has a second temperature in the range of 80 to 90 ℃.
The application has the beneficial effects that: compared with the prior art, the application provides a gas trapping and storing system and a method. The gas trapping and storing system of the present application comprises: absorption unit: the absorption unit is provided with a first inlet and a first outlet, carbon-containing flue gas is sent into the absorption unit from the first inlet, carbon dioxide is contained in the carbon-containing flue gas, the carbon-containing flue gas contacts with absorption liquid in the absorption unit to form a first solution, and the first solution is sent out from the first outlet; the desorption unit is provided with a second inlet, and the first solution sent out from the first outlet is sent into the desorption unit from the second inlet; and the gas transmission unit is used for feeding gas into the desorption unit, and the gas contacts with the first solution to complete desorption of at least part of carbon dioxide to form a second solution, and the second solution is fed into the absorption unit from the desorption unit. According to the gas trapping and storing system, partial pressure of carbon dioxide in the desorption system is reduced by utilizing the desorption gas, so that desorption reaction of the carbon dioxide is promoted, regeneration energy consumption of the desorption system is reduced, and system operation cost is reduced.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings that are needed in the description of the embodiments will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present application, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of stripping desorption for double membrane theory;
FIG. 2 is a schematic diagram of a gas trapping and storing system according to an embodiment of the application;
FIG. 3 is a schematic flow chart of a gas trapping method according to an embodiment of the application;
in the figure, 100-absorption unit, 110-absorption column 101-first inlet, 102-first outlet, 103-third inlet, 200-desorption unit, 210-desorption column, 201-second inlet, 202-second outlet, 203-third outlet, 204-fourth inlet, 300-gas transfer unit, 301-membrane separator, 302-condenser, 303-second heater, 304-fifth inlet, 400-circulation unit, 401-first circulation pump, 402-second circulation pump, 403-heat exchanger, 4031-first heat exchange outlet, 4032-second heat exchange outlet, 404-first heater, 405-cooler.
Detailed Description
The following description of the embodiments of the present application will be made clearly and fully with reference to the accompanying drawings, in which it is evident that the embodiments described are only some, but not all embodiments of the application. All other embodiments, which can be made by those skilled in the art based on the embodiments of the application without making any inventive effort, are intended to fall within the scope of the application. In addition, in the description of the present application, the term "comprising" means "including but not limited to". The terms first, second, third and the like are used merely as labels, and do not impose numerical requirements or on the order of construction. Various embodiments of the application may exist in a range of forms; it should be understood that the description in a range format is merely for convenience and brevity and should not be construed as a rigid limitation on the scope of the application; it is therefore to be understood that the range description has specifically disclosed all possible sub-ranges and individual values within that range. For example, it should be considered that a description of a range from 1 to 6 has specifically disclosed sub-ranges, such as from 1 to 3, from 1 to 4, from 1 to 5, from 2 to 4, from 2 to 6, from 3 to 6, etc., as well as single numbers within the ranges, such as 1, 2, 3, 4, 5, and 6, wherever applicable. In addition, whenever a numerical range is referred to herein, it is meant to include any reference number (fractional or integer) within the indicated range.
Stripping of CO 2 The basic raw gas stripping and desorption are based on the double-membrane theory, as shown in fig. 1. The double-film theory considers that a phase interface exists between the gas phase and the liquid phase which are contacted with each other, and a gas film and a liquid film exist at two sides respectively. In the desorption process, the concentration gradient of the air film and the liquid film is CO 2 Mass transfer driving force between gas phase and liquid phase due to gas-liquid two-phase CO 2 Partial pressure is different, under the pushing of pressure difference, CO 2 Reaches the liquid film by the way of molecular diffusion and then enters the air film through a phase interface, thereby leading CO to be 2 Desorbing from the absorption rich liquid. Thus, using solute-free nitrogen or solvent vapor as a carrier gas, CO is 2 Blowing out from the absorption liquid to reduce gas phase CO 2 Partial pressure, thereby improving the mass transfer driving force of the desorption process, and thus enabling CO to be 2 The desorption from the absorption rich liquid can be continued. Stripping of CO 2 Has the advantages of low energy consumption and CO propulsion 2 Desorption reaction rate, CO reduction 2 Desorption reaction temperature, thereby reducing CO 2 The energy consumption in the desorption process reduces the running cost of the system; and the greater the amount of gas introduced, the more CO is desorbed 2 The greater the amount. But due to the limitation of the ship operation environment, the desorbed CO is trapped 2 Requiring storage and subsequent conversion in a ship's tanksUtilization of the process of CO 2 In order to solve the problems of the prior art, the present application provides a gas trapping and storing system, as shown in fig. 2, comprising: the absorption unit 100, the absorption unit 100 is provided with a first inlet 101 and a first outlet 102, carbon-containing flue gas is sent into the absorption unit 100 from the first inlet 101, carbon dioxide is contained in the carbon-containing flue gas, the carbon-containing flue gas contacts with absorption liquid in the absorption unit 100 to form a first solution, and the first solution is sent out from the first outlet 102; a desorption unit 200, the desorption unit 200 having a second inlet 201, the first solution sent from the first outlet 102 being sent from the second inlet 201 to the desorption unit 200; and a gas transfer unit 300, wherein the gas transfer unit 300 is used for feeding desorption gas into the desorption unit 200, and the desorption gas contacts with the first solution to complete desorption of at least part of carbon dioxide, so as to form a second solution, and the second solution is fed into the absorption unit 100 from the desorption unit 200. The gas trapping and storing system reduces the regeneration energy consumption of the system while guaranteeing the complete function of the ship power carbon trapping system, and can further advance the carbon trapping technology to be applied to the field of ship carbon emission reduction.
