WO2022184646A1 - Procédé et appareil de liquéfaction d'un gaz riche en co2 - Google Patents
Procédé et appareil de liquéfaction d'un gaz riche en co2 Download PDFInfo
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- WO2022184646A1 WO2022184646A1 PCT/EP2022/054998 EP2022054998W WO2022184646A1 WO 2022184646 A1 WO2022184646 A1 WO 2022184646A1 EP 2022054998 W EP2022054998 W EP 2022054998W WO 2022184646 A1 WO2022184646 A1 WO 2022184646A1
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- Prior art keywords
- liquid
- flow
- heat exchanger
- subcooled
- product
- Prior art date
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- 238000000034 method Methods 0.000 title claims description 21
- 239000007788 liquid Substances 0.000 claims abstract description 151
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 92
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 46
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 27
- 238000004821 distillation Methods 0.000 claims abstract description 27
- 230000005514 two-phase flow Effects 0.000 claims abstract description 19
- 239000012535 impurity Substances 0.000 claims abstract description 10
- 239000000047 product Substances 0.000 claims description 24
- 239000012263 liquid product Substances 0.000 claims description 23
- 238000011144 upstream manufacturing Methods 0.000 claims description 7
- 230000008016 vaporization Effects 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 5
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims 1
- 229910052799 carbon Inorganic materials 0.000 claims 1
- 238000010792 warming Methods 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 description 21
- 239000012071 phase Substances 0.000 description 17
- 239000007789 gas Substances 0.000 description 16
- 238000003860 storage Methods 0.000 description 13
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 229910052786 argon Inorganic materials 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 238000011176 pooling Methods 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000010992 reflux 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0027—Oxides of carbon, e.g. CO2
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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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
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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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
- F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
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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
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
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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
- F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
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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
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
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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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/04—Mixing or blending of fluids with the feed 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/80—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
- 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
- F25J2230/30—Compression of the feed 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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/80—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass 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
- F25J2270/02—Internal refrigeration with liquid vaporising loop
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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
- F25J2270/80—Quasi-closed internal or closed external carbon dioxide 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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
Definitions
- the present invention relates to a process and an apparatus for liquefying a CO2-rich gas.
- the CO2 under pressure is liquefied and can be produced at low pressure but it is often desired to produce the CO2 also at medium pressure within the same unit.
- the separating zone, exchanges as well as the associated equipment would ideally be sized so as to be able to adapt according to demand.
- the present invention relates to a CO2-rich feed CO2 liquefaction process involving the CO2 itself in an open circuit or an external refrigeration cycle (ammonia or CO2 for example).
- the exchange zone which can be a brazed aluminum type exchanger, is sized so as to be able to produce liquid CO2 at medium pressure and therefore at medium temperature, but also at low pressure and therefore at low temperature.
- FR2995985 describes a process in which a liquid from a distillation column of a mixture containing carbon dioxide
- the pressure of the product sent to the storages is essentially an average pressure between 13 bara and 20 bara. This is the consequence of storage investment optimizations and the availability of large-scale low-pressure storage technologies. Indeed, medium pressure means storing at temperatures between -20°C and -35°C. On the contrary, recent studies show a growing interest in the development of the low pressure production chain (between 6 and 8 bara). This level of pressure makes it possible to reduce the quantity of material necessary for the manufacture of storage and therefore to increase the volume of liquid CO2 transported by sea. However, this assumes storing the CO2 at a lower temperature between -46 and -52°C.
- An object of the invention is to optimize the heat exchanger of a liquefaction process in order to be able to subcool a product and a refrigeration cycle liquid in the same passage.
- the invention also makes it possible to produce liquefied CO2 at two different pressures.
- a process for separating a flow containing at least 95% mol of carbon dioxide as well as at least one impurity lighter than carbon dioxide by distillation in which: i) The flow is cooled in a heat exchanger and separated in a distillation column or by a partial condensation step in a separator pot, ii) A liquid flow containing at least 99% is withdrawn from the bottom of the column or pot.
