CN216604643U - Large scale CO capture2Device - Google Patents
Large scale CO capture2Device Download PDFInfo
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- CN216604643U CN216604643U CN202121367753.8U CN202121367753U CN216604643U CN 216604643 U CN216604643 U CN 216604643U CN 202121367753 U CN202121367753 U CN 202121367753U CN 216604643 U CN216604643 U CN 216604643U
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- 238000000034 method Methods 0.000 claims abstract description 82
- 238000003795 desorption Methods 0.000 claims abstract description 79
- 239000003463 adsorbent Substances 0.000 claims abstract description 44
- 238000001179 sorption measurement Methods 0.000 claims abstract description 32
- 238000001816 cooling Methods 0.000 claims abstract description 31
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 73
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 9
- 239000002826 coolant Substances 0.000 description 7
- 239000002808 molecular sieve Substances 0.000 description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- 238000007599 discharging Methods 0.000 description 4
- 239000003546 flue gas Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 3
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- 239000012621 metal-organic framework Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- VILCJCGEZXAXTO-UHFFFAOYSA-N 2,2,2-tetramine Chemical compound NCCNCCNCCN VILCJCGEZXAXTO-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229920002873 Polyethylenimine Polymers 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 238000010170 biological method Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- FAGUFWYHJQFNRV-UHFFFAOYSA-N tetraethylenepentamine Chemical compound NCCNCCNCCNCCN FAGUFWYHJQFNRV-UHFFFAOYSA-N 0.000 description 1
- 229960001124 trientine Drugs 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
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- 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
Abstract
The utility model relates to CO2The technical field of desorption, in particular to large-scale CO capture2Provided is a device. The device comprises: the control unit, the gas inlet pipeline unit, the gas outlet pipeline unit and the adsorbent are used for realizing CO (carbon monoxide) by setting first set time, second set time and third set time2The adsorption, desorption and cooling are carried out in the same desorption tower in the trapping process, and the CO can be obviously improved2Capture efficiency, accelerate CO2Capture process rate to achieve large scale CO2Trapping; in addition, the device can realize' adsorption-desorption-Circulation of the cooling process to achieve large scale CO removal2。
Description
Technical Field
The utility model relates to CO2The technical field of desorption, in particular to large-scale CO capture2Provided is a device.
Background
CO2The trapping and separating method is a research hotspot which is widely concerned in the world at present, and various new technologies are continuously proposed and developed; at present, CO2The trapping and separating method mainly comprises a liquid solvent absorption method, an adsorption method, a biological method, a membrane separation method, a low-temperature freezing method and the like, and the adsorption method is a good emission reduction technology due to low energy consumption, small pollution, easy automation and the like.
CN107485960A discloses an amine solid adsorbent for removing CO in flue gas2The device comprises reactors (1-a, 1-b), a water saturator (2), a gas-solid separator (3), a cooler (4), a vacuum pump (5-a, 5-b) and a water washing tank (6); wherein, the reactor (1-a) is connected with the reactor (1-b) in parallel, the flue gas to be treated passes through the water saturator (2) and then is connected with the upper part of the reactor (1-a, 1-b), the lower part of the reactor (1-a, 1-b) is connected with the gas-solid separator (3), and the treated purified gas is emptied after passing through the lower part of the reactor (1-a, 1-b) and the gas-solid separator (3); the upper parts of the reactors (1-a, 1-b) are connected with vacuum pumps (5-a, 5-b), the vacuum pumps (5-a) and the vacuum pumps (5-b) are connected in parallel, outlets of the vacuum pumps (5-a, 5-b) are connected with a cooler (4), and the cooler (4) is connected with a water washing tank (6). CO in the device2The adsorption and the regeneration are carried out in the same reactor, thereby simplifying the device; however, the reactor in this apparatus is a conventional fixed bed, and CO is present in the flue gas2In the adsorption process, the operation is complex, the efficiency is low, and the device is seriously limited to large-scale CO2And (4) application in trapping.
