CN102538395A - Carbon dioxide purification technology - Google Patents
Carbon dioxide purification technology Download PDFInfo
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- CN102538395A CN102538395A CN2012100541450A CN201210054145A CN102538395A CN 102538395 A CN102538395 A CN 102538395A CN 2012100541450 A CN2012100541450 A CN 2012100541450A CN 201210054145 A CN201210054145 A CN 201210054145A CN 102538395 A CN102538395 A CN 102538395A
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- Prior art keywords
- carbon dioxide
- heat exchanger
- waste gas
- rectifying
- rectification
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 84
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 42
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 42
- 238000005516 engineering process Methods 0.000 title abstract description 6
- 238000000746 purification Methods 0.000 title abstract description 3
- 239000002912 waste gas Substances 0.000 claims abstract description 36
- 238000010521 absorption reaction Methods 0.000 claims abstract description 23
- 238000001816 cooling Methods 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims abstract description 5
- 238000005057 refrigeration Methods 0.000 claims description 33
- 230000004087 circulation Effects 0.000 claims description 22
- 238000000034 method Methods 0.000 claims description 19
- 239000000178 monomer Substances 0.000 claims description 9
- 230000006835 compression Effects 0.000 claims description 7
- 238000007906 compression Methods 0.000 claims description 7
- 238000004458 analytical method Methods 0.000 claims description 3
- 239000002994 raw material Substances 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 238000003795 desorption Methods 0.000 abstract 2
- 238000001179 sorption measurement Methods 0.000 abstract 2
- 238000000605 extraction Methods 0.000 abstract 1
- 230000003139 buffering effect Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 235000019628 coolness Nutrition 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Classifications
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- 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
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- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
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- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
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- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/64—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end by pressure-swing adsorption [PSA] at the hot end
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- 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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- 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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
- F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
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- 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
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- 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/32—Compression of the product stream
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- 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/04—Internal refrigeration with work-producing gas expansion loop
- F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
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- 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
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- 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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/62—Details of storing a fluid in a tank
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention relates to a carbon dioxide purification technology, which includes the steps as follows: carbon dioxide feed gas is cooled through a master heat exchanger and introduced in a rectification column for rectification, so as to obtain liquid carbon dioxide; a waste gas outlet is arranged at the top of the rectification column, and waste gas generated in the rectification enters an auxiliary heat exchanger for cooling, passes by an expansion refrigerating cycle for providing cold quantity for the master heat exchanger and the auxiliary heat exchanger and finally discharged; a PSA (pressure swing adsorption) device is arranged on a discharge channel for the waste gas generated in the rectification, and used for adsorbing the waste gas; desorption gas and carbon dioxide with higher purity are generated after the absorption; the carbon dioxide with higher purity can be compressed and cooled, and then introduced in the rectification column for rectification; and the desorption gas returns to the discharge channel for the waste gas generated in rectification and is discharged. As the PSA device is adopted in the invention for absorbing waste gas generated in the rectification, and carbon dioxide with higher purity generated in the adsorption is sent to the rectification column for rectification, and by the combination with the arranged expansion refrigerating cycle, the technology can further reduce the energy consumption for the rectification of carbon dioxide, improve the extraction rate of carbon dioxide, and reduce the manufacturing cost.
Description
Technical field
The present invention relates to a kind of carbon dioxide purifying technique.
Background technology
In the prior art, adopt the rectifying mode to obtain liquid carbon dioxide product usually to the purification of carbon dioxide.Owing to also contain a certain amount of carbon dioxide in the waste gas that rectifying produces, therefore, condensing unit be set behind rectifying column.In order to cut down the consumption of energy, the waste expansion that this condensing unit adopts rectifying to produce freezes cold is provided.Adopt the energy consumption of this rectification process still higher, also have the space that reduces, and this technology recovery rate is low, also have the space that promotes.
Summary of the invention
The purpose of this invention is to provide a kind of cut down the consumption of energy and increase recovery rate the carbon dioxide purifying technique.