In some embodiments, the gas capture storage system further comprises a circulation unit 400, the circulation unit 400 comprising a first circulation pump 401, an inlet of the first circulation pump 401 being in communication with the first outlet 102, the second inlet 201 being in communication.
In some embodiments, the main structure of the absorption unit 100 is an absorption tower having a first inlet 101 for the carbonaceous flue gas to be fed into, and in some embodiments, the first inlet 101 is located below the absorption tower, and the carbonaceous flue gas is fed from the first inlet 101 to below the absorption tower, where the carbonaceous flue gas flows from bottom to top.
In some implementations, the absorption unit 100 has a third inlet 103, which in some embodiments is located above the absorption tower, from which the absorption liquid sprays from top to bottom, and from the bottom of which the carbonaceous flue gas enters upward, completing the absorption of the carbonaceous flue gas by the absorption liquid, wherein carbon dioxide in the carbonaceous flue gas is absorbed by the absorption liquid, forming a first solution (rich liquid).
In some implementations, a packing may be disposed within the absorber tower for increasing the contact area and adsorption efficiency of the absorption liquid with the carbonaceous flue gas, and in some embodiments, the packing may be selected from one or more of corrugated plate, ceramic packing, metal packing. The filler may be used in bulk or structured.
In some embodiments, the form, size, type and specification of the packing may be such that the actual removal of CO is based on 2 And selecting parameters such as efficiency, pressure drop requirement in the absorption tower, flooding rate requirement, operation condition and the like.
In some embodiments, the absorbing liquid comprises an organic amine solution, and a single or mixed organic amine solution such as MEA (ethanolamine), MDEA (2-methyl-diethylaminoethanolamine), DEA (diethanolamine) and the like can be used.
In some embodiments, after the carbonaceous flue gas is adsorbed by the absorption liquid, clean flue gas is discharged from the top of the absorption tower.
In some embodiments, the main structure of the desorption unit 200 is a desorption tower 210, and the first solution (rich solution, CO absorbed) in the desorption tower 210 2 Is fed into the desorption column 210 by means of a pump stack).
In some embodiments, a second inlet 201 is provided on the desorber 210, and the first solution is fed from the second inlet 201 to the desorber, and in some embodiments, the second inlet 201 is located above the desorber 210, and the first solution is fed from the top of the desorber 210 to the desorber 210.
In some embodiments, the desorption gas is simultaneously fed into the desorption column 210, and the desorption gas may be nitrogen or solvent vapor without solute. In some embodiments, the desorber 210 has a fourth inlet 204 through which the desorption gas is fed into the desorber 210, and in some embodiments, the fourth inlet 204 is disposed inside the desorber 210. The rich liquid is desorbed in the desorption tower 210 to release CO again 2 A second solution (lean solution) is formed.
In some embodiments, the desorber 210 has a second outlet 202, and in some embodiments, the second outlet 202 is located at the bottom of the desorber 210 and the second solution is fed to the absorber 110 through the second outlet 202.
In some implementationsIn embodiments, the desorber 210 has a third outlet 203, and in some embodiments, the third outlet 203 is located at the top of the desorber 210, the third outlet 203 being for delivering product gas located within the desorber 210. In some embodiments, the product gas at the third outlet 203 at the top of the desorber 210 comprises CO 2 、N 2 And a small amount of water vapor, are fed into the gas delivery unit 300.