CN108339371A discloses a method for continuously adsorbing CO2The apparatus of (1), the apparatus comprising: the device comprises an adsorption device, a screening device, a lifter and a gas-liquid separator; the adsorption device comprises a moving bed adsorber and mainly comprises an adsorption section, a desorption section and a cooling section. The device realizes CO2AdsorptionThe apparatus imposes higher demands on the adsorbent, requires the adsorbent to have a low density, and is difficult to use for large-scale CO due to the influence of the gravity of the adsorbent itself2And (4) trapping.
Therefore, there is a need for a method for large scale CO capture2The apparatus of (1).
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome the defect of CO capture by the existing adsorption method2In the process, due to multiple restrictions of the adsorbent, the trapping device and the trapping process, the CO is difficult to be trapped on a large scale2To provide a large scale CO capture2Device for the realization of CO2Capture of concentrated CO2Adsorption, CO2The desorption/adsorbent regeneration and the adsorbent cooling are carried out in the same desorption tower, which can obviously improve CO2Capture efficiency, accelerate CO2Capture process rate, large scale CO realization2Trapping; meanwhile, the device reduces the number of adsorption towers in the trapping process and reduces the fixed investment.
In order to achieve the above object, the present invention provides a method for large scale CO capture2An apparatus, the apparatus comprising: the device comprises a desorption tower filled with an adsorbent, a control unit, and an air inlet pipeline unit and an air outlet pipeline unit which are respectively arranged at an air inlet end and an air outlet end of the desorption tower; the air inlet pipeline unit comprises a first air inlet pipeline, a second air inlet pipeline and a third air inlet pipeline, and the air outlet pipeline unit comprises a first air outlet pipeline, a second air outlet pipeline and a third air outlet pipeline;
wherein, the control unit with desorption tower, inlet air duct unit and outlet air duct unit are connected respectively for:
A. setting a first set time to enable the desorption tower to be in an adsorption process;
B. after the adsorption process is kept for the first set time, setting a second set time to enable the desorption tower to be in a desorption process;
C. after the desorption process is kept for the second set time, setting a third set time to enable the desorption tower to be in a cooling process;
D. repeating A-C after the cooling process is kept for a third set time to realize large-scale CO capture2。
Preferably, the first air inlet pipeline, the second air inlet pipeline and the third air inlet pipeline are respectively provided with a first air inlet valve, a second air inlet valve and a third air inlet valve; and the first air outlet pipeline, the second air outlet pipeline and the third air outlet pipeline are respectively provided with a first air outlet valve, a second air outlet valve and a third air outlet valve.
Preferably, the first intake valve and the first exhaust valve have a first operating condition and a first closed condition; and/or the second intake valve and the second exhaust valve have a second operating state and a second closed state; and/or the third inlet valve and the third outlet valve have a third working state and a third closing state.
Preferably, the first air inlet valve and the first air outlet valve are linked; and/or the second air inlet valve is linked with the second air outlet valve; and/or the third air inlet valve and the third air outlet valve are linked.
Preferably, when the first air inlet valve and the first air outlet valve are in the first working state, the second air inlet valve and the second air outlet valve are in the second closing state, the third air inlet valve and the third air outlet valve are in the third closing state, and the original CO-containing state is set2The mixed gas enters the desorption tower through the first gas inlet pipeline, and the adsorbent adsorbs the original CO2CO in mixed gas2And discharging the obtained net removal gas through the first gas outlet pipeline.
Preferably, in the adsorption process, the first set time is set to be 3-300 min.
Preferably, when the second inlet valve and the second outlet valve are in the second working state, the first inlet valve and the first outlet valve are in the first closed state, the third inlet valve and the third outlet valve are in the third closed state, and the high-temperature high-concentration CO is set2Gas enters the removing tower through the second gas inlet pipeline and enters the removing towerAdsorb CO2The adsorbent is desorbed to obtain CO-rich gas2And gas is discharged through the second gas outlet pipeline.
Preferably, in the desorption process, the second set time is set to be 3-300 min.
