WO2024052279A1 - Air separation unit and air separation method - Google Patents
Air separation unit and air separation method Download PDFInfo
- Publication number
- WO2024052279A1 WO2024052279A1 PCT/EP2023/074169 EP2023074169W WO2024052279A1 WO 2024052279 A1 WO2024052279 A1 WO 2024052279A1 EP 2023074169 W EP2023074169 W EP 2023074169W WO 2024052279 A1 WO2024052279 A1 WO 2024052279A1
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- WIPO (PCT)
- Prior art keywords
- nitrogen
- oxygen
- rectification column
- gas
- drawn
- Prior art date
Links
- 238000000926 separation method Methods 0.000 title claims abstract description 51
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 503
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 342
- 239000001301 oxygen Substances 0.000 claims abstract description 342
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 342
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 230
- 239000007788 liquid Substances 0.000 claims abstract description 168
- 239000007789 gas Substances 0.000 claims abstract description 89
- 239000006200 vaporizer Substances 0.000 claims abstract description 86
- 229910001873 dinitrogen Inorganic materials 0.000 claims abstract description 43
- 239000003507 refrigerant Substances 0.000 claims abstract description 28
- 238000000034 method Methods 0.000 claims abstract description 22
- 230000008016 vaporization Effects 0.000 claims abstract description 6
- 239000002912 waste gas Substances 0.000 claims description 22
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 12
- 229910001882 dioxygen Inorganic materials 0.000 claims description 12
- 238000001704 evaporation Methods 0.000 description 19
- 230000008020 evaporation Effects 0.000 description 19
- 238000001816 cooling Methods 0.000 description 16
- 238000004519 manufacturing process Methods 0.000 description 9
- 230000006837 decompression Effects 0.000 description 8
- 238000000605 extraction Methods 0.000 description 8
- 238000011144 upstream manufacturing Methods 0.000 description 6
- 238000005259 measurement Methods 0.000 description 5
- 238000009529 body temperature measurement Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 238000009530 blood pressure measurement Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000011555 saturated liquid Substances 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
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
- F25J3/04—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 for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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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
- F25J3/04—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 for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
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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
- F25J3/04—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 for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/0423—Subcooling of liquid process streams
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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
- F25J3/04—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 for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04236—Integration of different exchangers in a single core, so-called integrated cores
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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
- F25J3/04—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 for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
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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
- F25J3/04—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 for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
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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
- F25J3/04—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 for air
- F25J3/04406—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 for air using a dual pressure main column system
- F25J3/0443—A main column system not otherwise provided, e.g. a modified double column flowsheet
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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
- F25J3/04—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 for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04793—Rectification, e.g. columns; Reboiler-condenser
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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
- F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
- F25J2200/94—Details relating to the withdrawal point
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/10—Boiler-condenser with superposed stages
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
Definitions
- the present invention relates to a method and a separation unit for producing high- purity nitrogen and high-purity oxygen by separating air.
- an oxygen-containing liquid drawn from the nitrogen rectification column is rectified in an oxygen rectification column.
- the oxygencontaining liquid is supplied to an upper portion of the rectification column, and high- purity oxygen is collected in an oxygen rectification column bottom portion by means of a rectifying operation with a vapour stream supplied by an oxygen vaporizer in the rectification column bottom portion.
- a portion of the feed air or the oxygen-containing liquid e.g., see Patent Document 2
- an oxygen-rich liquid drawn from the nitrogen rectification column bottom portion may be used as a heat medium in the oxygen vaporizer.
- the liquid drawn from the nitrogen rectification column i.e., the oxygen-containing liquid or oxygen-rich liquid
- the liquid drawn from the nitrogen rectification column is a saturated liquid at the time when it is drawn from the nitrogen rectification column, so a portion of this liquid evaporates when the liquid is decompressed, which leads to a process loss. It is therefore preferable for the liquid to be cooled before being decompressed in order to reduce the amount of evaporation during decompression.
- the oxygen-rich liquid may be cooled by means of nitrogen drawn from the nitrogen rectification column, or a waste gas vaporized in the nitrogen condenser, etc. (e.g., see US 5711167 A), or the oxygen-rich liquid may also be cooled by means of the oxygen vaporizer (e.g., see US 2010/0242537 A1 and WO 2014/173496 A23).
- the vaporization capacity of the oxygen vaporizer is an important factor in determining the amount of high-purity oxygen which is produced.
- a portion of the feed air is supplied to the oxygen vaporizer, so it would seemingly be possible to freely set the vaporization capacity, but supplying the feed air to the oxygen vaporizer causes a relative reduction in the amount of feed air supplied to the nitrogen rectification column, which is therefore undesirable from the point of view of nitrogen production.
- the oxygen-rich liquid is cooled by means of the oxygen vaporizer, but when there is a reduction in thermal demand in the oxygen vaporizer, the oxygen-rich liquid may be supplied downstream without having been sufficiently cooled, and a portion of the liquid may evaporate during decompression, giving rise to thermal loss.