In some embodiments, the gas transfer unit 300 includes a membrane separator 301, the inlet of the membrane separator 301 being in communication with the third outlet 203, the membrane separator 301 being, in some embodiments, a nitrogen membrane separator, as well as separating nitrogen from carbon dioxide, the separated carbon dioxide being a high purity gas, and being sent to a storage tank for storage. The nitrogen separated by the membrane separator 301 is again fed into the desorption column 210 to be circulated. In some embodiments, the membrane separator 301 is equipped with a self-pressurizing device to raise the pressure of the product gas, and after passing through the membrane separation device, if the requirement of the liquefaction module on the ship is met, the conventional compression module can be omitted, and the product gas meeting the pressure can be directly liquefied and stored.
In order to achieve purification of the product gas, the gas transfer unit 300 further includes a condenser 302, the condenser 302 is disposed between the membrane separator 301 and the third outlet 203, the condenser 302 is used for separating water vapor in the product gas, and the separated condensed water vapor is sent to the desorption tower 210 for internal circulation, so as to supplement evaporation loss of the water vapor in the desorption tower 210.
In some embodiments, the gas delivery unit 300 includes a second heater 303, the desorption unit 200 has a fourth inlet 204, the second heater 303 is disposed between the membrane separators 301 and the fourth inlet 204, and is used to heat the desorption gas sent into the desorption column 210, maintain the temperature in the desorption column 210, in some embodiments the second heater 303 is an electric heater, and in some embodiments the temperature of the desorption gas heated by the second heater 303 is 85-95 ℃, such as 90 ℃.
In some embodiments, the gas transfer unit 300 has a fifth inlet 304, the fifth inlet 304 being used for feeding the desorption gas, and in some embodiments, the fifth inlet 304 is located between the second heater 303 and the membrane separator 301, for example, the fifth inlet 304 may feed nitrogen gas, which is fed into the second heater 303 together with the nitrogen gas fed from the membrane separator 301, to be heated, and then fed into the desorption column 210, for supplementing or adjusting the amount of the desorption gas fed into the desorption column 210.
In some embodiments, the trapping storage system of the present application further comprises a circulation unit 400, the circulation unit 400 comprising a first circulation pump 401, an inlet of the first circulation pump 401 being in communication with the first outlet 102, and the second inlet 201 being in communication, in some embodiments, the first circulation pump 401 is a rich liquid circulation pump.
The circulation unit 400 comprises a second circulation pump 402, the absorption unit 100 having a third inlet 103, the desorption unit 200 having a second outlet 202, the inlet of the second circulation pump 402 being in communication with the second outlet 202, the outlet of the second circulation pump 402 being in communication with the third inlet 103, the second circulation pump 402 being in some embodiments a lean liquid circulation pump.
In order to adjust the temperature of the lean/rich liquid fed into the absorption column 110 and the desorption column 210, the circulation unit 400 includes a heat exchanger 403, the heat exchanger 403 being respectively communicated with an outlet of the first circulation pump 401 and an outlet of the second circulation pump 402, the heat exchanger 403 having a first heat exchange outlet 4031, the first heat exchange outlet 4031 being communicated with the second inlet 201; the heat exchanger 403 has a second heat exchange outlet 4032, the second heat exchange outlet 4032 being in communication with the third inlet 103.
In some embodiments, the temperature of the first solution sent from the outlet of the first circulation pump 401 to the heat exchanger 403 ranges from 30 to 40 ℃, and after heat exchange by the heat exchanger 403, the temperature of the rich solution sent from the first heat exchange outlet 4031 of the heat exchanger 403 is about 75 to 85 ℃, such as 80 ℃.
In some embodiments, the temperature of the second solution sent from the outlet of the second circulation pump 402 to the heat exchanger 403 ranges from 85 ℃ to 95 ℃, such as 90 ℃, and after heat exchange by the heat exchanger 403, the temperature of the lean solution sent from the second heat exchange outlet 4032 of the heat exchanger 403 is about 45 ℃ to 55 ℃, such as 50 ℃.
In some embodiments, the circulation unit 400 includes a first heater 404, the first heater 404 being disposed between the first heat exchange outlet 4031 and the second inlet 201. The first heater 404 is used to heat the first solution sent from the heat exchanger 403 to a desired temperature, such as from 80 to 90 ℃.