For achieving the above object, the technical scheme that the present invention adopts is:
A kind of carbon dioxide purifying technique; Comprise CO 2 raw material gas rectifying in main heat exchanger cooling back feeding rectifying column is obtained liquid carbon dioxide product; The top of described rectifying column has waste gas outlet; The waste gas of rectifying generation gets into the auxiliary heat exchanger cooling and circulation is to discharge after described main heat exchanger and described auxiliary heat exchanger provide cold through swell refrigeration; Also being provided with pressure-swing absorption apparatus on the drain passageway of the waste gas that described rectifying produces adsorbs it; Absorption back produces separates gassing and the higher carbon dioxide of purity, carbon dioxide rectifying in compression and the described rectifying column of cooling back feeding that described purity is higher, and the described gassing of separating is got back in the drain passageway of waste gas of described rectifying generation and is discharged.
Preferably; Described pressure-swing absorption apparatus comprises two or many absorbing cylinders, the pipelines that are connected with described absorbing cylinder, is arranged at a plurality of valves on the described pipeline; The pipeline that the carbon dioxide that described purity is higher feeds described rectifying column is provided with absorption back surge tank, compressor, compression aftercooler, discharges the described pipeline of separating gassing and is provided with and separates the gassing surge tank.
Preferably; The circulation of described swell refrigeration is the multiple expansion kind of refrigeration cycle of series connection, and the waste gas that described rectifying produces is before described pressure-swing absorption apparatus absorption is arranged at described swell refrigeration circulation or after the circulation of described swell refrigeration or be arranged between the described swell refrigeration of any adjacent two-stage circulates.
Preferably, the circulation of described swell refrigeration comprises that the waste gas that described rectifying is produced feeds behind the booster expansion turbine and feeds in described auxiliary heat exchanger and the described main heat exchanger, forms the described swell refrigeration circulation of one-level.
Preferably, in the circulation of described swell refrigeration, the waste gas that described rectifying produces is earlier through the pressurized end of described booster expansion turbine, pass through the expanding end of described booster expansion turbine again.
Preferably, the waste gas that produces of described rectifying gets into described booster expansion turbine expanding end after going out the pressurized end of described booster expansion turbine again after getting into the expanding end of described booster expansion turbine behind the supercharger cooler or returning described main heat exchanger cooling.
Preferably, described booster expansion turbine is one or more.
Preferably, described auxiliary heat exchanger comprises one or more heat exchanger monomers, feeds the cold-producing medium that cold is provided in each described heat exchanger monomer.
Preferably, described pressure-swing absorption apparatus is that normal pressure is resolved or vacuum analysis.
Because technique scheme utilization; The present invention compared with prior art has advantage: because the present invention adopts pressure-swing absorption apparatus that the waste gas that rectifying produces is adsorbed; And will adsorb the higher carbon dioxide of purity that produces and send into rectifying in the rectifying column, the swell refrigeration that combines to be provided with circulates, and can further reduce the energy consumption of carbon dioxide rectifying; Improve the carbon dioxide draw rate, reduce production costs.
Description of drawings
Accompanying drawing 1 is the sketch map of a kind of carbon dioxide purifying technique of the present invention.
In the above accompanying drawing: 1, rectifying column; 2, first heat exchanger (auxiliary heat exchanger); 3, second heat exchanger (auxiliary heat exchanger); 4, the 3rd heat exchanger (auxiliary heat exchanger); 5, booster expansion turbine; 6, supercharger cooler; 7, absorbing cylinder; 8, absorption back surge tank; 9, separate the gassing surge tank; 10, compressor; 11, compression aftercooler; 12, main heat exchanger.
The specific embodiment
Below in conjunction with embodiment shown in the drawings the present invention is further described.
Embodiment one: shown in accompanying drawing 1.
A kind of carbon dioxide purifying technique is used for through rectifying carbon dioxide being purified.