- the present disclosure provides an air separation unit and an air separation method capable of increasing the amount of production of high-purity nitrogen and high-purity oxygen as compared to the conventional systems described above.
- Afirst air separation method according to the present disclosure comprises:
- a nitrogen rectification column into which the feed air is introduced; at least one nitrogen condenser for condensing nitrogen gas drawn from a column top portion of the nitrogen rectification column;
- the method above may comprise: i) a portion of an oxygen-enriched liquid drawn from the nitrogen rectification column is supplied to the nitrogen condenser after being cooled in the oxygen vaporizer, and the remainder of the oxygen-enriched liquid is supplied to the nitrogen condenser after being cooled in the sub-cooler (7) which uses, as a refrigerant, at least one of nitrogen gas supplied from the nitrogen rectification column and a gas supplied from a refrigerant side of the nitrogen condenser or ii) an oxygen-enriched liquid drawn from the nitrogen rectification column is cooled in the sub-cooler (7) which uses, as a refrigerant, at least one of nitrogen gas supplied from the nitrogen rectification column and a gas supplied from a refrigerant side of the nitrogen condenser, and is cooled in the oxygen vaporizer, then supplied to the nitrogen condenser.
- the method may comprise:
- the method above thus may comprise:
- the method above may comprise:
- a second air separation method according to the present disclosure constitutes:
- a nitrogen rectification column into which the feed air is introduced; at least one nitrogen condenser for condensing nitrogen gas drawn from a column top of the nitrogen rectification column;
- the method comprises a step (two-stage cooling step) in which an oxygenrich liquid drawn from a bottom portion of the nitrogen rectification column is cooled in the sub-cooler which uses, as a refrigerant, at least one of nitrogen gas supplied from the column top portion of the nitrogen rectification column and a gas supplied from a refrigerant side of the nitrogen condenser, and is cooled in the oxygen vaporizer , then supplied to the nitrogen condenser.
- the method above may comprise:
- the method above may comprise:
- Afirst air separation unit comprises:
- a nitrogen rectification column (comprising an intermediate or lower rectifying portion) into which the feed air that has passed through the main heat exchanger is introduced;
- At least one nitrogen condenser into which nitrogen gas (vaporized gas) drawn from a column top of the nitrogen rectification column is introduced, the at least one nitrogen condenser condensing (cooling) this gas and returning it to the column top portion;
- an expansion turbine for expanding a gas after the gas has been drawn from the at least one nitrogen condenser (column top portion of the first condenser) and passed through the sub-cooler and (a part of) the main heat exchanger;
- a compressor for compressing a recycled gas which is drawn from the at least one nitrogen condenser (column top portion of the second condenser) and compressed, then partially passes through the main heat exchanger , and then returns to the nitrogen rectification column;
- a high-purity oxygen rectification column comprising an oxygen rectifying portion or column top
- an oxygen-containing liquid including a gaseous form and a liquid form drawn from (an intermediate or upper rectifying portion of) the nitrogen rectification column
- an oxygen vaporizer which is arranged in a lower portion (of the oxygen rectifying portion) of the high-purity oxygen rectification column and serves to generate a vapour stream of oxygen gas;
- a nitrogen gas drawing pipeline forfeeding nitrogen gas (vaporized gas) drawn from the column top portion of the nitrogen rectification column to the sub-cooler and the main heat exchanger;
- a waste gas drawing pipeline for feeding, to the sub-cooler and the main heat exchanger , a gas drawn from the at least one nitrogen condenser (column top portion of the first condenser) which is passed through the sub-cooler and (a part of) the main heat exchanger and used in the expansion turbine;
- the unit may comprise:
- the unit may comprise: • a pipeline for feeding the oxygen-containing liquid drawn from the nitrogen rectification column to the column top portion of the high-purity oxygen rectification column.
