CN114669167A - Pressure swing adsorption and desorption gas recycling device - Google Patents
Pressure swing adsorption and desorption gas recycling device Download PDFInfo
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- CN114669167A CN114669167A CN202210141163.6A CN202210141163A CN114669167A CN 114669167 A CN114669167 A CN 114669167A CN 202210141163 A CN202210141163 A CN 202210141163A CN 114669167 A CN114669167 A CN 114669167A
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- 238000001179 sorption measurement Methods 0.000 title claims abstract description 42
- 238000003795 desorption Methods 0.000 title claims abstract description 16
- 238000004064 recycling Methods 0.000 title claims abstract description 11
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 196
- 239000007788 liquid Substances 0.000 claims abstract description 115
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 98
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 97
- 150000001412 amines Chemical class 0.000 claims abstract description 71
- 230000008929 regeneration Effects 0.000 claims abstract description 63
- 238000011069 regeneration method Methods 0.000 claims abstract description 63
- 230000018044 dehydration Effects 0.000 claims abstract description 43
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 43
- 238000010521 absorption reaction Methods 0.000 claims abstract description 42
- 238000001816 cooling Methods 0.000 claims abstract description 24
- 239000012535 impurity Substances 0.000 claims abstract description 14
- 238000002336 sorption--desorption measurement Methods 0.000 claims abstract description 13
- 238000010992 reflux Methods 0.000 claims description 7
- 239000012024 dehydrating agents Substances 0.000 claims description 3
- 238000004868 gas analysis Methods 0.000 claims 2
- 238000000034 method Methods 0.000 abstract description 7
- 239000002699 waste material Substances 0.000 abstract description 4
- 238000003912 environmental pollution Methods 0.000 abstract description 3
- 238000001035 drying Methods 0.000 abstract description 2
- VKYKSIONXSXAKP-UHFFFAOYSA-N hexamethylenetetramine Chemical compound C1N(C2)CN3CN1CN2C3 VKYKSIONXSXAKP-UHFFFAOYSA-N 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 118
- 238000011084 recovery Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 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
- 239000003245 coal Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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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
- B01D53/14—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 absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
-
- 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
- B01D53/14—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 absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- 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
- B01D53/14—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 absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- 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
- B01D53/14—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 absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
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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
- B01D53/26—Drying gases or vapours
- B01D53/265—Drying gases or vapours by refrigeration (condensation)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/22—Carbon dioxide
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- Gas Separation By Absorption (AREA)
Abstract
The invention relates to a pressure swing adsorption desorption gas recycling device, which comprises an absorption system, a regeneration system, a cooling pressurization system, a dehydration system and a rectification system, wherein the absorption system is used for dissolving carbon dioxide in input desorption gas in lean amine liquid to form amine-rich liquid and separating the amine-rich liquid to obtain combustible gas; the regeneration system is used for enabling the rich amine liquid to be in contact with the vaporized lean amine liquid to obtain lean amine liquid and gas with high carbon dioxide content, and sending the lean amine liquid back to the absorption system; the cooling and pressurizing system is used for cooling and pressurizing the gas with high carbon dioxide content into high-pressure low-temperature gas; the dehydration system is used for removing moisture in the high-pressure low-temperature gas to obtain dry carbon dioxide gas; the rectification system is used for rectifying and drying the carbon dioxide gas to obtain food-grade carbon dioxide, high-purity carbon dioxide and impurity gas. The invention can process the pressure swing adsorption and desorption gas to realize recycling, thereby reducing environmental pollution and resource waste.
Description
Technical Field
The invention relates to the technical field of gas recovery and treatment, in particular to a pressure swing adsorption desorption gas recycling device.
Background
When pressure swing adsorption is adopted to purify hydrogen in the process of preparing hydrogen by coal gasification, the analysis gas contains a large amount of combustible gas and carbon dioxide, and if the gas is directly discharged, the environment pollution and the resource waste are caused, so that the pressure swing adsorption analysis gas needs to be recycled.
Disclosure of Invention
The invention aims to provide a pressure swing adsorption desorption gas recycling device which can reduce environmental pollution and resource waste.