In some embodiments, the circulation unit 400 includes a cooler 405, the cooler 405 being disposed between the second heat exchange outlet 4032 and the third inlet 103, the cooler 405 being configured to reduce the temperature of the second solution entering the absorber tower 110, such as from 50 ℃ to 40 ℃.
As shown in fig. 3, a gas trapping method using the gas trapping storage system shown in fig. 2 includes:
the carbon-containing flue gas is sent into an absorption unit 100, the absorption unit 100 is provided with absorption liquid, the carbon-containing flue gas comprises carbon dioxide, and the absorption liquid is contacted with the carbon-containing flue gas to form a first solution; the first solution is fed into the desorption unit 200, and the gas transfer unit 300 feeds a desorption gas into the desorption unit 200 for desorbing carbon dioxide in the first solution; the desorbed first solution forms a second solution, which is fed from the desorption unit 200 to the absorption unit 100.
In some embodiments, the catalyst contains CO 2 The high temperature ship tail gas of (2) flows through the absorption tower 110, the countercurrent convection mass transfer is carried out on the ship tail gas and the absorption liquid in the absorption tower 110, and then the clean tail gas is discharged from the top of the absorption tower 110. The rich liquid enters the desorption tower 210 from the top after being heated by the heat exchanger 403 under the action of the pump group. In the desorption tower 210, the rich liquid enters the tower from the upper part, nitrogen enters the tower from the lower part after being heated by the first heater 404, the rich liquid is desorbed under the action of hot nitrogen, and CO is released again 2 . Product gas (CO) at the top outlet of the stripping column 2 +N 2 +small amount of water vapor) passes through condenser 302 and membrane separator 301, purified high purity CO 2 The gas is discharged from the system for further storage. The separated nitrogen gas enters the desorption column 210 from the lower part of the desorption column 210 again through the membrane separator 301 and the first heater 404 to continue the next cycle.
In some embodiments, the absorption liquid is an organic amine solution, and the application adopts the organic amine solution to absorb CO in carbon-containing flue gas 2 Performing chemical absorption and desorption, wherein the desorption gas is nitrogen, stripping and desorption are performed by adopting nitrogen,reducing CO in the Desorption column 210 Environment 2 Partial pressure, promoting desorption reaction. The positive reaction (absorption) occurs at normal temperature of 30-40 ℃ and normal pressure, and the reverse reaction (desorption) occurs at lower temperature of 80-90 ℃ and normal pressure.
In a specific application, absorber 110 has a first gas pressure in the range of 0.8 to 1.2bar, such as 1bar. The optimum gas pressure of the absorber 110 of the present application is 1bar, and the entire system does not need to apply any pressure, reducing the component pressure for the circulation pump and the like in the circulation unit 400. In addition, CO in the desorption column 210 is reduced by nitrogen gas 2 Partial pressure of gas to promote CO 2 The desorption reaction occurs, so that the regeneration energy consumption of the system is reduced, and the running cost of the system is reduced. In a specific application example, the absorber 110 has a first temperature therein, and the first temperature ranges from 30 to 40 ℃.
In a specific application example, the desorber 210 has a second gas pressure in the pressure range of 0.8 to 1.2bar, such as 1bar. The optimum air pressure of the desorption column 210 of the present application is 1bar, and the whole system does not need to apply any pressure, so that the pressure of elements such as a circulating pump in the circulating unit 400 and the dosage of a pump group are reduced, and the construction difficulty is reduced. In a specific application example, the desorber 210 has a second temperature in the range of 80 to 90 ℃.
The application adopts nitrogen gas to extract and desorb CO 2 The absorption liquid is not required to be heated to the desorption temperature of 110-120 ℃, so that the energy consumption requirement on the ship end is reduced, and the functional integrity of the system is ensured.