- the unit may comprise:
- the unit may comprise:
- a second air separation unit according to the present disclosure comprises:
- a nitrogen rectification column (comprising an intermediate or lower rectifying portion) into which the feed air that has passed through the main heat exchanger is introduced;
- At least one nitrogen condenser into which nitrogen gas (vaporized gas) drawn from a column top of the nitrogen rectification column is introduced, the at least one nitrogen condenser condensing (cooling) this gas and returning it to the column top portion;
- an expansion turbine for expanding a gas after the gas has been drawn from the at least one nitrogen condenser (column top portion of the first condenser) and passed through the sub-cooler and (a part of) the main heat exchanger;
- a compressor for compressing a recycled gas which is drawn from the at least one nitrogen condenser (column top portion of the second condenser) and compressed, then partially passes through the main heat exchanger, and then returns to the nitrogen rectification column;
- a high-purity oxygen rectification column comprising an oxygen rectifying portion or column top
- an oxygen-containing liquid including a gaseous form and a liquid form drawn from (an intermediate or upper rectifying portion of) the nitrogen rectification column
- an oxygen vaporizer which is arranged in a lower portion (of the oxygen rectifying portion) of the high-purity oxygen rectification column and serves to generate a vapour stream of oxygen gas;
- a waste gas drawing pipeline for feeding, to the sub-cooler and the main heat exchanger, a gas drawn from the at least one nitrogen condenser (column top portion of the first condenser) which is passed through the sub-cooler and (a part of) the main heat exchanger and used in the expansion turbine;
- the unit may comprise:
- the unit may comprise:
- the unit may comprise:
- the unit may comprise:
- a third air separation unit according to the present disclosure comprises:
- a nitrogen rectification column (comprising an intermediate or lower rectifying portion) into which the feed air that has passed through the main heat exchanger is introduced;
- At least one nitrogen condenser into which nitrogen gas (vaporized gas) drawn from a column top of the nitrogen rectification column is introduced, the at least one nitrogen condenser condensing (cooling) this gas and returning it to the column top portion;
- an expansion turbine for expanding a gas after the gas has been drawn from the at least one nitrogen condenser (column top portion of the first condenser) and passed through the sub-cooler and (a part of) the main heat exchanger;
- a compressor for compressing a recycled gas which is drawn from the at least one nitrogen condenser (column top portion of the second condenser) and compressed, then partially passes through the main heat exchanger , and then returns to the nitrogen rectification column;
- a high-purity oxygen rectification column comprising an oxygen rectifying portion or column top
- an oxygen-containing liquid including a gaseous form and a liquid form drawn from (an intermediate or upper rectifying portion of) the nitrogen rectification column
- an oxygen vaporizer which is arranged in a lower portion (of the oxygen rectifying portion) of the high-purity oxygen rectification column and serves to generate a vapour stream of oxygen gas;
- a nitrogen gas drawing pipeline forfeeding nitrogen gas (vaporized gas) drawn from the column top portion of the nitrogen rectification column to the sub-cooler and the main heat exchanger;
- a waste gas drawing pipeline for feeding, to the sub-cooler and the main heat exchanger , a gas drawn from the at least one nitrogen condenser (column top portion of the first condenser) which is passed through the sub-cooler and (a part of) the main heat exchanger and used in the expansion turbine;
- the unit may comprise:
- the unit may comprise, instead of the pipeline:
- the unit may comprise:
- a pressurization apparatus for pressurizing the high-purity oxygen liquid drawn from the bottom portion of the high-purity oxygen rectification column; and • an extraction pipeline through which a high-purity oxygen liquid drawn from the bottom portion of the high-purity oxygen rectification column is fed to the sub-cooler and the main heat exchanger via the pressurization apparatus.
- the high-purity oxygen liquid extracted by the extraction pipeline may be passed through the main heat exchanger (vaporized) to form oxygen gas which is then fed to a point of demand.
- the air separation units may comprise:
- the air separation units may comprise:
- a compressor-expander which includes the expansion turbine and the compressor. At least a portion of the power obtained by the expansion turbine is used as power for the compressor, whereby power that can be recovered in the expansion turbine can be efficiently utilized.
- “High-purity oxygen” means oxygen having a purity of 99.99% or greater, for example.
- “High-purity nitrogen” means nitrogen having a purity of 99.99% or greater, for example.
- the oxygen-rich liquid drawn from the nitrogen rectification column is cooled in the oxygen vaporizer while at the same time being cooled in the sub-cooler which uses, as a refrigerant, nitrogen gas supplied from the nitrogen rectification column and waste gas supplied from a refrigerant side of the nitrogen condenser, and, as a result, the oxygen-rich liquid can be sufficiently cooled and thermal efficiency can be improved, even if thermal demand in the oxygen vaporizer varies.
- the oxygen-containing liquid is further cooled by means of heat exchange with waste gas in the oxygen rectification column which is drawn from the oxygen rectification column, thereby making it possible to further reduce evaporation loss associated with decompression.
- the oxygen-containing liquid is cooled at the same time as being utilized as a heat medium in the oxygen vaporizer, thereby enabling a reduction in evaporation loss arising as a result of decompression when the oxygen-containing liquid is introduced into the oxygen rectification column, and the amount of vapour produced in the oxygen vaporizer is increased, which therefore also contributes to increasing the amount of production of high-purity oxygen.
- FIG. 1 A shows an air separation unit according to embodiment 1 .
- FIG. 1 B shows an air separation unit according to a different mode of embodiment 1 .
- FIG. 2 shows an air separation unit according to embodiment 2.
- FIG. 3A shows an air separation unit according to embodiment 3.
- FIG. 3B shows an air separation unit according to a different mode of embodiment 3.
- FIG. 4 shows an air separation unit according to embodiment 4.
- FIG. 5 shows an air separation unit according to embodiment 5.
- FIG. 6 shows an air separation unit according to embodiment 6.