In order to achieve the purpose, the invention adopts the technical scheme that:
a pressure swing adsorption analytic gas recycle device is used for processing analytic gas used in a pressure swing adsorption process, and the pressure swing adsorption analytic gas recycle device comprises:
an absorption system for dissolving carbon dioxide in the input decomposed gas in an amine-poor liquid to form an amine-rich liquid and separating the amine-rich liquid to obtain combustible gas;
a regeneration system connected to the absorption system for contacting the amine-rich liquid with the vaporized amine-lean liquid to obtain an amine-lean liquid and a gas with a high carbon dioxide content, and returning the amine-lean liquid to the absorption system;
the cooling pressurization system is connected with the regeneration system and is used for cooling and pressurizing the gas with high carbon dioxide content into high-pressure low-temperature gas;
The dehydration system is connected with the cooling pressurization system and is used for removing moisture in the high-pressure low-temperature gas to obtain dry carbon dioxide gas;
and the rectification system is connected with the dehydration system and is used for rectifying the dry carbon dioxide gas to obtain food-grade carbon dioxide, high-purity carbon dioxide and impurity gas.
The absorption system comprises an absorption tower, the absorption tower is provided with a desorption gas inlet, a lean amine liquid inlet, a combustible gas outlet and an amine-rich liquid outlet, the desorption gas is input into the absorption tower through the desorption gas inlet, the lean amine liquid inlet is connected with the regeneration system, the combustible gas outlet outputs the combustible gas, and the amine-rich liquid outlet is connected with the regeneration system.
And the rich amine liquid outlet is connected with the regeneration system through a rich liquid pump and an amine liquid heat exchanger.
The regeneration system comprises a regeneration tower and a regeneration tower evaporator arranged at the lower part of the regeneration tower, the regeneration tower is provided with an amine-rich liquid inlet, an amine-poor liquid outlet, a vaporized amine-poor liquid inlet and a high-carbon-dioxide-content gas outlet, the absorption system is connected with the amine-rich liquid inlet, the amine-poor liquid outlet is connected with the vaporized amine-poor liquid inlet through the regeneration tower evaporator, the amine-poor liquid outlet is connected with the absorption system through an amine liquid heat exchanger, a amine liquid pump and an amine liquid cooler, and the high-carbon-dioxide-content gas outlet is connected with the cooling pressurization system.
The regeneration tower evaporator is connected with a steam source to obtain steam as a heat source.
The cooling pressurization system comprises a carbon dioxide cooler, a carbon dioxide compressor and a normal-temperature precooler which are sequentially connected.
The dehydration system comprises a dehydration adsorption cylinder which is alternately switched to carry out adsorption and regeneration, the dehydration adsorption cylinder is provided with a high-pressure low-temperature gas inlet and a dry carbon dioxide gas outlet, the high-pressure low-temperature gas inlet is connected with the cooling pressurization system, the dry carbon dioxide gas outlet is connected with the rectification system, and an adsorption dehydrating agent is arranged in the dehydration adsorption cylinder.
The dehydration system further comprises a heater, the dehydration adsorption cylinder is further provided with a regeneration gas inlet, and a regeneration gas source is connected to the regeneration gas inlet through the heater.
The rectifying system comprises a first rectifying tower, a first rectifying tower reboiler arranged at the bottom of the first rectifying tower, a second rectifying tower and a second rectifying tower reboiler arranged at the bottom of the second rectifying tower, wherein the first rectifying tower is provided with a liquid inlet, a carbon dioxide gas outlet and an impurity gas outlet, the second rectifying tower is provided with a gas inlet, a high-purity carbon dioxide outlet and a carbon dioxide gas outlet, and the first rectifying tower reboiler and the second rectifying tower reboiler are respectively provided with a gas inlet and a liquid outlet; the gas inlet of the first rectifying tower reboiler and the gas inlet of the second rectifying tower reboiler are both connected with the dehydration system, the liquid outlet of the first rectifying tower reboiler and the liquid outlet of the second rectifying tower reboiler are both connected with the liquid inlet of the first rectifying tower, the impurity gas is output from the impurity gas outlet of the first rectifying tower to the first rectifying tower, the food grade carbon dioxide is output to the first rectifying tower through a carbon dioxide gas outlet of the first rectifying tower, the carbon dioxide gas outlet of the first rectifying tower is connected with the gas inlet of the second rectifying tower, the food grade carbon dioxide is output from the second rectifying tower through the carbon dioxide gas outlet of the second rectifying tower, and the high-purity carbon dioxide is output from the second rectifying tower through a high-purity carbon dioxide outlet of the second rectifying tower.