- Part of the liquid flow is sent to cool in the heat exchanger to form a subcooled liquid
- At least part of the subcooled liquid is expanded to produce a two-phase flow
- the two-phase flow to form a gas and a liquid and at least part of the liquid is sent to be heated in the heat exchanger by indirect heat exchange with at least part of the flow to be separated and with the at least part of the liquid to so us to cool, the at least part of the liquid vaporizing in the heat exchanger and vi)
- a) Part of the liquid from step v) is taken as the first liquid product, optionally after pressurization in a pump or b) taking part of the subcooled liquid as the first liquid product
- a second liquid product is produced by taking part of the bottom liquid from the column or pot without cooling it in the heat exchanger and preferably without expanding it and viii ) The first and second products are produced simultaneously.
- a process for separating a flow containing at least 95% mol of carbon dioxide as well as at least one impurity lighter than carbon dioxide by distillation in which according to a first and a second mode of operation: i) The flow is cooled in a heat exchanger and it is separated in a distillation column or a separator pot ii) A liquid flow containing at least 99% mol of carbon dioxide and iii) at least part of the liquid flow is sent to cool in the heat exchanger to form an undercooled liquid iv) at least part of the undercooled liquid is expanded to produce a two-phase flow, v ) The two-phase flow is separated to form a gas and a liquid and at least part of the liquid is sent to heat up in the heat exchanger by indirect heat exchange with at least part of the flow to be separated and with the at least a n part of the liquid to be subcooled, the at least part of the liquid vaporizing in the heat exchanger and vi) a) according to the first and a second mode of operation: i
- a common pump is used to bring a) During the first mode of operation i) Part of the subcooled liquid or ii) part of the liquid from step v) to its final pressure to form the first product and b) During the second mode of operation the portion of the uncooled bottom liquid in the heat exchanger to its final pressure to form the second product.
- an apparatus for separating a flow containing at least 95% mol of carbon dioxide as well as at least one impurity lighter than carbon dioxide by distillation comprising a heat exchanger heat (20), a distillation column (30) or a separator pot, expansion means (V3), means for sending the flow to cool in the heat exchanger, means for sending the cooled flow to separate in the distillation column or in the pot, means for withdrawing from the bottom of the column or the pot a liquid flow containing at least 99% mol of carbon dioxide, means for sending at least part (12) of the liquid flow cooled in the heat exchanger to form a subcooled liquid (3), means for sending at least part of the subcooled liquid to the expansion means to produce a two-phase flow, a phase separator (40) to separate the two-phase flow to form a gas and a liquid, means for sending at least a part (14) of the liquid from the phase separator to be heated in the heat exchanger by indirect heat exchange with at least part of the flow to be separated and
- the apparatus comprises means for sending vaporized liquid from the phase separator into the heat exchanger to mix with the flow to be separated upstream of the heat exchanger.
- the heat exchanger has two ends, one designed to operate at a hotter temperature than the other, the means for sending the flow to be separated in the exchanger to cool being connected to the end designed to operate at the hotter temperature and the means for sending the cooled stream to separate in the distillation column or in the pot being connected to the end designed to operate at the colder temperature.
- the heat exchanger has two ends, one designed to operate at a hotter temperature than the other, the means for sending at least part of the liquid flow to cool in the heat exchanger to form a subcooled liquid being connected to the end designed to operate at the cooler temperature.
- the heat exchanger has two ends, one designed to operate at a hotter temperature than the other, the means for sending at least part of the liquid from the phase separator to heat up in the heat exchanger being connected at the end designed to operate at the cooler temperature.
- the heat exchanger has two ends, one designed to operate at a hotter temperature than the other including means for drawing vaporized phase separator liquid into the heat exchanger from the end designed to operate at the hottest temperature.
- the apparatus comprises means for sending liquid from the vaporized phase separator into the heat exchanger to mix with the flow to be separated upstream of the heat exchanger.
- the apparatus comprises a common pump (55) to bring a) during the first period i) the part of the subcooled liquid or ii) a part of the liquid from step v) to its final pressure to form the first product and b ) During the second period the portion of the uncooled bottom liquid in the heat exchanger to its final pressure to form the second product.
- liquid product and the vaporized liquid are initially cooled together in the same passage(s) of the heat exchanger.
- the distillation column can include structured packings or trays.
- the apparatus may include a pump downstream of the phase separator.
- FIG.1] [FIG.2] and FIG.3] illustrate methods according to the invention.
- flow 1 containing at least 95 mol% carbon dioxide also contains at least one other impurity, such as oxygen, nitrogen, argon, carbon monoxide.
- Flow 1 is compressed in a compressor 10 to a first pressure higher than that of column 30 to form a compressed flow 2 at a first pressure.
