CN114405221A - For CO2Energy recovery system for non-condensable gas at top of rectifying tower in capturing device - Google Patents
For CO2Energy recovery system for non-condensable gas at top of rectifying tower in capturing device Download PDFInfo
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- CN114405221A CN114405221A CN202111313939.XA CN202111313939A CN114405221A CN 114405221 A CN114405221 A CN 114405221A CN 202111313939 A CN202111313939 A CN 202111313939A CN 114405221 A CN114405221 A CN 114405221A
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- 238000011084 recovery Methods 0.000 title claims abstract description 28
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 47
- 230000023556 desulfurization Effects 0.000 claims abstract description 47
- 238000011069 regeneration method Methods 0.000 claims abstract description 46
- 230000008929 regeneration Effects 0.000 claims abstract description 45
- 238000001179 sorption measurement Methods 0.000 claims abstract description 45
- 238000001035 drying Methods 0.000 claims abstract description 42
- 238000000034 method Methods 0.000 claims abstract description 18
- 239000003507 refrigerant Substances 0.000 claims abstract description 6
- 230000008569 process Effects 0.000 claims description 14
- 230000001172 regenerating effect Effects 0.000 claims description 14
- 239000002274 desiccant Substances 0.000 claims description 11
- 239000003463 adsorbent Substances 0.000 claims description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 8
- 229910021536 Zeolite Inorganic materials 0.000 claims description 6
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 6
- 239000010457 zeolite Substances 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 239000000377 silicon dioxide Substances 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 abstract description 54
- 230000000087 stabilizing effect Effects 0.000 abstract description 5
- 238000001816 cooling Methods 0.000 abstract description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 3
- 239000003546 flue gas Substances 0.000 abstract description 3
- 239000011521 glass Substances 0.000 abstract description 3
- 230000008878 coupling Effects 0.000 abstract description 2
- 238000010168 coupling process Methods 0.000 abstract description 2
- 238000005859 coupling reaction Methods 0.000 abstract description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 36
- 229910002092 carbon dioxide Inorganic materials 0.000 description 29
- 239000001569 carbon dioxide Substances 0.000 description 18
- 230000008901 benefit Effects 0.000 description 5
- 239000012535 impurity Substances 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 150000004767 nitrides Chemical class 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 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
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/261—Drying gases or vapours by adsorption
-
- 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
- B01D53/28—Selection of materials for use as drying agents
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0266—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/104—Alumina
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
- B01D2253/108—Zeolites
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Drying Of Gases (AREA)
Abstract
The invention relates to the field of flue gas treatment in the glass industry, and discloses a method for treating CO2The energy recovery device comprises a compressor, wherein the output end of the compressor is connected with a pressure stabilizing tank, the output end of the pressure stabilizing tank is connected with a desulfurization bed A/B, the output end of the desulfurization bed A/B is connected with a drying bed A/B, the drying bed A/B is connected with an adsorption bed A/B through a second cooler, the adsorption bed A/B is connected with a rectifying tower through a precooler and a liquefier, the rectifying tower is communicated with a noncondensable gas main pipe through a desulfurization regeneration heater, a drying regeneration heater and an adsorption regeneration heater, and the noncondensable gas main pipe is used for CO2Energy of non-condensable gas at top of rectifying tower in capturing deviceThe recovery system uses the non-condensable gas at the tower top as a refrigerant and is in a precooler with the main stream CO2And (4) heat exchange, namely cooling the temperature of the cold energy from 40 ℃ to 35 ℃, and energy coupling is performed, so that 11kW of cold energy recovery is successfully realized.
Description
Technical Field
The invention relates to the field of flue gas treatment in the glass industry, in particular to a method for treating CO2And a non-condensable gas energy recovery system at the top of the rectifying tower in the capturing device.