The dehydration system is connected to a gas inlet of the first rectifying tower reboiler and a gas inlet of the second rectifying tower reboiler after passing through a first low-temperature precooler; the carbon dioxide gas outlet of the first rectifying tower is connected with the gas inlet of the second rectifying tower through a second low-temperature precooler; the second rectifying tower is also provided with a reflux inlet, and one branch branched from the carbon dioxide gas outlet of the second rectifying tower is connected to the reflux inlet through a third low-temperature precooler. .
Due to the application of the technical scheme, compared with the prior art, the invention has the following advantages: the invention can process the pressure swing adsorption desorption gas to realize recycling, thereby reducing environmental pollution and resource waste.
Drawings
FIG. 1 is a schematic view of a pressure swing adsorption desorption gas recycling apparatus according to the present invention.
In the above drawings: 1. an absorption tower; 2. an amine liquid cooler; 3. a barren liquor pump; 4. an amine liquid heat exchanger; 5. a regeneration tower; 6. a carbon dioxide cooler; 7. a carbon dioxide compressor; 8. a normal temperature precooler; 9. a rich liquor pump; 10. a regeneration tower evaporator; 11. a first dehydration adsorption cylinder; 12. a second dehydration adsorption cylinder; 13. an electric heater; 14. a first low-temperature precooler; 15. a first rectification column; 16. a first rectifier reboiler; 17. a second low-temperature precooler; 18. a second rectification column; 19. a second rectification column reboiler; 20. and a third low-temperature precooler.
Detailed Description
The invention will be further described with reference to examples of embodiments shown in the drawings to which the invention is attached.
The first embodiment is as follows: as shown in fig. 1, a pressure swing adsorption (psa) gas recovery and utilization apparatus includes an absorption system, a regeneration system, a cooling and pressurizing system, a dehydration system and a rectification system, wherein the regeneration system is connected to the absorption system, the cooling and pressurizing system is connected to the regeneration system, the dehydration system is connected to the cooling and pressurizing system, and the rectification system is connected to the dehydration system.
The absorption system is used for dissolving carbon dioxide in input desorption gas in lean amine liquid (the lean amine liquid is an aqueous solution containing MDEA with the mass fraction of 40% and DEA with the mass fraction of 1% -5%) to form rich amine liquid (the rich amine liquid is an aqueous solution formed by absorbing CO2 by the lean amine liquid), and separating to obtain combustible gas (the combustible gas mainly comprises H2、CH4CO, etc.). The absorption system comprises an absorption tower 1, wherein the absorption tower 1 is provided with a desorption gas inlet at the bottom of the absorption tower, an amine-poor liquid inlet at the top of the absorption tower, a combustible gas outlet at the top of the absorption tower and an amine-rich liquid outlet at the bottom of the absorption tower. The desorption gas is input into the absorption tower 1 through a desorption gas inlet, the lean amine liquid inlet is connected with the regeneration system, the combustible gas outlet outputs combustible gas, and the rich amine liquid outlet is connected with the regeneration system, in particular to the rich amine liquid outlet which is connected with the regeneration system through a rich solution pump 9 and an amine liquid heat exchanger 4.
The regeneration system is used for contacting the rich amine liquid with the vaporized lean amine liquid to obtain lean amine liquid and gas with high carbon dioxide content, and sending the lean amine liquid back to the absorption system. The regeneration system comprises a regeneration tower 5 and a regeneration tower evaporator 10 arranged at the lower part of the regeneration tower 5. The regeneration tower 5 has an amine-rich liquid inlet at its upper portion, an amine-lean liquid outlet at its bottom portion, a vaporized amine-lean liquid inlet at its lower portion, and a high carbon dioxide content gas outlet at its top portion. An rich amine liquid outlet of an absorption tower 1 in the absorption system is connected with an rich amine liquid inlet of a regeneration tower 5 after passing through a rich liquid pump 9 and an amine liquid heat exchanger 4; the lean amine liquid outlet of the regeneration tower 5 is connected with the vaporized lean amine liquid inlet through a regeneration tower evaporator 10, and the regeneration tower evaporator 10 is connected with a steam source to obtain steam as a heat source; the lean amine liquid outlet is also connected with a lean amine liquid inlet of an absorption tower 1 in the absorption system through an amine liquid heat exchanger 4, a lean liquid pump 3 and an amine liquid cooler 2; the high carbon dioxide content gas outlet of the regeneration tower 5 is connected with a cooling pressurization system.