- the lines connecting compressor 10 and exchanger 20 are dotted because if the flow is already under pressure, compressor 10 will not be necessary.
- the first pressure is higher by at least 1 bar than that of column 30, preferably by at least 10 bara, or even at least 20, 30 or 40 bars higher than that of column 30.
- the first pressure can be at least 35 bara.
- the column pressure can be 40 bara.
- the compressed flow 2 is cooled in the heat exchanger 20 with indirect exchange to form a cooled and liquefied flow at the first pressure.
- the cooled and liquefied flow is divided into two parts 4.6 in the heat exchanger. Part 4 exits heat exchanger 20 at an intermediate temperature T 1 thereof without having been expanded upstream of the splitting point.
- the two fractions 4.6 are at the first pressure higher than that of the column by at least 1 bar.
- the second fraction 6 continues its cooling to the cold end of the heat exchanger 20 to subcool it in the main heat exchanger to a minimum temperature close to the triple point of CO2. Then it is expanded to the pressure of column 30 in valve V2 and sent as a liquid flow to the top of distillation column 30.
- the column is a simple column, having no overhead condenser. It contains structured trays or packings and operates at a second pressure lower than the first pressure.
- the first fraction 4 is sent to column 30 after expansion from the first pressure to the pressure of column 30 in valve V1.
- the bottom liquid of column 30 contains at least 99 mol% carbon dioxide and is divided into two parts.
- Part 5 at the pressure of column 30 serves as a liquid product rich in carbon dioxide.
- Part 12 is sent to an intermediate level of exchanger 20 at a temperature lower than that at which flow 4 leaves the exchanger.
- Part 12 is subcooled in exchanger 20 to the cold end and then split in two.
- a fraction 3 is expanded in valve V3 to form a separate two-phase flow in a phase separator 40.
- the gaseous part 16 is heated in the exchanger 20 and is sent to the compressor 10.
- the liquid part 14 is vaporized and heated in the heat exchanger 20 from the cold end to the hot end. It can be divided into several parts which are expanded to different pressures, introduced at the cold end or at an intermediate point of the heat exchanger 20 and vaporized at different pressures, to optimize the heat exchange.
- the vaporization pressure of flow 14 can be greater than, equal to or lower than the pressure of flow 1 to be treated.
- the vaporized flow 18 is sent to an intermediate level of the compressor 10.
- Fraction 4 of subcooled liquid 12 is expanded in a valve V4 to bring it to a pressure lower than that of liquid 5.
- the column overhead gas 11 contains at least one impurity lighter than carbon dioxide such as oxygen, nitrogen and argon. It can heat up in the heat exchanger 20.
- the liquid 5 is sent to storage at a pressure between 10 and 40 bara, for example between 13 and 20 bara constituting the medium pressure product and the liquid 4 at between 6 and 8 bara constitutes the low pressure product.
- Column 30 operates at at least 10 bara, preferably between 10 and 40 bara, for example between 13 and 20 bara.
- the product 8 can be derived from the liquid of the phase separator 40.
- all the subcooled liquid 12 is expanded in a valve V3 to form a two-phase mixture.
- This mixture is separated in a phase separator 40, the gas being heated as for [Fig.1]; the liquid 8 is divided into two fractions, one 50 being vaporized in the heat exchanger and the rest 4 being pressurized in a pump P to form a product.
- liquid 4 can be produced at a pressure higher, lower or equal to that of product 5.
- the liquid 5 can be sent to storage at a pressure between 10 and 40 bara, for example between 13 and 20 bara constituting the medium pressure product and the liquid 4 at between 6 and 8 bara constitutes the low pressure product.
- the phase separator must be at a pressure between the pressure required for low pressure storage pressure, i.e. between 5.5 bara and 8 bara for storage at 7 bara, so it is necessary to use the pump P to reach the pressure of storage, in particular in the case where the installation constraints make it necessary to install the storage at a long distance from the liquefier.
- the invention can make it possible to modify the configuration of state-of-the-art liquefiers so that they can produce CO 2 in different modes and in an optimized manner:
- the liquefier In order to allow the modes with low pressure production, the liquefier must be dimensioned on the low production production only because it is the most restrictive case with respect to the sub-cooling of the production flow.
- This vaporized low-pressure CO 2 comes from the bottom of the distillation column, is subcooled before being expanded and injected into the heat exchanger.