Background
Carbon dioxide is the most dominant greenhouse gas, and its increased content contributes approximately 70% to the enhancement of the greenhouse effect. Carbon capture, sequestration and utilization technology (CCS) is a process in which carbon dioxide discharged during production is purified and then put into a new production process. The process can recycle the carbon dioxide and generate economic benefits. Pure oxygen glass kiln can generate a large amount of high CO2The content of the flue gas contains 30-36% of carbon dioxide. For the enterprise, CO recovery2Can change waste into valuable and obtain considerable economic benefit, so CO2The recycling of the waste water is a measure of win-win social benefit, environmental benefit and enterprise benefit. The process adopts a rectifying tower device to obtain food-grade CO2A small amount of N mixed in the column top is generated2、O2Low temperature CO of2Residual gas is matched with a rectification tower top non-condensable gas energy recovery and resource comprehensive utilization system for reasonably utilizing the energy and resources, so that green normal operation of a CCS (continuous cooling system) can be effectively ensured, energy consumption is saved, the quality of finished gas is improved, and higher popularization significance is realized along with the development of the CCS technology, so that the system for CO recovery and comprehensive utilization of the energy and resources is provided for the CO recovery and regeneration2And a non-condensable gas energy recovery system at the top of the rectifying tower in the capturing device.
Disclosure of Invention
Technical problem to be solved
Aiming at the defects of the prior art, the invention provides a method for CO2The energy recovery system for the non-condensable gas at the top of the rectifying tower in the capturing device solves the problems.
(II) technical scheme
In order to achieve the above purpose, the invention provides the following technical scheme: for CO2Energy recovery of non-condensable gas at top of rectifying tower in capturing deviceThe device comprises a compressor, the output of compressor is connected with the surge tank, desulfurization bed A/B is connected to the output of surge tank, dry bed A/B is connected to desulfurization bed A/B's output, dry bed A/B is connected with adsorption bed A/B through the second cooler, adsorption bed A/B passes through the precooler and liquefier and connects the rectifying column, the rectifying column passes through desulfurization regeneration heater, dry regeneration heater and adsorption regeneration heater intercommunication noncondensable gas house steward.
Preferably, the output end of the desulfurization bed A/B is communicated with the non-condensable gas main pipe, and the desulfurization regeneration heater is connected with the input end of the desulfurization bed A/B.
Preferably, the output end of the drying bed A/B is connected with a non-condensable gas main pipe, and the drying regeneration heater is connected with the input end of the drying bed A/B.
Preferably, the output end of the adsorption bed A/B is connected with a non-condensable gas main pipe, and the output end of the adsorption bed A/B is connected with an adsorption regeneration heater.
Preferably, the output ends of the desulfurization regeneration heater, the drying regeneration heater and the adsorption regeneration heater are connected through pipelines, the connecting pipelines of the desulfurization regeneration heater, the drying regeneration heater and the adsorption regeneration heater are communicated with the non-condensable gas main pipe, and the output end of the rectifying tower is connected with the pipelines of the desulfurization regeneration heater, the drying regeneration heater and the adsorption regeneration heater through valves.
Preferably, an adsorbent for further desulfurization is arranged in the desulfurization bed A/B, a zeolite desiccant is arranged in the drying bed A/B, and an alumina desiccant and a silica filtering agent are arranged in the adsorption bed A/B.
Preferably, the second cooler refrigerant is circulating water.
(III) advantageous effects
Compared with the prior art, the invention provides a method for CO2The energy recovery system for the non-condensable gas at the top of the rectifying tower in the capturing device has the following beneficial effects:
1. the catalyst is used for CO2The energy recovery system for the non-condensable gas at the top of the rectifying tower in the capture device uses the non-condensable gas at the top of the rectifying tower as a refrigerant and is mixed with main material flow CO in a precooler2And (4) heat exchange, namely cooling the temperature of the cold energy from 40 ℃ to 35 ℃, and energy coupling is performed, so that 11kW of cold energy recovery is successfully realized.
2. The catalyst is used for CO2In the energy recovery system for the non-condensable gas at the top of the rectifying tower in the capturing device, the non-condensable gas at the top of the heated tower is continuously heated to the required temperature by the electric heater, and then the desulfurization bed, the drying bed and the adsorption bed are purged, so that the energy consumption of the electric heater is reduced.