The cooling and pressurizing system is used for cooling and pressurizing the gas with high carbon dioxide content into high-pressure low-temperature gas. The cooling pressurization system comprises a carbon dioxide cooler 6 (providing cold energy through cooling water), a carbon dioxide compressor 7 and a normal-temperature precooler 8 which are connected in sequence.
The dehydration system is used for removing water in the high-pressure low-temperature gas to obtain dry carbon dioxide gas. The dehydration system comprises two dehydration adsorption cylinders which are alternately switched to carry out adsorption and regeneration, namely a first dehydration adsorption cylinder 11 and a second dehydration adsorption cylinder 12, each dehydration adsorption cylinder is provided with a high-pressure low-temperature gas inlet and a dry carbon dioxide gas outlet, and an adsorption dehydrating agent is arranged in each dehydration adsorption cylinder. The high-pressure low-temperature gas inlet of the dehydration adsorption cylinder is connected with the outlet of a normal-temperature precooler 8 in the cooling pressurization system, and the dry carbon dioxide gas outlet is connected with the rectification system. The dehydration system also comprises a heater, such as an electric heater 13, the dehydration adsorption cylinder is also provided with a regeneration gas inlet, a regeneration gas source is connected to the regeneration gas inlet through the heater, and the regeneration gas adopts dry nitrogen or air, so that the performance is recovered by heating the regeneration gas after the adsorption saturation of one dehydration adsorption cylinder.
The rectification system is used for rectifying and drying the carbon dioxide gas to obtain food-grade carbon dioxide, high-purity carbon dioxide and impurity gas. The rectifying system comprises a first rectifying tower 15, a first rectifying tower reboiler 16 arranged at the bottom of the first rectifying tower 15, a second rectifying tower 18 and a second rectifying tower reboiler 19 arranged at the bottom of the second rectifying tower 18. The first rectifying tower 15 has a liquid inlet at its top, a carbon dioxide gas outlet at its bottom, and an impurity gas outlet at its top. The second rectifying column 18 has a gas inlet at its upper portion, a high purity carbon dioxide outlet at its lower portion, and carbon dioxide gas outlets at its top and bottom, respectively. The first rectifying tower reboiler 16 and the second rectifying tower reboiler 19 have a gas inlet and a liquid outlet, respectively. The gas inlet of the first rectifying tower reboiler 16 and the gas inlet of the second rectifying tower reboiler 19 are connected with the dry carbon dioxide gas outlet of the dehydration adsorption cylinder in the dehydration system, and the liquid outlet of the first rectifying tower reboiler 16 and the liquid outlet of the second rectifying tower reboiler 19 are connected with the liquid inlet of the first rectifying tower 15. The impurity gas is output from the impurity gas outlet of the first rectifying tower 15 to the first rectifying tower 15, the food-grade carbon dioxide is output from the carbon dioxide gas outlet of the first rectifying tower 15 to the first rectifying tower 15, the carbon dioxide gas outlet of the first rectifying tower 15 is connected with the gas inlet of the second rectifying tower 18, the food-grade carbon dioxide is output from the carbon dioxide gas outlet of the second rectifying tower 18 to the second rectifying tower 18, and the high-purity carbon dioxide is output from the high-purity carbon dioxide outlet of the second rectifying tower 18 to the second rectifying tower 18.
In addition, the dry carbon dioxide gas outlet of the dehydration adsorption cylinder in the dehydration system can be connected to the gas inlet of the first rectifying tower reboiler 16 and the gas inlet of the second rectifying tower reboiler 19 through the first low-temperature precooler 14. The carbon dioxide gas outlet of the first rectifying tower 15 is connected with the gas inlet of the second rectifying tower 18 through a second low-temperature precooler 17. The second rectification column 18 also has a reflux inlet at the top thereof, and one branch from which the carbon dioxide gas outlet of the second rectification column 18 branches off is connected to the reflux inlet via a third cryogenic precooler 20.