Preferably, when the third air inlet valve and the third air outlet valve are in the third working state, the first air inlet valve and the first air outlet valve are in the first closed state, the second air inlet valve and the second air outlet valve are in the second closed state, and a cooling medium is set to enter the desorption tower through the third air inlet pipeline to desorb CO2And cooling the adsorbent to obtain cooled tail gas, and discharging the cooled tail gas through the third gas outlet pipeline.
Preferably, in the cooling process, the third set time is set to 3-300 min.
According to the technical scheme, the device comprising the control unit, the air inlet pipeline unit and the air outlet pipeline unit and the adsorbent are adopted, and the CO is realized by setting the first set time, the second set time and the third set time2The adsorption, desorption and cooling are carried out in the same desorption tower in the trapping process, and the CO can be obviously improved2Capture efficiency, accelerate CO2Capture process rate to achieve large scale CO2Trapping; in addition, the device can realize the circulation of the process of 'adsorption-desorption-cooling' through the control unit, thereby realizing the large-scale removal of CO2。
Meanwhile, the device simplifies the device and equipment and reduces the fixed investment.
Drawings
FIG. 1 is a large scale CO capture system provided by the present invention2Schematic illustration of the apparatus.
Description of the reference numerals
I. A removing tower II, a control unit III-1 and a first air inlet pipeline
III-2, a second air inlet pipeline III-3, a third air inlet pipeline IV-1 and a first air outlet pipeline
IV-2, a second air outlet pipeline IV-3, a third air outlet pipeline 1 and a first air inlet valve
1 ', a first air outlet valve 2, a second air inlet valve 2', a second air outlet valve
3. Third air inlet valve 3' and third air outlet valve
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
In the present invention, unless otherwise specified, the terms "first", "second", and "third" do not indicate a sequential order, nor do they indicate a limitation on each material or step, but merely distinguish the materials or steps, for example, the terms "first", "second", and "third" in the "first intake duct", "second intake duct", and "third intake duct" are merely used to distinguish that these are not the same intake duct.
The utility model provides a method for large-scale CO capture2Apparatus, as shown in figure 1, comprising: the device comprises a desorption tower I filled with an adsorbent, a control unit II, and an air inlet pipeline unit and an air outlet pipeline unit which are respectively arranged at an air inlet end and an air outlet end of the desorption tower; the air inlet pipeline unit comprises a first air inlet pipeline III-1, a second air inlet pipeline III-2 and a third air inlet pipeline III-3, and the air outlet pipeline unit comprises a first air outlet pipeline IV-1, a second air outlet pipeline IV-2 and a third air outlet pipeline IV-3;
wherein, the control unit II with desorption tower I, inlet duct unit and outlet duct unit are connected respectively for:
A. setting a first set time to enable the desorption tower I to be in an adsorption process;
B. after the adsorption process is kept for the first set time, setting a second set time to enable the desorption tower I to be in a desorption process;
C. after the desorption process is kept for the second set time, setting a third set time to enable the desorption tower I to be in a cooling process;
D. repeating A-C after the cooling process is kept for a third set time to realize large-scale CO capture2。
In the present invention, there is a wide selection range of the kind of the adsorbent without any special description, and the present invention is not described in detail herein.
In one embodiment of the present invention, the adsorbent is selected from at least one of a carbon-based honeycomb-based adsorbent, an amino honeycomb-based adsorbent, a molecular sieve-based honeycomb adsorbent, and a metal oxide-based honeycomb adsorbent; further preferably, the carbon-based honeycomb adsorbent is selected from porous honeycomb activated carbon including but not limited to coal honeycomb activated carbon, wood honeycomb activated carbon; the molecular sieve based honeycomb adsorbent is selected from at least one of a 3A molecular sieve, a 4A molecular sieve, a 5A molecular sieve and a 13X molecular sieve; the metal oxide-based honeycomb adsorbent is selected from alumina honeycomb adsorbents and/or metal organic framework honeycomb adsorbents (MOFs); the amino honeycomb adsorbent is selected from porous honeycomb solid organic amines, including but not limited to ethanolamine, diethanolamine, triethylene tetramine, tetraethylene pentamine and polyethyleneimine.