3. The catalyst is used for CO2The energy recovery system for the non-condensable gas at the top of the rectifying tower in the capturing device directly utilizes the heated non-condensable gas at the top of the rectifying tower when purging the desulfurization bed, the drying bed and the adsorption bed, thereby avoiding introducing other impurity gases and ensuring the rectification purity of the following process.
4. The catalyst is used for CO2In the energy recovery system for the non-condensable gas at the top of the rectifying tower in the capturing device, a second cooler is added in the processes of sequentially purifying a desulfurization bed, a drying bed and an adsorption bed, so that the temperature stability of carbon dioxide and the activity of an adsorbent are ensured, the loss of the adsorbent is reduced, and the emission of pollutants such as nitride to the atmosphere is indirectly reduced.
Drawings
FIG. 1 is a schematic diagram of the system of the present invention.
In the figure: 1. a compressor; 2. a surge tank; 3. a noncondensable gas main pipe; 4. a desulfurization bed A/B; 5. a desulfurization regeneration heater; 6. Drying the regenerative heater; 7. a drying bed A/B; 8. a second cooler; 9. adsorption beds A/B; 10. an adsorption regeneration heater; 11. a precooler; 12. a liquefier; 13. a rectifying tower.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Referring to fig. 1, the energy recovery device for the top noncondensable gas of the rectifying tower for the capture device of the CO surge tank 2 comprises a compressor 1, wherein the output end of the compressor 1 is connected with the surge tank 2, the output end of the surge tank 2 is connected with a desulfurization bed a/B4, the output end of a desulfurization bed a/B4 is connected with a drying bed a/B7, the drying bed a/B7 is connected with an adsorption bed a/B9 through a second cooler 8, the adsorption bed a/B9 is connected with a rectifying tower 13 through a precooler 11 and a liquefier 12, and the rectifying tower 13 is communicated with a noncondensable gas main 3 through a desulfurization regenerative heater 5, a drying regenerative heater 6 and an adsorption regenerative heater 10.
Further, the output end of the desulfurization bed A/B4 is communicated with the non-condensable gas main pipe 3, and the desulfurization regeneration heater 5 is connected with the input end of the desulfurization bed A/B4.
Further, the output end of the drying bed A/B7 is connected with the non-condensable gas main pipe 3, and the drying regeneration heater 6 is connected with the input end of the drying bed A/B7.
Further, the output end of the adsorption bed A/B9 is connected with the non-condensable gas main pipe 3, and the output end of the adsorption bed A/B9 is connected with the adsorption regeneration heater 10.
Further, the output ends of the desulfurization regeneration heater 5, the drying regeneration heater 6 and the adsorption regeneration heater 10 are all connected through a pipeline, the connecting pipelines of the desulfurization regeneration heater 5, the drying regeneration heater 6 and the adsorption regeneration heater 10 are communicated with the non-condensable gas main pipe 3, and the output end of the rectifying tower 13 is connected with the pipelines of the desulfurization regeneration heater 5, the drying regeneration heater 6 and the adsorption regeneration heater 10 through valves.
Further, an adsorbent for further desulfurization is arranged in the desulfurization bed A/B4, a zeolite desiccant is arranged in the drying bed A/B7, and an alumina desiccant and a silica filtering agent are arranged in the adsorption bed A/B9.
The refrigerant of the second cooler 8 is circulating water.