- Feed air is introduced into a main heat exchanger 1 where heat exchange is performed.
- a sub-cooler 7 has a different heat exchange function from the main heat exchanger 1 .
- the main heat exchanger 1 and the sub-cooler 7 are depicted as being connected in fig. 1A but their heat exchange functions are separate.
- refrigerants in the sub-cooler 7 are at least: nitrogen gas supplied from a column top portion 23 of a nitrogen rectification column 2, and a gas supplied from a column top portion 31 (refrigerant side) of a first condenser 3.
- the feed air that has passed through the main heat exchanger 1 is introduced into the nitrogen rectification column 2.
- the nitrogen rectification column 2 comprises a bottom portion 21 , a rectifying portion 22, and a column top portion 23.
- a feed air pipeline L1 passes the feed air through the main heat exchanger 1 and introduces the feed air into a lower rectifying portion 221 of the nitrogen rectification column 2.
- Nitrogen gas (nitrogen-rich gas) drawn from the column top 23 of the nitrogen rectification column 2 is passed, by way of a nitrogen gas pipeline L23, through the sub-cooler 7 and the main heat exchanger 1 , from which it is drawn as product nitrogen.
- Nitrogen gas (vaporized gas) drawn from the column top portion 23 of the nitrogen rectification column 2 is introduced into the first condenser 3 which condenses (cools) this gas.
- the nitrogen gas is fed by means of a pipeline L231 from the column top portion 23 to the first condenser 3 where it is cooled and then returned to the column top portion 23.
- Nitrogen gas (vaporized gas) drawn from the column top portion 23 of the nitrogen rectification column 2 is introduced into a second condenser 4 which condenses (cools) this gas.
- the nitrogen gas is fed by means of a pipeline L232 from the column top portion 23 to the second condenser 4 where it is cooled and then returned to the column top portion 23.
- a pressure on the refrigerant side of the first condenser 3 is lower than a pressure on the refrigerant side of the condenser 4.
- a high-pressure oxygen-rich liquid concentrated in the second condenser 4 is decompressed by a decompression valve and then fed to the first condenser 3 as a low-pressure refrigerant.
- a compressor 91 and an expansion turbine 92 function as a compressor-expander 9.
- the expansion turbine 92 expands a gas drawn from the column top portion 31 of the first condenser 3, after the gas has passed through the sub-cooler 7 and a part of the main heat exchanger 1 .
- the expanded gas passes through the sub-cooler 7 and the main heat exchanger 1 , and is treated as waste gas.
- a waste gas pipeline L31 the gas which is drawn from the column top 31 of the first condenser 3 is passed through the sub-cooler 7 and a part of the main heat exchanger 1 , expanded in the expansion turbine 92, and then passed through the sub-cooler 7 and the main heat exchanger 1 , from which it is drawn.
- the compressor 91 compresses the gas drawn from a column top portion 41 of the second condenser 4.
- the compressed gas passes through a part of the main heat exchanger 1 and is introduced into a gas phase in the bottom portion 21 of the nitrogen rectification column 2.
- a recycling pipeline L41 the gas which is drawn from the column top portion 41 of the second condenser 4 is compressed by the compressor 91 , passed through a part of the main heat exchanger 1 , and introduced into the gas phase in the bottom portion 21 of the nitrogen rectification column 2
- An oxygen-containing liquid (including a gaseous form and a liquid form) drawn from an intermediate rectifying portion 222 of the nitrogen rectification column 2 is supplied to a high-purity oxygen rectification column 5.
- the high-purity oxygen rectification column 5 includes a lower portion 51 , a rectifying portion 52, and a column top portion 53.
- An oxygen vaporizer is installed in the lower portion 51 of the high-purity oxygen rectification column 5 and generates a vapour stream of oxygen gas.
- a pipeline L22 draws the oxygen-containing liquid from the intermediate rectifying portion 222 of the nitrogen rectification column 2 and feeds the liquid into the column top portion 53 of the high-purity oxygen rectification column 5.
- a pipeline L53 draws the gas from the column top portion 53 of the high-purity oxygen rectification column 5 and merges into the waste gas pipeline L31 upstream of the main heat exchanger 1.
- An extraction pipeline L51 is a pipeline for extracting a high-purity oxygen liquid from the bottom portion 51 of the high-purity oxygen rectification column 5.
- the extraction pipeline L51 may be a pipeline for feeding the high-purity oxygen liquid to only either one of the sub-cooler 7 or the main heat exchanger 1 , or the pipeline L51 may be a pipeline for feeding to both, or it may function as a pipeline for supplying the high-purity oxygen liquid as a high-purity oxygen gas product.
- a means for increasing the pressure of the high-purity oxygen liquid may be provided before the high-purity oxygen liquid is fed to the sub-cooler 7 or to the main heat exchanger 1 .