The device is used for treating the desorbed gas used in the pressure swing adsorption process, and the process flow is as follows:
the desorption gas used in the pressure swing adsorption process is sent into the absorption tower 1 from the bottom, and is contacted with the lean amine liquid flowing from the tower top in the absorption tower 1, and the carbon dioxide in the desorption gas is dissolved in the lean amine liquid, so that combustible gas is obtained at the tower top, and amine-rich liquid is obtained at the tower bottom. The combustible gas can be used as fuel for recovery and can also be used as raw material to return to the gas making section. Rich amine liquid output by the absorption tower 1 is sent to the top of the regeneration tower 5 after passing through a rich liquid pump 9 and an amine liquid heat exchanger 4, lean amine liquid flowing from the bottom of the tower is heated and vaporized by a regeneration tower evaporator 10 and then contacts with the rich amine liquid flowing from the top of the tower, gas with carbon dioxide content of 95% is obtained at the top of the regeneration tower 5, namely high carbon dioxide content gas, lean amine liquid is obtained at the bottom of the tower, and the lean amine liquid is sent to the absorption tower 1 for recycling after passing through the amine liquid heat exchanger 4, a lean liquid pump 3 and an amine liquid cooler 2. The gas with the carbon dioxide content of 95% obtained at the top of the regeneration tower 5 is processed by a carbon dioxide cooler 6, a carbon dioxide compressor 7 and a normal-temperature pre-cooler 8 to obtain the carbon dioxide gas with the temperature of 2.2 MPa/7 ℃, namely the high-pressure low-temperature gas. The high-pressure low-temperature gas is dehydrated by a dehydration system to obtain dry carbon dioxide gas. After being cooled by the first low-temperature precooler 14, the dry carbon dioxide gas is respectively sent into a first rectifying tower reboiler 16 and a second rectifying tower reboiler 19 in two paths, the liquid obtained by condensation is sent into the first rectifying tower 15 for rectification, food-grade carbon dioxide is obtained at the bottom of the first rectifying tower 15, and part of impurity gas is discharged from the top. At least part of the food-grade carbon dioxide obtained from the first rectifying tower 15 is extracted and sent into a second rectifying tower 18 for rectification, so that high-purity carbon dioxide is obtained at the bottom of the second rectifying tower 18, and food-grade carbon dioxide is obtained at the top of the tower. The second rectification column 18 provides cooling using a third cryogenic precooler 20 to produce a reflux. Both the food-grade carbon dioxide and the high-purity carbon dioxide products can be provided with a low-temperature precooler so as to have certain supercooling degree and reduce vaporization.
The above embodiments are only for illustrating the technical idea and features of the present invention, and the purpose of the present invention is to enable those skilled in the art to understand the content of the present invention and implement the present invention, and not to limit the protection scope of the present invention by this means. All equivalent changes and modifications made according to the spirit of the present invention should be covered in the protection scope of the present invention.
Claims (10)
1. The utility model provides a pressure swing adsorption analytic gas recycle device for handle the analytic gas that uses in the pressure swing adsorption technology, its characterized in that: the pressure swing adsorption desorption gas recycle device comprises:
an absorption system for dissolving carbon dioxide in the input decomposed gas in an amine-poor liquid to form an amine-rich liquid and separating the amine-rich liquid to obtain combustible gas;
a regeneration system connected to the absorption system for contacting the amine-rich liquid with the vaporized amine-lean liquid to obtain an amine-lean liquid and a gas with a high carbon dioxide content, and returning the amine-lean liquid to the absorption system;
the cooling and pressurizing system is connected with the regeneration system and is used for cooling and pressurizing the high-carbon-dioxide-content gas into high-pressure low-temperature gas;
the dehydration system is connected with the cooling pressurization system and is used for removing moisture in the high-pressure low-temperature gas to obtain dry carbon dioxide gas;
And the rectification system is connected with the dehydration system and is used for rectifying the dry carbon dioxide gas to obtain food-grade carbon dioxide, high-purity carbon dioxide and impurity gas.
2. The pressure swing adsorption desorption gas recycle device according to claim 1, which is characterized in that: the absorption system comprises an absorption tower, the absorption tower is provided with a desorption gas inlet, a lean amine liquid inlet, a combustible gas outlet and an amine-rich liquid outlet, the desorption gas is input into the absorption tower through the desorption gas inlet, the lean amine liquid inlet is connected with the regeneration system, the combustible gas outlet outputs the combustible gas, and the amine-rich liquid outlet is connected with the regeneration system.
3. The pressure swing adsorption desorption gas recycle device according to claim 2, which is characterized in that: and the rich amine liquid outlet is connected with the regeneration system through a rich liquid pump and an amine liquid heat exchanger.