In the utility model, the gas inlet end and the gas outlet end of the removal tower are respectively and independently determined by the gas inlet and outlet directions; when gas enters from bottom to top, the gas inlet end of the removal tower is the bottom of the removal tower, and the gas outlet end of the removal tower is the top of the removal tower; when the gas goes up and down, the gas inlet end of the removal tower is the top of the removal tower, and the gas outlet end of the removal tower is the bottom of the removal tower.
In the present invention, without a special description, the connection of the control unit with the desorption tower, the gas inlet pipeline unit, and the gas outlet pipeline unit means that one end of the control unit is connected with the first gas inlet pipeline, the second gas inlet pipeline, and the third gas inlet pipeline, respectively, the other end of the control unit is connected with the first gas outlet pipeline, the second gas outlet pipeline, and the third gas outlet pipeline, respectively, the control unit is further connected with the desorption tower, and preferably, the control unit is further connected with the middle portion of the desorption tower.
According to the present invention, preferably, the first air intake pipeline III-1, the second air intake pipeline III-2 and the third air intake pipeline III-3 are respectively provided with a first air intake valve 1, a second air intake valve 2 and a third air intake valve 3; and the first air outlet pipeline IV-1, the second air outlet pipeline IV-2 and the third air outlet pipeline IV-3 are respectively provided with a first air outlet valve 1 ', a second air outlet valve 2 ' and a third air outlet valve 3 '.
According to the utility model, preferably, said first intake valve and 1 first outlet valve 1' have a first operating condition and a first closed condition; and/or the second intake valve 2 and the second outlet valve 2' have a second operating condition and a second closed condition; and/or the third inlet valve 3 and the third outlet valve 3' have a third operating state and a third closed state.
In the present invention, the first operating state, the second operating state, and the third operating state are each independently an open state, unless otherwise specified.
According to the utility model, preferably, the first intake valve 1 and the first outlet valve 1' are linked; and/or the second air inlet valve 2 and the second air outlet valve 2' are linked; and/or the third air inlet valve 3 and the third air outlet valve 3' are linked.
According to the present invention, preferably, when the first intake valve 1 and the first exhaust valve 1 ' are in the first working state, the second intake valve 2 and the second exhaust valve 2 ' are in the second closed state, the third intake valve 3 and the third exhaust valve 3 ' are in the third closed state, and the original CO content is set2The mixed gas enters the desorption tower I through the first gas inlet pipeline III-1, and the adsorbent adsorbs the original CO2CO in mixed gas2And the obtained net removal gas is discharged through the first gas outlet pipeline IV-1.
In the present invention, the raw material contains CO without specific description2The mixed gas mainly contains CO2、N2、O2、H2O。
In the present invention, preferably, the raw material contains CO2CO in mixed gas2A concentration of 4 to 60 volume percent, e.g., 4 volume percent, 10 volume percent, 15 volume percent, 20 volume percent, 25 volume percent, 30 volume percent, 35 volume percent, 40 volume percent, 45 volume percent, 50 volume percent, 55 volume percent, and 60 volume percent, and any value in a range consisting of any two values; the original contains CO2The temperature of the mixed gas is 20 to 50 ℃, for example, 20 ℃, 25 ℃, 30 ℃, 35 ℃, 40 ℃, 45 ℃ and 50 ℃, and any value in the range of any two values.
In the present invention, unless otherwise specified, the fact that the removal column is in the adsorption process means that the adsorbent in the removal column is in the adsorption process.
In the present invention, in the adsorption process, the first set time is set to be 3 to 300min, for example, 3min, 5min, 10min, 15min, 20min, 30min, 50min, 100min, 150min, 200min, 250min, 300min, and any value in a range of any two values, preferably 5 to 30 min. That is, the desorption column is in the adsorption process for the first set time.