- a portion of the oxygen-rich liquid drawn from a bottom portion 211 of the nitrogen rectification column 2 is supplied to the second condenser 4 after being cooled in the oxygen vaporizer s, and the remainder of the oxygen-rich liquid is supplied to the second condenser 4 after being cooled in the sub-cooler 7 which uses, as a refrigerant, nitrogen gas supplied from the column top portion 23 of the nitrogen rectification column 2 and a gas supplied from the column top portion 31 (refrigerant side) of the first condenser 3.
- the high-purity oxygen liquid drawn from the high-purity oxygen rectification column 5 also functions as a refrigerant.
- a pipeline L100a is a pipeline for feeding a part of the oxygen-rich liquid drawn from the bottom portion 21 of the nitrogen rectification column 2 by a pipe L100 to the subcooler 7, and feeding same to the second condenser 4.
- a pipeline L100b is a pipeline forfeeding the remainder of the oxygen-rich liquid drawn from the bottom portion 21 of the nitrogen rectification column 2 by the pipe L100 as a heat source in the oxygen vaporizer 6, and feeding same to the second condenser 4.
- the nitrogen gas drawing pipeline L23 is a pipeline for feeding nitrogen gas (vaporised gas) drawn from the column top portion 23 of the nitrogen rectification column 2 to the sub-cooler 7 and the main heat exchanger 1 .
- a control unit 110 determines a flow rate of the oxygen-rich liquid fed to the oxygen vaporizer 6 and controls the flow rate of the oxygen-rich liquid so as to supply a quantity of heat corresponding to a target amount of evaporation in the oxygen vaporizer 6. It should be noted that the target amount of evaporation is set in accordance with a production amount of product high-purity oxygen, and a process balance in the nitrogen rectification column 2 and the high-purity oxygen rectification column 5.
- the amount of evaporation in the oxygen vaporizer 6 may be obtained from a pressure in the high-purity oxygen rectification column 5, a production amount of the product high-purity oxygen collected in the bottom portion 51 , or a purity of the product high-purity oxygen.
- the pressure in the high-purity oxygen rectification column 5 may be measured in the column top portion 53, the rectifying portion (intermediate portion) 52, or the lower portion 51 .
- the production amount of the product high-purity oxygen may be measured by a flowmeter arranged in the extraction pipeline L51 for drawing the product high-purity oxygen, or it may be calculated from a liquid level gauge in the lower portion 51 of the high-purity oxygen rectification column 5.
- the purity of the product high-purity oxygen may be the measured purity of oxygen liquid collected in the lower portion 51 of the high-purity oxygen rectification column 5, or it may be measured by drawing oxygen gas from the gas phase portion in the lower portion 51 .
- the flow rate of the oxygen-rich liquid may be determined by means of a heat capacity of the oxygen-rich liquid, and a difference between an inlet temperature (measured by a thermometer) and an outlet temperature (measured by a thermometer) in the oxygen vaporizer 6.
- the heat capacity of the oxygen-rich liquid may be estimated from temperature-pressure-composition, and an average value in an assumed operating range may be used as a constant.
- the flow rate of the oxygen-rich liquid fed to the oxygen vaporizer 6 is measured by a flowmeter F1 provided in the pipeline L101 b.
- the flowmeter F1 may be a differential pressure flowmeter, a vortex flowmeter, or a mass flowmeter, etc., for example.
- the flow rate of the oxygen-rich liquid may be calculated from a difference between an indicated value of an oxygen-containing liquid flowmeter (flowmeter provided in the pipe L22) and an indicated value of a flowmeter for waste gas from the high-purity oxygen rectification column 5 (flowmeter provided in the pipe L53).
- the control unit 110 controls the flow rate by adjusting a first control valve V1 provided in the pipeline L1 OOb so that the measurement result (flow rate) at the flowmeter F1 enables a quantity of heat corresponding to the target amount of evaporation to be supplied, in other words, the control unit 110 controls the amount of evaporation by adjusting the quantity of heat supplied.
- the control unit 110 may also control the flow rate of oxygen-rich liquid circulating through the pipeline L100a by adjusting a second control valve V2 provided in the pipeline L100a, in addition to the first control valve V1.
- the flow rate of the oxygen-rich liquid is controlled once the inlet temperature and the outlet temperature of the oxygen-rich liquid circulating through the oxygen vaporizers have been stabilised.
- the inlet temperature of the oxygen-rich liquid in the oxygen vaporizer 6 is equal to a saturation temperature in the bottom portion 21 of the nitrogen rectification column 2, and is unaffected by the oxygen-rich liquid in the sub-cooler 7. This means that the remaining oxygen-rich liquid which is not supplied to the oxygen vaporizer 6, out of the oxygen-rich liquid drawn from the bottom portion 21 of the nitrogen rectification column 2, can be fed to the sub-cooler 7 for cooling, while operability of the oxygen vaporizer 6 is maintained.
- This different mode comprises a bypass pipeline L100b1 .