In some embodiments, carbon dioxide is captured by:
the carbon-containing flue gas is sent into an absorption unit 100, the absorption unit 100 is provided with absorption liquid, the carbon-containing flue gas comprises carbon dioxide, the absorption liquid is contacted with the carbon-containing flue gas to form a first solution, the absorption liquid in an absorption tower 110 is an organic amine solution, the temperature in the absorption tower is 40 ℃, and the air pressure in the absorption tower 110 is 1bar;
after the first solution is subjected to heat exchange through the heat exchanger 403, the first solution is sent to the desorption unit 200, and the temperature of the first solution subjected to heat exchange through the heat exchanger 403 is increased from 40 ℃ to 80 ℃; when the temperature in the desorption column 210 is maintained at 80 ℃, the first heater 404 is not required to be heated at this time, and when the temperature in the desorption column 210 is maintained at 90 ℃, the rich liquid is heated to 90 ℃ by the first heater 404 and sent into the desorption column 210;
the gas transfer unit 300 feeds a desorption gas, which is nitrogen, into the desorption unit 200, heats the nitrogen to 90 c by the second heater 303, feeds the nitrogen into the desorption column 210 from bottom to top, and is used to desorb carbon dioxide in the first solution, the temperature of the desorption column 210 is maintained at 80 to 90 c, the gas pressure is 1bar, and in this embodiment, the temperature of the desorption column 210 is maintained at 90 c,
the desorbed first solution forms a second solution, the second solution is subjected to heat exchange by the heat exchanger 403, the temperature of the second solution is reduced from 90 ℃ to 50 ℃ after heat exchange by the heat exchanger 403, and then the second solution is cooled to 40 ℃ by a cooler arranged between the heat exchanger 403 and the third inlet 103 of the absorption tower 110 and is fed into the absorption tower 110.
The product gas sent from the third outlet 203 of the desorption tower 210 is cooled to 30 ℃ by a condenser 302 and sent to a nitrogen membrane separator, the carbon dioxide separated by the nitrogen membrane separator is sent to the next procedure, and the separated nitrogen enters the circulation again.
Referring to table 1, the energy consumption for carbon dioxide desorption and the energy consumption for the stripping and desorption process of the present application in table 1 are compared: the setting parameters of the absorption tower are the same, and the carbon dioxide desorption is different from the application in that a gas transmission unit is not arranged, the temperature range in the desorption tower in the carbon dioxide desorption method is 110-120 ℃, the pressure is 1.5bar, and the temperature range of the desorption tower is 80-90 ℃ and the pressure is 1bar.
Table 1 comparison of energy consumption for different processes
TABLE 2 stripping and energy consumption in the present application
Note 1: the energy consumption of Table 2 was 150Nm 3 Calculating the product gas; sensible heat 40-80 includes the sum of the energy consumption of the first heater and the second heater;
as can be seen from the results in tables 1 and 2, the present application captures carbon dioxide in the carbon-containing flue gas by the stripping and desorbing method, which can greatly reduce the energy consumption of the system, reduce the temperature of the rich liquid fed into the desorber 210 by the circulation unit 400, and reduce the energy consumption of the whole system. The application can separate carbon dioxide and desorption gas through the nitrogen membrane separator, and the separated carbon dioxide can directly liquefy and store the product gas meeting the pressure without adding a pressurizing device separately. And the present application reduces the desorption pressure of carbon dioxide by feeding the desorption gas into the desorption column 210.
In the foregoing embodiments, the descriptions of the embodiments are emphasized, and for parts of one embodiment that are not described in detail, reference may be made to related descriptions of other embodiments.
The foregoing has described in detail a gas trapping and storing system and method according to embodiments of the present application, and specific examples have been applied herein to illustrate the principles and embodiments of the present application, and the above description of the embodiments is only for aiding in understanding the method and core idea of the present application; meanwhile, as those skilled in the art will have variations in the specific embodiments and application scope in light of the ideas of the present application, the present description should not be construed as limiting the present application.
Claims (14)
1. A gas capture storage system, comprising:
an absorption unit (100), wherein the absorption unit (100) is provided with a first inlet (101) and a first outlet (102), carbon-containing flue gas is sent into the absorption unit (100) from the first inlet (101), the carbon-containing flue gas contains carbon dioxide, the carbon-containing flue gas contacts with absorption liquid in the absorption unit (100) to form a first solution, and the first solution is sent out from the first outlet (102);
a desorption unit (200), wherein the desorption unit (200) is provided with a second inlet (201), and the first solution sent out from the first outlet (102) is sent into the desorption unit (200) from the second inlet (201);
and a gas transfer unit (300), wherein the gas transfer unit (300) is used for feeding desorption gas into the desorption unit (200), the desorption gas contacts with the first solution to complete desorption of at least part of the carbon dioxide and form a second solution, and the second solution is fed into the absorption unit (100) from the desorption unit (200).
2. The gas capture storage system of claim 1, further comprising a circulation unit (400), the circulation unit (400) comprising a first circulation pump (401), an inlet of the first circulation pump (401) being in communication with the first outlet (102), an outlet of the first circulation pump (401) being in communication with the second inlet (201).