According to an embodiment of the present invention, when the first intake valve 1 and the first exhaust valve 1 ' are in the first working state, the second intake valve 2 and the second exhaust valve 2 ' are in the second closed state, the third intake valve 3 and the third exhaust valve 3 ' are in the third closed state, and the original CO is set2The mixed gas enters the desorption tower I through the first gas inlet pipeline III-1, and the adsorbent adsorbs the original CO2CO in mixed gas2The obtained net removal gas is discharged through the first gas outlet pipeline IV-1; in the adsorption process, setting the first set time to be 3-300min, preferably 5-30min, so that the desorption tower I is in the adsorption process; in thatAnd after the adsorption process is kept for the first set time, setting a second set time to enable the desorption tower to be in a desorption process.
According to the present invention, preferably, when the second intake valve 2 and the second exhaust valve 2 ' are in the second working state, the first intake valve 1 and the first exhaust valve 1 ' are in the first closed state, the third intake valve 3 and the third exhaust valve 3 ' are in the third closed state, and the high-temperature high-concentration CO is set2The gas enters the desorption tower I through the second gas inlet pipeline III-2 and adsorbs CO2The adsorbent is desorbed to obtain CO-rich gas2The gas is discharged through the second gas outlet pipeline IV-2.
In the utility model, in the removing tower, high-temperature high-concentration CO is added2Gas and adsorbed CO2So that CO adsorbed in the adsorbent is brought into contact with the adsorbent2Heated for desorption to obtain CO-rich2Gas and regenerated adsorbent.
According to the present invention, preferably, the high temperature and high concentration CO2The temperature of the gas is 80-240 ℃, e.g., 80 ℃, 90 ℃, 100 ℃, 120 ℃, 150 ℃, 180 ℃, 200 ℃, 220 ℃ and 240 ℃, and any value in the range of any two values; the high-temperature high-concentration CO2CO in gas2The concentration is 80-100% by volume, for example, 80%, 83%, 85%, 87%, 90%, 93%, 95%, 97%, and 100% by volume, and any value in the range of any two numerical values.
In the present invention, unless otherwise specified, the fact that the removal column is in the desorption process means that the adsorbent in the removal column is in the desorption process.
In the present invention, preferably, in the desorption process, the second set time is set to be 3 to 300min, for example, 3min, 5min, 10min, 15min, 20min, 30min, 50min, 100min, 150min, 200min, 250min, 300min, and any value in a range of any two values, preferably 3 to 30 min. That is, the desorption column is in the desorption process for the second set time.
According to an embodiment of the present invention, when the second intake valve 2 and the second exhaust valve 2 ' are in the second working state, the first intake valve 1 and the first exhaust valve 1 ' are in the first closed state, the third intake valve 3 and the third exhaust valve 3 ' are in the third closed state, and the high-temperature high-concentration CO is set2The gas enters the desorption tower I through the second gas inlet pipeline III-2 and adsorbs CO2The adsorbent is desorbed to obtain CO-rich gas2Gas is discharged through the second gas outlet pipeline IV-2; in the desorption process, setting the second set time to be 3-300min, preferably 3-30min, so that the desorption tower is in the desorption process; and after the desorption process is kept for the second set time, setting a third set time to enable the desorption tower to be in a cooling process.
According to the present invention, preferably, when the third air intake valve 3 and the third air outlet valve 3 ' are in the third working state, the first air intake valve 1 and the first air outlet valve 1 ' are in the first closed state, the second air intake valve 2 and the second air outlet valve 2 ' are in the second closed state, and the cooling medium is set to enter the desorption tower I through the third air intake pipe III-3, so as to desorb CO2And cooling the adsorbent to obtain cooled tail gas, and discharging the cooled tail gas through the third gas outlet pipeline IV-3.
According to the present invention, it is preferable that the temperature of the cooling medium is 10 to 30 ℃, for example, 10 ℃, 15 ℃, 20 ℃, 25 ℃ and 30 ℃, and any value in the range of any two numerical values.
In the present invention, there is a wide range of choices for the kind of the cooling medium. Preferably, the cooling medium is selected from air and/or an inert gas, preferably air.
In the present invention, unless otherwise specified, the fact that the removal column I is in a cooling process means that the adsorbent in the removal column I is in a cooling process.