- the bypass pipeline L100b1 branches from the pipeline L100b upstream from the oxygen vaporizers and merges with the pipeline L100b downstream from the oxygen vaporizer 6, without passing through the oxygen vaporizer 6.
- a control valve V11 is provided in the pipeline L100b upstream from the oxygen vaporizer 6, and a control valve V12 is provided in the bypass pipeline L100b1.
- the control unit 110 performs control as in embodiment 1. Furthermore, the control unit 110 controls the control valve V11 to close and the control valve V12 to open, and the oxygen-rich liquid is fed to the bypass pipeline L100b1. As a result, even if the amount of evaporation in the oxygen vaporizer 6 is excessive, a part of the oxygenrich liquid is allowed to circulate to the bypass pipeline L100b1 while the oxygen-rich liquid in the sub-cooler 7 is stably cooled, and the amount of evaporation in the oxygen vaporizer 6 can be appropriately regulated as a result.
- An air separation unit A1 according to embodiment 2 will be described with the aid of fig. 2.
- the air separation unit A1 of embodiment 2 has a different configuration from that of the air separation unit A1 of embodiment 1 in that a second heat exchanger 8 is provided.
- Components which are the same as those of embodiment 1 will not be described or will only be briefly described.
- the second heat exchanger 8 performs heat exchange between the oxygencontaining liquid drawn from the intermediate rectifying portion 222 of the nitrogen rectification column 2, and a gas drawn from the column top portion 53 of the high- purity oxygen rectification column 5.
- a pipeline L101 is a pipeline for feeding the oxygen-containing liquid drawn from the nitrogen rectification column 2 to the column top portion 53 of the high-purity oxygen rectification column 5 via the second heat exchanger 8.
- the oxygen-containing liquid is further cooled by the second heat exchanger 8, thereby making it possible to reduce evaporation loss associated with decompression.
- the air separation unit A2 according to embodiment 3 will be described with the aid of fig. 3A.
- the air separation unit A2 of embodiment 3 has a different configuration from that of the air separation unitAI of embodiment 1 in that a pipeline L100c is provided, without the pipelines L100a and L100b being provided. Components which are the same as those of embodiment 1 will not be described or will only be briefly described.
- the pipeline L100c is a pipeline for feeding the oxygen-rich liquid drawn from the bottom portion 21 of the nitrogen rectification column 2 to the sub-cooler 7, then feeding the oxygen-rich liquid as a heat source in the oxygen vaporizer 6, and next feeding same to the second condenser 4.
- the oxygen-rich liquid drawn from the bottom portion 21 of the nitrogen rectification column 2 is cooled in the sub-cooler 7 which uses, as a refrigerant, nitrogen gas supplied from the column top portion 23 of the nitrogen rectification column 2 and a gas supplied from the column top portion 31 (refrigerant side) of the first condenser 3, then cooled in the oxygen vaporizer s, and then supplied to the second condenser 4.
- a control unit 120 determines a flow rate of the oxygen-rich liquid fed to the oxygen vaporizer 6 and controls the flow rate of the oxygen-rich liquid so as to supply a quantity of heat corresponding to a target amount of evaporation in the oxygen vaporizer 6. It should be noted that the target amount of evaporation is set in accordance with a production amount of product high-purity oxygen, and a process balance in the nitrogen rectification column 2 and the high-purity oxygen rectification column 5.
- the control unit 120 controls the flow rate of the oxygen-rich liquid so as to stabilize the temperature of the oxygen-rich liquid at the inlet of the oxygen vaporizer 6.
- the amount of oxygen-rich liquid cooled in the sub-cooler 7 is controlled to a constant level.
- the flow rate of the oxygen-rich liquid supplied to the oxygen vaporizers is measured by a flowmeter F2 provided in the pipeline L100c.
- the control unit 120 controls the flow rate by adjusting a control valve V3 provided in the pipeline L100c so that the measurement result (flow rate) at the flowmeter F2 enables a quantity of heat corresponding to the target amount of evaporation to be supplied, in other words, the control unit 120 controls the amount of evaporation by adjusting the quantity of heat supplied.
- This different mode comprises a bypass pipeline L100c1 .
- the bypass pipeline L100c1 branches from the pipeline L100c upstream from the oxygen vaporizers and merges with the pipeline L100c downstream from the oxygen vaporizer 6, without passing through the oxygen vaporizer 6.
- a valve V4 is provided in the pipeline L100c upstream from the oxygen vaporizer 6, and a valve V5 is provided in the bypass pipeline L100c1.
- the control unit 120 performs control as in embodiment 3. Furthermore, the control unit 120 controls the valve V4 to close and the valve V5 to open, and the oxygen-rich liquid is fed to the bypass pipeline L100c1. As a result, even if the amount of evaporation in the oxygen vaporizer 6 is excessive, the oxygen-rich liquid is allowed to circulate to the bypass pipeline L100c1 while the oxygen-rich liquid in the subcooler 7 is stably cooled, and the amount of evaporation in the oxygen vaporizer 6 can be appropriately regulated as a result.