4. The pressure swing adsorption desorption gas recycle device according to claim 1, which is characterized in that: the regeneration system comprises a regeneration tower and a regeneration tower evaporator arranged at the lower part of the regeneration tower, the regeneration tower is provided with an amine-rich liquid inlet, an amine-poor liquid outlet, a vaporized amine-poor liquid inlet and a high-carbon-dioxide-content gas outlet, the absorption system is connected with the amine-rich liquid inlet, the amine-poor liquid outlet is connected with the vaporized amine-poor liquid inlet through the regeneration tower evaporator, the amine-poor liquid outlet is connected with the absorption system through an amine liquid heat exchanger, a amine liquid pump and an amine liquid cooler, and the high-carbon-dioxide-content gas outlet is connected with the cooling pressurization system.
5. The Pressure Swing Adsorption (PSA) gas analysis recycling apparatus according to claim 4, wherein: the regeneration tower evaporator is connected with a steam source to obtain steam as a heat source.
6. The pressure swing adsorption desorption gas recycle device according to claim 1, which is characterized in that: the cooling pressurization system comprises a carbon dioxide cooler, a carbon dioxide compressor and a normal-temperature precooler which are sequentially connected.
7. The pressure swing adsorption desorption gas recycle device according to claim 1, which is characterized in that: the dehydration system comprises a dehydration adsorption cylinder which is alternately switched to carry out adsorption and regeneration, the dehydration adsorption cylinder is provided with a high-pressure low-temperature gas inlet and a dry carbon dioxide gas outlet, the high-pressure low-temperature gas inlet is connected with the cooling pressurization system, the dry carbon dioxide gas outlet is connected with the rectification system, and an adsorption dehydrating agent is arranged in the dehydration adsorption cylinder.
8. The pressure swing adsorption desorption gas recycle device according to claim 7, which is characterized in that: the dehydration system further comprises a heater, the dehydration adsorption cylinder is further provided with a regeneration gas inlet, and a regeneration gas source is connected to the regeneration gas inlet through the heater.
9. The pressure swing adsorption desorption gas recycle device according to claim 1, which is characterized in that: the rectifying system comprises a first rectifying tower, a first rectifying tower reboiler arranged at the bottom of the first rectifying tower, a second rectifying tower and a second rectifying tower reboiler arranged at the bottom of the second rectifying tower, wherein the first rectifying tower is provided with a liquid inlet, a carbon dioxide gas outlet and an impurity gas outlet, the second rectifying tower is provided with a gas inlet, a high-purity carbon dioxide outlet and a carbon dioxide gas outlet, and the first rectifying tower reboiler and the second rectifying tower reboiler are respectively provided with a gas inlet and a liquid outlet; the gas inlet of the first rectifying tower reboiler and the gas inlet of the second rectifying tower reboiler are both connected with the dehydration system, the liquid outlet of the first rectifying tower reboiler and the liquid outlet of the second rectifying tower reboiler are both connected with the liquid inlet of the first rectifying tower, the impurity gas is output from the impurity gas outlet of the first rectifying tower to the first rectifying tower, the food-grade carbon dioxide is output from the first rectifying tower through a carbon dioxide gas outlet of the first rectifying tower, the carbon dioxide gas outlet of the first rectifying tower is connected with the gas inlet of the second rectifying tower, the food grade carbon dioxide is output from the second rectifying tower through the carbon dioxide gas outlet of the second rectifying tower, and the high-purity carbon dioxide is output from the second rectifying tower through a high-purity carbon dioxide outlet of the second rectifying tower.
10. The Pressure Swing Adsorption (PSA) gas analysis recycling apparatus according to claim 9, wherein: the dehydration system is connected to a gas inlet of the first rectifying tower reboiler and a gas inlet of the second rectifying tower reboiler after passing through a first low-temperature precooler; the carbon dioxide gas outlet of the first rectifying tower is connected with the gas inlet of the second rectifying tower through a second low-temperature precooler; the second rectifying tower is also provided with a reflux inlet, and one branch branched from the carbon dioxide gas outlet of the second rectifying tower is connected to the reflux inlet through a third low-temperature precooler.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210141163.6A CN114669167A (en) | 2022-02-16 | 2022-02-16 | Pressure swing adsorption and desorption gas recycling device |
Applications Claiming Priority (1)
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