The rectifying in main heat exchanger 12 cooling back feeding rectifying column 1 of this process using rectifying column 1, CO 2 raw material gas obtains liquid carbon dioxide product.The top of rectifying column 1 has waste gas outlet, and the waste gas that rectifying produces is discharged after discharging rectifying column 1 and process waste gas drain passageway by this waste gas outlet.The waste gas drain passageway is provided with auxiliary heat exchanger, and this auxiliary heat exchanger comprises one or more heat exchanger monomers, feeds the cold-producing medium that cold is provided in each heat exchanger monomer.Be provided with three heat exchanger monomers in the present embodiment; Be respectively first heat exchanger 2, second heat exchanger 3, the 3rd heat exchanger 4; After cooling off through three heat exchanger monomers successively, the waste gas that rectifying produces, gets into the multiple expansion kind of refrigeration cycle of series connection then through main heat exchanger 12.
In the present embodiment, be provided with three grades of swell refrigeration circulations.Every grade of swell refrigeration circulation includes a booster expansion turbine 5 and a supercharger cooler 6.Also can booster expansion turbine 5 of swell refrigeration cycle sharings at different levels.
The waste gas that rectifying produces feeds the pressurized end of booster expansion turbine 5 earlier, goes out behind the pressurized end of booster expansion turbine 5 through getting into the expanding end of booster expansion turbine 5 behind the supercharger cooler 6 again.The waste gas that rectifying produces goes out in each heat exchanger monomer of feeding auxiliary heat exchanger behind the expanding end of booster expansion turbine 5 and the main heat exchanger 12 provides cold, forms the circulation of one-level swell refrigeration, gets into the next stage swell refrigeration then and circulates.Waste gas through the circulation of afterbody swell refrigeration is discharged.
On the drain passageway of the waste gas that rectifying produces, also be provided with pressure-swing absorption apparatus, this pressure-swing absorption apparatus is arranged at before the multiple expansion kind of refrigeration cycle or after the multiple expansion kind of refrigeration cycle or be arranged between any adjacent double expansion kind of refrigeration cycle.Pressure-swing absorption apparatus is that normal pressure is resolved or vacuum analysis.In the present embodiment, between circulation of second level swell refrigeration and the circulation of third level swell refrigeration, being provided with pressure-swing absorption apparatus adsorbs the waste gas that rectifying produces.Pressure-swing absorption apparatus comprises two or many absorbing cylinders 7, the pipelines that are connected with absorbing cylinder 7, is arranged at a plurality of valves on the pipeline; Each absorbing cylinder 7 replaces accomplishes absorption or regeneration, will adsorb through the waste gas of second level swell refrigeration circulation and produce respectively and separate gassing and the higher carbon dioxide of purity.The higher carbon dioxide surge tank 8 buffering backs after adsorbing of purity get into compressor 10; After compressor 10 compressions and cooler 11 coolings after compression, feed the top rectifying of rectifying column 1, separate gassing and after separating gassing surge tank 9 bufferings, get back in the circulation of third level swell refrigeration.
The foregoing description only is explanation technical conceive of the present invention and characteristics, and its purpose is to let the personage who is familiar with this technology can understand content of the present invention and enforcement according to this, can not limit protection scope of the present invention with this.All equivalences that spirit is done according to the present invention change or modify, and all should be encompassed within protection scope of the present invention.
Claims (9)
1. carbon dioxide purifying technique; Comprise CO 2 raw material gas rectifying in main heat exchanger cooling back feeding rectifying column is obtained liquid carbon dioxide product; The top of described rectifying column has waste gas outlet; The waste gas of rectifying generation gets into the auxiliary heat exchanger cooling and circulation is to discharge after described main heat exchanger and described auxiliary heat exchanger provide cold through swell refrigeration; It is characterized in that: also be provided with pressure-swing absorption apparatus on the drain passageway of the waste gas that described rectifying produces it is adsorbed; Absorption back produces separates gassing and the higher carbon dioxide of purity, carbon dioxide rectifying in compression and the described rectifying column of cooling back feeding that described purity is higher, and the described gassing of separating is got back in the drain passageway of waste gas of described rectifying generation and is discharged.