- the air separation unit A3 of embodiment 4 has a different configuration from that of the air separation unit A1 of embodiment 1 in that a pipeline L103 is provided, without the pipeline L22 being provided. Components which are the same as those of embodiment 1 will not be described or will only be briefly described.
- the pipeline L103 is a pipeline for drawing the oxygen-containing liquid from the intermediate rectifying portion 222 of the nitrogen rectification column, feeding this liquid as a heat source in the oxygen vaporizer 6, then feeding the liquid to the column top portion 53 of the high-purity oxygen rectification column 5.
- This configuration utilises two types of liquids as the heat source in the oxygen vaporizer 6, namely the oxygen-rich liquid and the oxygen-containing liquid.
- the oxygen-containing liquid is utilized as a heat medium and cooled in the oxygen vaporizer s, thereby enabling a reduction in evaporation loss arising as a result of decompression when the oxygen-containing liquid is introduced into the oxygen rectification column 5. That is to say, the amount of vapour produced in the oxygen vaporizers is increased, which therefore contributes to increasing the amount of production of high-purity oxygen.
- the air separation unit A3 of embodiment 5 has a different configuration from that of the air separation unit A3 of embodiment 4 in that a pipeline L104 is provided, without the pipeline L103 being provided. Components which are the same as those of embodiment 4 will not be described or will only be briefly described.
- the second heat exchanger 8 performs heat exchange between the oxygencontaining liquid drawn from the intermediate rectifying portion 222 of the nitrogen rectification column 2 and utilized as a heat medium in the oxygen vaporizers, and a gas drawn from the column top portion 53 of the high-purity oxygen rectification column 5.
- the pipeline L104 is a pipeline for feeding the oxygen-containing liquid drawn from the nitrogen rectification column 2 to the oxygen vaporizer 6, then feeding this liquid to the column top portion 53 of the high-purity oxygen rectification column 5 via the second heat exchanger 8.
- the oxygen-containing liquid is further cooled by the second heat exchanger 8, thereby making it possible to reduce evaporation loss associated with decompression.
- the air separation unit A3 of embodiment 6 has a different configuration from that of the air separation unit A3 of embodiment 5 in that a pressurization apparatus 65 is provided. Components which are the same as those of embodiment 5 will not be described or will only be briefly described.
- the pressurization apparatus 65 pressurizes the high-purity oxygen liquid drawn from the bottom portion in the lower portion 51 of the high-purity oxygen rectification column 5.
- the pressurized high-purity oxygen liquid is fed to the sub-cooler 7 and the main heat exchanger 1 via the extraction pipeline L51 , from where it can be extracted as high- pressure, high-purity oxygen gas.
- Embodiment 1 example in fig. 1
- Feed air is supplied to a warm end of the main heat exchanger 1 at 10.86 barA, a temperature of 55°C, and a flow rate of 1065 Nm 3 /h, cooled to -162°C, and then supplied to the nitrogen rectification column 2.
- Nitrogen gas is drawn from the column top portion 23 of the nitrogen rectification column 2 at 575 Nm 3 /h, warmed in the sub-cooler 7 and the main heat exchanger 1 , and then drawn out.
- An oxygen-rich liquid comprising 39% oxygen is drawn at 836 Nm 3 /h from the bottom portion 21 of the nitrogen rectification column 2, and 621 Nm 3 /h thereof is fed to the sub-cooler 7 and cooled to -171°C, then supplied to the second condenser 4.
- the other 215 Nm 3 /h is cooled to -177°C in the oxygen vaporizer 6 then supplied to the second condenser 4.
- Recycled air is generated in the second nitrogen condenser 4 at 6.5 barA and 417 Nm 3 /h, and the pressure is boosted to 10.8 barA in the compressor 91 , after which the recycled air is cooled in the main heat exchanger 1 then returned and recycled to the nitrogen rectification column 2.
- Waste gas is generated in the first condenser 3 at 5.1 barA and 419 Nm 3 /h, warmed to -137°C in the sub-cooler 7 and the main heat exchanger 1 , and then cooled while simultaneously being expanded in the expansion turbine 92, once again warmed in the sub-cooler 7 and the main heat exchanger 1 , and then treated as waste gas.
- an oxygen-containing liquid comprising 19% oxygen is drawn at 71 Nm 3 /h, decompressed to 1.5 barA, and then supplied to the column top portion 53 of the high-purity oxygen rectification column 5.
- a high-purity oxygen liquid is drawn at 4.3 Nm 3 /h from the bottom portion in the lower portion 51 of the high-purity oxygen rectification column 5.
- Waste gas is drawn from the column top portion 53 at 66.7 Nm 3 /h, mixed with the waste gas supplied from the expansion turbine 92, then warmed in the sub-cooler 7 and the main heat exchanger 1 and treated as waste gas.