The main flow of the carbon dioxide process:
introducing 95% carbon dioxide gas into a buffer tank through a fan, then feeding the carbon dioxide gas into a compressor 1 for pressurization, cooling, dividing water and stabilizing pressure, increasing the pressure of the carbon dioxide gas to a pressure stabilizing tank 2, raising the temperature to 40 ℃ by using a drying regenerative heater 6Mpa, and sequentially feeding the carbon dioxide gas into a desulfurization bed A/B4, a drying bed A/B7 and an adsorption bed A/B9 to adsorb impurities. Wherein, the desulfurization bed A/B4 is internally provided with desulfurization adsorbent active carbon; zeolite desiccant is arranged in the desiccant bed A/B7, and the zeolite not only can be used as the desiccant, but also can be used as an adsorbent to adsorb substances such as dust, SOx, NOx and the like due to the huge specific surface area of the zeolite; the adsorbent bed A/B9 is provided with alumina desiccant and silica filter. The material flow enters a desulfurizing bed A/B4 to remove sulfide and then enters a drying bed A/B7, the heat release temperature in the drying and adsorption process is raised to 80 ℃, so a second cooler 8 is arranged, and the material flow enters an adsorption bed A/B9 to remove trace impurities such as grease, nitride and the like after being cooled to 40 ℃ by the second cooler 8 (the refrigerant is circulating water); the absorbed material flow (pressure stabilizing tank 2, drying regeneration heater 6Mpa,40 deg.C) enters into precooler 11, and is cooled to 35 deg.C by the throttled low-temperature noncondensable gas (-55 deg.C) discharged from the top of rectifying tower 13, and then enters into liquefier for liquefaction. And after the cold energy of the non-condensable gas is released, the non-condensable gas as regeneration gas passes through the electric heater and then enters a desulfurization/drying/adsorption regeneration system, and after impurities are carried, the regeneration gas enters a non-condensable gas main pipe 3. The liquefied material flow enters a rectification system, light components of noncondensable gases such as nitrogen, oxygen, a small amount of carbon dioxide and the like are removed from the top of the tower, and a high-purity carbon dioxide product with the purity of more than 99.9 percent is obtained at the bottom of the tower. Remarking: each set of the desulfurization bed, the drying bed and the adsorption bed is designed into two bed bodies (A and B) with the same volume, and the bed bodies are filled with equivalent desulfurizing agents, drying agents and various high-efficiency adsorbents. The two beds are alternately operated, and the production is continuously carried out.
The non-condensable gas process flow comprises the following steps:
the low-temperature carbon dioxide after the liquefier enters a rectifying tower 13 for separation and purification, high-purity carbon dioxide is obtained at the bottom of the rectifying tower 13, low-temperature carbon dioxide non-condensable gas mixed with a small amount of N surge tank 2 and O surge tank 2 generated at the top of the tower is throttled to have a temperature of-55 ℃, the temperature is raised to an adsorption regeneration heater of 10 ℃ after heat exchange of a precooler, then a part of the low-temperature carbon dioxide non-condensable gas is discharged to the air through a non-condensable gas main pipe, and a part of the low-temperature carbon dioxide non-condensable gas is used as regeneration gas to be blown to the bed bodies of various equipment through regeneration heaters of a desulfurization bed A/B4, a drying bed A/B7 and an adsorption bed A/B9, and the blown gas is collected to the non-condensable gas main pipe and is discharged to the atmosphere. The energy recovery and resource comprehensive utilization system for the non-condensable gas at the top of the rectifying tower 13 realizes cold recycling, is green and energy-saving, avoids introducing other impurity gases to purge a bed body, is favorable for purifying carbon dioxide, and indirectly reduces the energy consumption of the rectifying tower 13.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (7)
1. For CO2Energy recovery of non-condensable gas at top of rectifying tower among trapping apparatus, including compressor (1), the output of compressor (1) is connected with surge tank (2), desulfurization bed A/B (4) is connected to the output of surge tank (2), drying bed A/B (7) is connected to the output of desulfurization bed A/B (4), drying bed A/B (7) are connected with adsorption bed A/B (9) through second cooler (8), and adsorption bed A/B (9) are through precooler (11) and liquefier (12) connection rectifying column (13), rectifying column (13) are through desulfurization regeneration heater (5), dry regeneration heater (6) and adsorption regeneration heater (10) intercommunication non-condensable gas house steward (3).