2. a kind of carbon dioxide purifying technique according to claim 1; It is characterized in that: described pressure-swing absorption apparatus comprises two or many absorbing cylinders, the pipelines that are connected with described absorbing cylinder, is arranged at a plurality of valves on the described pipeline; The pipeline that the carbon dioxide that described purity is higher feeds described rectifying column is provided with absorption back surge tank, compressor, compression aftercooler, discharges the described pipeline of separating gassing and is provided with and separates the gassing surge tank.
3. a kind of carbon dioxide purifying technique according to claim 1; It is characterized in that: the circulation of described swell refrigeration is the multiple expansion kind of refrigeration cycle of series connection, and the waste gas that described rectifying produces is before described pressure-swing absorption apparatus absorption is arranged at described swell refrigeration circulation or after the circulation of described swell refrigeration or be arranged between the described swell refrigeration of any adjacent two-stage circulates.
4. a kind of carbon dioxide purifying technique according to claim 1; It is characterized in that: the circulation of described swell refrigeration comprises that the waste gas that described rectifying is produced feeds behind the booster expansion turbine and feeds in described auxiliary heat exchanger and the described main heat exchanger, forms the described swell refrigeration circulation of one-level.
5. a kind of carbon dioxide purifying technique according to claim 4; It is characterized in that: in the circulation of described swell refrigeration, the waste gas that described rectifying produces is earlier through the pressurized end of described booster expansion turbine, pass through the expanding end of described booster expansion turbine again.
6. a kind of carbon dioxide purifying technique according to claim 5 is characterized in that: the waste gas that described rectifying produces gets into described booster expansion turbine expanding end after going out the pressurized end of described booster expansion turbine again after getting into the expanding end of described booster expansion turbine behind the supercharger cooler or returning described main heat exchanger cooling.
7. a kind of carbon dioxide purifying technique according to claim 4 is characterized in that: described booster expansion turbine is one or more.
8. a kind of carbon dioxide purifying technique according to claim 1 is characterized in that: described auxiliary heat exchanger comprises one or more heat exchanger monomers, feeds the cold-producing medium that cold is provided in each described heat exchanger monomer.
9. a kind of carbon dioxide purifying technique according to claim 1 is characterized in that: described pressure-swing absorption apparatus is that normal pressure is resolved or vacuum analysis.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100541450A CN102538395A (en) | 2012-03-05 | 2012-03-05 | Carbon dioxide purification technology |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100541450A CN102538395A (en) | 2012-03-05 | 2012-03-05 | Carbon dioxide purification technology |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104192845A (en) * | 2014-09-15 | 2014-12-10 | 杨皓 | Comprehensive utilization technology for producing distillate gas in liquid carbon dioxide purifying tower from pressure swing adsorption decarbonization tail gas |
| CN105513661A (en) * | 2016-01-15 | 2016-04-20 | 中国科学技术大学 | Cleaning waste gas pressure swing adsorption purification and recycling method and device for fusion reactor hot room |
| CN106430194A (en) * | 2016-10-10 | 2017-02-22 | 浙江海天气体有限公司 | Purification equipment for high-purity carbon dioxide |
| CN110801639A (en) * | 2019-11-11 | 2020-02-18 | 杭州快凯高效节能新技术有限公司 | Method for recovering carbon dioxide by multistage liquefaction and fractional refrigeration of industrial tail gas |
| CN114413568A (en) * | 2022-02-25 | 2022-04-29 | 华陆工程科技有限责任公司 | Three-stage compression expansion driven industrial tail gas carbon dioxide recovery cold box device |
| CN114669167A (en) * | 2022-02-16 | 2022-06-28 | 苏州市兴鲁空分设备科技发展有限公司 | Pressure swing adsorption and desorption gas recycling device |
| CN115448313A (en) * | 2022-09-26 | 2022-12-09 | 北京北大先锋科技股份有限公司 | Method and device for separating and recovering industrial carbon dioxide from gas of steel mill |
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Application publication date: 20120704 |