- an oxygen-rich liquid drawn from the bottom portion of the nitrogen rectification column 2 is fed to the oxygen vaporizer 6 and then fed to the second condenser 4, without the sub-cooler 7 of embodiment 1 being provided.
- the configuration comprises only the pipeline L100b, without the pipeline L100a.
- the amount of high-purity oxygen liquid produced by the high-purity oxygen rectification column of the example was confirmed to be between 1.1 and 1.3 times that of the comparative example.
- the refrigerants in the sub-cooler 7 were at least: nitrogen gas supplied from the column top portion 23 of the nitrogen rectification column 2, and a gas supplied from the column top portion 31 (refrigerant side) of the first condenser 3, but as another embodiment, a pipeline by which the pipeline L31 feeds to the main heat exchanger 1 without passing through the sub-cooler 7, or a bypass pipe for feeding to the main heat exchanger 1 without passing through the sub-cooler 7 may further be provided. Furthermore, as another embodiment, a pipeline by which the nitrogen gas pipeline L23 feeds to the main heat exchanger 1 without passing through the sub-cooler 7, or a bypass pipe for feeding to the main heat exchanger 1 without passing through the sub-cooler 7 may further be provided.
- pressure regulators and flow rate controllers, etc. may be installed in each pipeline in order to regulate pressure and regulate flow rate.
- control valves and gate valves, etc. may be installed in each line.
- pressure regulators and temperature measurement devices, etc. may be installed in each column in order to regulate pressure and regulate temperature.
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JP2022141120A JP2024058676A (ja) | 2022-09-06 | 2022-09-06 | 空気分離装置および空気分離方法 |
JP2022-141120 | 2022-09-06 |
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WO2024052279A1 true WO2024052279A1 (en) | 2024-03-14 |
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PCT/EP2023/074169 WO2024052279A1 (en) | 2022-09-06 | 2023-09-04 | Air separation unit and air separation method |
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Citations (8)
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US5711167A (en) | 1995-03-02 | 1998-01-27 | Air Liquide Process & Construction | High efficiency nitrogen generator |
JP2001336876A (ja) * | 2000-05-29 | 2001-12-07 | Nippon Sanso Corp | 窒素製造方法及び装置 |
US20100242537A1 (en) | 2009-03-24 | 2010-09-30 | Linde Ag | Process and apparatus for cryogenic air separation |
WO2014173496A2 (de) | 2013-04-25 | 2014-10-30 | Linde Aktiengesellschaft | Verfahren zur gewinnung eines luftprodukts in einer luftzerlegungsanlage mit zwischenspeicherung und luftzerlegungsanlage |
EP3327393A1 (de) * | 2016-11-25 | 2018-05-30 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur gewinnung eines hochreinsauerstoffproduktstroms durch tieftemperaturzerlegung von luft |
DE202018006161U1 (de) * | 2018-10-23 | 2019-05-27 | Linde Aktiengesellschaft | Anlage zur Tieftemperaturzerlegung von Luft |
US20200182543A1 (en) * | 2017-05-31 | 2020-06-11 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Gas production system |
US20220260312A1 (en) * | 2019-11-26 | 2022-08-18 | Linde Gmbh | Process and plant for low-temperature fractionation of air |
-
2022
- 2022-09-06 JP JP2022141120A patent/JP2024058676A/ja active Pending
-
2023
- 2023-08-18 TW TW112131128A patent/TW202417794A/zh unknown
- 2023-09-04 WO PCT/EP2023/074169 patent/WO2024052279A1/en unknown
Patent Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
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US5711167A (en) | 1995-03-02 | 1998-01-27 | Air Liquide Process & Construction | High efficiency nitrogen generator |
JP2001336876A (ja) * | 2000-05-29 | 2001-12-07 | Nippon Sanso Corp | 窒素製造方法及び装置 |
US20100242537A1 (en) | 2009-03-24 | 2010-09-30 | Linde Ag | Process and apparatus for cryogenic air separation |
WO2014173496A2 (de) | 2013-04-25 | 2014-10-30 | Linde Aktiengesellschaft | Verfahren zur gewinnung eines luftprodukts in einer luftzerlegungsanlage mit zwischenspeicherung und luftzerlegungsanlage |
EP3327393A1 (de) * | 2016-11-25 | 2018-05-30 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur gewinnung eines hochreinsauerstoffproduktstroms durch tieftemperaturzerlegung von luft |
US20200182543A1 (en) * | 2017-05-31 | 2020-06-11 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Gas production system |
DE202018006161U1 (de) * | 2018-10-23 | 2019-05-27 | Linde Aktiengesellschaft | Anlage zur Tieftemperaturzerlegung von Luft |
US20220260312A1 (en) * | 2019-11-26 | 2022-08-18 | Linde Gmbh | Process and plant for low-temperature fractionation of air |
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JP2024058676A (ja) | 2024-04-26 |
TW202417794A (zh) | 2024-05-01 |
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