2. A process for CO according to claim 12The top noncondensable gas energy recovery system of the rectifying tower in the trapping apparatus is characterized in that: the output end of the desulfurization bed A/B (4) is communicated with the non-condensable gas main pipe (3), and the desulfurization regeneration heater (5) is connected with the input end of the desulfurization bed A/B (4).
3. A process for CO according to claim 12The top noncondensable gas energy recovery system of the rectifying tower in the trapping apparatus is characterized in that: the output end of the drying bed A/B (7) is connected with the non-condensable gas main pipe (3), and the drying regeneration heater (6) is connected with the input end of the drying bed A/B (7).
4. A process for CO according to claim 12The top noncondensable gas energy recovery system of the rectifying tower in the trapping apparatus is characterized in that: the output end of the adsorption bed A/B (9) is connected with the non-condensable gas main pipe (3), and the output end of the adsorption bed A/B (9) is connected with the adsorption regeneration heater (10).
5. A process for CO according to claim 12The top noncondensable gas energy recovery system of the rectifying tower in the trapping apparatus is characterized in that: the output ends of the desulfurization regenerative heater (5), the drying regenerative heater (6) and the adsorption regenerative heater (10) are connected through pipelines, the connecting pipelines of the desulfurization regenerative heater (5), the drying regenerative heater (6) and the adsorption regenerative heater (10) are communicated with the noncondensable gas main pipe (3), and the output end of the rectifying tower (13) is connected with the pipelines of the desulfurization regenerative heater (5), the drying regenerative heater (6) and the adsorption regenerative heater (10) through valves.
6. A process for CO according to claim 12The top noncondensable gas energy recovery system of the rectifying tower in the trapping apparatus is characterized in that: an adsorbent used for further desulfurization is arranged in the desulfurization bed A/B (4), a zeolite desiccant is arranged in the drying bed A/B (7), and an alumina desiccant and a silica filtering agent are arranged in the adsorption bed A/B (9).
7. A process for CO according to claim 12The top noncondensable gas energy recovery system of the rectifying tower in the trapping apparatus is characterized in that: the refrigerant of the second cooler (8) is circulating water.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111313939.XA CN114405221A (en) | 2021-11-08 | 2021-11-08 | For CO2Energy recovery system for non-condensable gas at top of rectifying tower in capturing device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202111313939.XA CN114405221A (en) | 2021-11-08 | 2021-11-08 | For CO2Energy recovery system for non-condensable gas at top of rectifying tower in capturing device |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203419745U (en) * | 2013-07-18 | 2014-02-05 | 毛亚成 | Carbon dioxide distillation recycling device with double gas cabinets |
| CN106348298A (en) * | 2016-08-30 | 2017-01-25 | 兰州裕隆气体有限责任公司 | Efficient and energy-saving system for rectifying and purifying carbon dioxide |
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| CN113149012A (en) * | 2021-03-29 | 2021-07-23 | 本钢板材股份有限公司 | Method for extracting carbon dioxide by using blast furnace gas |
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| CN203419745U (en) * | 2013-07-18 | 2014-02-05 | 毛亚成 | Carbon dioxide distillation recycling device with double gas cabinets |
| CN106348298A (en) * | 2016-08-30 | 2017-01-25 | 兰州裕隆气体有限责任公司 | Efficient and energy-saving system for rectifying and purifying carbon dioxide |
| CN106979664A (en) * | 2017-03-06 | 2017-07-25 | 毛恒松 | Atmospheric carbon dioxide liquifying method |
| CN107062798A (en) * | 2017-03-06 | 2017-08-18 | 毛恒松 | Atmospheric carbon dioxide liquefaction system and method |
| CN210832753U (en) * | 2019-08-14 | 2020-06-23 | 东营市港城热力有限公司 | Carbon dioxide compression and purification system of coal-fired boiler |
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| CN113149012A (en) * | 2021-03-29 | 2021-07-23 | 本钢板材股份有限公司 | Method for extracting carbon dioxide by using blast furnace gas |
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