3. The gas capture storage system of claim 2, wherein the circulation unit (400) comprises a second circulation pump (402), the absorption unit (100) has a third inlet (103), the desorption unit (200) has a second outlet (202), the inlet of the second circulation pump (402) is in communication with the second outlet (202), and the outlet of the second circulation pump (402) is in communication with the third inlet (103).
4. A gas capture storage system according to claim 3, wherein the circulation unit (400) comprises a heat exchanger (403), the heat exchanger (403) being in communication with the outlet of the first circulation pump (401) and the outlet of the second circulation pump (402), respectively.
5. The gas capture storage system of claim 4, wherein the heat exchanger (403) has a first heat exchange outlet (4031), the first heat exchange outlet (4031) being in communication with the second inlet (201); the heat exchanger (403) has a second heat exchange outlet (4032), the second heat exchange outlet (4032) being in communication with the third inlet (103).
6. The gas capture storage system of claim 5, wherein the circulation unit (400) comprises a first heater (404), the first heater (404) being disposed between the first heat exchange outlet (4031) and the second inlet (201).
7. The gas capture storage system of claim 5, wherein the circulation unit (400) comprises a cooler (405), the cooler (405) being disposed between the second heat exchange outlet (4032) and the third inlet (103).
8. The gas capture storage system of claim 5, wherein the gas transfer unit (300) comprises a membrane separator (301), the desorption unit (200) having a third outlet (203), an inlet of the membrane separator (301) being in communication with the third outlet (203).
9. The gas capture storage system of claim 8, wherein the gas transfer unit (300) comprises a condenser (302), the condenser (302) being disposed between the membrane separator (301) and the third outlet (203).
10. The gas capture storage system of claim 8, wherein the gas transfer unit (300) comprises a second heater (303), the desorption unit (200) having a fourth inlet (204), the second heater (303) being disposed between the membrane separator (301) and the fourth inlet (204).
11. The gas trapping storage system according to claim 8, wherein the gas transfer unit (300) has a fifth inlet (304), the fifth inlet (304) being for feeding a desorption gas.
12. A gas trapping method, comprising:
the carbon-containing flue gas is sent into an absorption unit (100), an absorption liquid is arranged in the absorption unit (100), the carbon-containing flue gas comprises carbon dioxide, and a first solution is formed after the absorption liquid is contacted with the carbon-containing flue gas;
the first solution is sent to a desorption unit (200), and a gas conveying unit (300) sends desorption gas into the desorption unit (200) for desorbing carbon dioxide in the first solution;
the desorbed first solution forms a second solution, which is fed from the desorption unit (200) to the absorption unit (100).
13. The gas capturing method according to claim 12, wherein the absorption unit (100) has a first gas pressure in a pressure range of 0.8 to 1.2bar; and/or the number of the groups of groups,
the absorption unit (100) has a first temperature in the range of 30-40 ℃.
14. The gas trapping method according to claim 12, wherein the desorption unit (200) has a second gas pressure in a pressure range of 0.8 to 1.2bar; and/or the number of the groups of groups,
the desorption unit (200) has a second temperature in the range of 80-90 ℃.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101185825A (en) * | 2007-09-14 | 2008-05-28 | 江苏惠利特环保设备有限公司 | Oil gas recovery method and device using absorption method and membrane separating method integration technology |
| CN101830462A (en) * | 2010-06-03 | 2010-09-15 | 清华大学 | CO2 trapping method combining dimethyl carbonate absorption and membrane desorption |
| WO2015076859A1 (en) * | 2013-11-22 | 2015-05-28 | Eliot Gerber | Production of electric power from fossil fuel with almost zero air pollution |
| CN218637003U (en) * | 2022-10-31 | 2023-03-17 | 福建龙净环保股份有限公司 | Flue gas carbon dioxide capture system |
-
2023
- 2023-09-28 CN CN202311284358.7A patent/CN117180928A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101185825A (en) * | 2007-09-14 | 2008-05-28 | 江苏惠利特环保设备有限公司 | Oil gas recovery method and device using absorption method and membrane separating method integration technology |
| CN101830462A (en) * | 2010-06-03 | 2010-09-15 | 清华大学 | CO2 trapping method combining dimethyl carbonate absorption and membrane desorption |
| WO2015076859A1 (en) * | 2013-11-22 | 2015-05-28 | Eliot Gerber | Production of electric power from fossil fuel with almost zero air pollution |
| CN218637003U (en) * | 2022-10-31 | 2023-03-17 | 福建龙净环保股份有限公司 | Flue gas carbon dioxide capture system |
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