In the present invention, it is preferable that the third set time is set to 3 to 300min, for example, 3min, 5min, 10min, 15min, 20min, 30min, 50min, 100min, 150min, 200min, 250min, 300min, and any value in a range of any two numerical values, preferably 3 to 30min, in the cooling process. That is, the removal column is in a cooling process for a third set time.
According to a specific embodiment of the present invention, when the third air intake valve 3 and the third air outlet valve 3 ' are in the third operating state, the first air intake valve 1 and the first air outlet valve 1 ' are in the first closed state, the second air intake valve 2 and the second air outlet valve 2 ' are in the second closed state, and the cooling medium is set to enter the desorption tower I through the third air intake pipe III-3, so as to desorb CO2Cooling the adsorbent to obtain cooled tail gas, and discharging the cooled tail gas through the third gas outlet pipeline IV-3; in the cooling process, setting the third set time to be 3-300min, preferably 3-30min, so that the removal tower is in the cooling process; after the cooling process is kept for the third set time, the first set time is set, and a new round of CO trapping is started2。
The following description of the large scale CO capture in conjunction with the schematic of the apparatus of FIG. 1 provided by the present invention2。
As shown in fig. 1, the apparatus includes: the device comprises a desorption tower I filled with an adsorbent, a control unit II, and an air inlet pipeline unit and an air outlet pipeline unit which are respectively arranged at an air inlet end and an air outlet end of the desorption tower; the air inlet pipeline unit comprises a first air inlet pipeline III-1, a second air inlet pipeline III-2 and a third air inlet pipeline III-3, and the air outlet pipeline unit comprises a first air outlet pipeline IV-1, a second air outlet pipeline IV-2 and a third air outlet pipeline IV-3; the control unit II is respectively connected with the desorption tower I, the gas inlet pipeline unit and the gas outlet pipeline unit;
a first air inlet valve 1, a second air inlet valve 2 and a third air inlet valve 3 are respectively arranged on the first air inlet pipeline III-1, the second air inlet pipeline III-2 and the third air inlet pipeline III-3; and the first air outlet pipeline IV-1, the second air outlet pipeline IV-2 and the third air outlet pipeline IV-3 are respectively provided with a first air outlet valve 1 ', a second air outlet valve 2 ' and a third air outlet valve 3 '.
A. When the first air inlet valve 1 and the first air outlet valve 1 ' are in the first working state, the second air inlet valve 2 and the second air outlet valve 2 ' are in the second closing state, the third air inlet valve 3 and the third air outlet valve 3 ' are in the third closing state, and the original CO content is set2Mixed gas (temperature 40 ℃; CO)2The concentration is 15 vol%) enters the desorption tower I through the first air inlet pipeline III-1, and the carbon-based honeycomb adsorbent adsorbs CO in the raw flue gas2The obtained net removal gas is discharged through the first gas outlet pipeline IV-1; in the adsorption process, setting a first set time to be 10min so that the desorption tower is in the adsorption process; after the adsorption process is kept for 10min for the first set time, setting a second set time to enable the desorption tower to be in a desorption process;
B. when the second air inlet valve 2 and the second air outlet valve 2 ' are in the second working state, the first air inlet valve 1 and the first air outlet valve 1 ' are in the first closing state, the third air inlet valve 3 and the third air outlet valve 3 ' are in the third closing state, and high-temperature and high-concentration CO is set2Gas (temperature 150 ℃ C.; CO)2The concentration was 95% by volume; ) Enters the desorption tower I through the second gas inlet pipeline III-2 and adsorbs CO2The obtained adsorbent is desorbed to obtain CO rich2Gas is discharged through the second gas outlet pipeline IV-2; in the desorption process, setting the second set time to be 15min, so that the desorption tower is in the desorption process; after the desorption process is kept for 15min, setting a third set time to enable the desorption tower to be in a cooling process;
C. when the third air inlet valve 3 and the third air outlet valve 3 ' are in the third working state, the first air inlet valve 1 and the first air outlet valve 1 ' are in the first closed state, the second air inlet valve 2 and the second air outlet valve 2 ' are in the second closed state, a cooling medium (air with the temperature of 15 ℃) is arranged to enter the desorption tower I through the third air inlet pipeline III-3, and CO is desorbed2Cooling the adsorbent to obtain cooled tail gasThe third air outlet pipeline IV-3 discharges; in the cooling process, setting the third set time to be 20min so that the removal tower is in the cooling process; after the cooling process is kept for the third set time for 20min, resetting the first set time to enable the desorption tower to be in the adsorption process;
D. repeating the steps A-C to realize large-scale CO capture2。
The device provided by the utility model realizes CO by setting the first set time, the second set time and the third set time through the control unit2In the trapping process, adsorption, desorption and cooling are carried out in the same desorption tower, and then the adsorbent filled in the desorption tower is combined, so that the CO is further improved2Capture efficiency, accelerate CO2Capture process rate to achieve large scale CO2Trapping; meanwhile, the device simplifies the device and equipment and reduces the fixed investment.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the utility model, many simple modifications can be made to the technical solution of the utility model, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the utility model, and all fall within the scope of the utility model.
Claims (7)
1. Large-scale CO capture2An apparatus, characterized in that the apparatus comprises: the device comprises a desorption tower filled with an adsorbent, a control unit, and an air inlet pipeline unit and an air outlet pipeline unit which are respectively arranged at an air inlet end and an air outlet end of the desorption tower; the air inlet pipeline unit comprises a first air inlet pipeline, a second air inlet pipeline and a third air inlet pipeline, and the air outlet pipeline unit comprises a first air outlet pipeline, a second air outlet pipeline and a third air outlet pipeline;
the control unit is respectively connected with the desorption tower, the gas inlet pipeline unit and the gas outlet pipeline unit and can be controlled to carry out an adsorption process, a desorption process and a cooling process in the same desorption tower;
the first air inlet pipeline, the second air inlet pipeline and the third air inlet pipeline are respectively provided with a first air inlet valve, a second air inlet valve and a third air inlet valve; a first air outlet valve, a second air outlet valve and a third air outlet valve are respectively arranged on the first air outlet pipeline, the second air outlet pipeline and the third air outlet pipeline;
the first intake valve and the first exhaust valve have a first operating state and a first closed state; the second intake valve and the second exhaust valve have a second working state and a second closed state; the third air inlet valve and the third air outlet valve have a third working state and a third closing state;
the first air inlet valve is linked with the first air outlet valve; the second air inlet valve is linked with the second air outlet valve; and the third air inlet valve is linked with the third air outlet valve.
2. The apparatus according to claim 1, wherein when the first inlet valve and the first outlet valve are in the first operating state, the second inlet valve and the second outlet valve are in the second closed state, the third inlet valve and the third outlet valve are in the third closed state, and the control unit controls to perform the adsorption process in the desorption tower.
3. The apparatus according to claim 1 or 2, wherein the first set time is set to 3-300min during the adsorption process.
4. The apparatus according to claim 1, wherein when the second inlet valve and the second outlet valve are in the second operating state, the first inlet valve and the first outlet valve are in the first closed state, the third inlet valve and the third outlet valve are in the third closed state, and the control unit controls the desorption process in the desorption tower.
5. The apparatus according to claim 1 or 2, wherein a second set time is set to 3-300min during the desorption.
6. The apparatus according to claim 1, wherein when the third inlet valve and the third outlet valve are in the third operating state, the first inlet valve and the first outlet valve are in the first closed state, the second inlet valve and the second outlet valve are in the second closed state, and the control unit controls the cooling process to be performed in the rejection column.
7. The apparatus according to claim 1 or 2, wherein a third set time is set to 3-300min during the cooling process.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121367753.8U CN216604643U (en) | 2021-06-18 | 2021-06-18 | Large scale CO capture2Device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121367753.8U CN216604643U (en) | 2021-06-18 | 2021-06-18 | Large scale CO capture2Device |
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| CN216604643U true CN216604643U (en) | 2022-05-27 |
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