- the invention mainly consists of pooling the subcooling pass of the bottom of the distillation column at the cold end of the exchanger for the production CO 2 and the cycle CO 2 . This avoids a “dry” pass when producing at medium pressure only. In low-pressure liquid production mode only or partially, this pass will process the cycle CO 2 as well as the production CO 2 to be subcooled. In medium pressure production mode only, this pass will only see the cycle CO 2 pass to undercool.
- FIG. 2 Another variant in [Fig, 2] consists in pooling the expansion valves and a separation pot in addition to the subcooling pass.
- a gas phase will be generated by low-pressure expansion of cycle CO2.
- a pot 40 is commonly used in order to separate the gas phase and the liquid phase before introduction into the exchanger.
- the generated liquid phase 8 can then also be partly used as low-pressure production. This makes it possible to use a single pot to separate the gas from the liquid from the cycle CO2 from that of the production.
- overhead gas 11 may or may not be reheated in the exchanger: the same is true for gas 16.
- a distillation column is described to effect the separation. It will be understood that at least one separator pot can replace the column or be arranged upstream of the column. In this case, the pot would be supplied by flow 4, flow 6 not existing. The liquid in the pot would be split into two parts to form flow rates 5, 12.
- the gas 11 from the pot would be sent to the atmosphere or reheated in the exchanger 20.
- FIG.3 shows a variant of the previous figures where the process makes it possible to produce a single liquid rich in carbon dioxide with a single pump but at two different pressures to choose from.
- the flow 5 must be pumped in order to obtain sufficient pressure on arrival at the storage. This is also true when, for constraints related to the installation or the size, the storages are installed at a certain distance from the liquefier.
- a pump 55 is installed on stream 5.
- the apparatus comprises a single pump 55 of liquid rich in carbon dioxide which can be fed alternately by one of two flow rates at two different pressures.
- valve V4 is closed and valve V5 is opened. All the liquid from the phase separator 40 is sent to vaporize in the exchanger 20.
- the bottom liquid 5 of the column is sent to the pump 55 at the pressure of the column 30 and is pumped to form a liquid 45 at a pressure higher.
- valve V4 is opened and valve V5 is closed. Part 14 of the liquid from the phase separator 40 is sent to vaporize in the exchanger 20. The rest 4 of the liquid passes through the valve V4 and arrives at the inlet of the pump 55 at a pressure lower than that of the column 30 and is pumped to form a liquid 45 at a lower pressure. Since valve V5 is closed, liquid 5 is not sent to pump 55.
- the pump 55 must therefore adapt to pressurizing the liquid from two different pressures to produce the liquid 45 at two different pressures.
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- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
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Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
KR1020237029500A KR20230154423A (ko) | 2021-03-04 | 2022-02-28 | Co2가 풍부한 가스의 액화 방법 및 장치 |
JP2023550175A JP2024509384A (ja) | 2021-03-04 | 2022-02-28 | Co2富化ガスを液化するための方法及び装置 |
EP22708161.9A EP4302028A1 (fr) | 2021-03-04 | 2022-02-28 | Procédé et appareil de liquéfaction d'un gaz riche en co2 |
AU2022230711A AU2022230711A1 (en) | 2021-03-04 | 2022-02-28 | Method and apparatus for liquefying a co2-rich gas |
CA3210124A CA3210124A1 (fr) | 2021-03-04 | 2022-02-28 | Procede et appareil de liquefaction d'un gaz riche en co2 |
Applications Claiming Priority (2)
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FR2102132A FR3120427B1 (fr) | 2021-03-04 | 2021-03-04 | Procédé et appareil de liquéfaction d’un gaz riche en CO2 |
FRFR2102132 | 2021-03-04 |
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WO2022184646A1 true WO2022184646A1 (fr) | 2022-09-09 |
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PCT/EP2022/054998 WO2022184646A1 (fr) | 2021-03-04 | 2022-02-28 | Procédé et appareil de liquéfaction d'un gaz riche en co2 |
Country Status (7)
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EP (1) | EP4302028A1 (fr) |
JP (1) | JP2024509384A (fr) |
KR (1) | KR20230154423A (fr) |
AU (1) | AU2022230711A1 (fr) |
CA (1) | CA3210124A1 (fr) |
FR (1) | FR3120427B1 (fr) |
WO (1) | WO2022184646A1 (fr) |
Citations (7)
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US20080156035A1 (en) * | 2004-07-16 | 2008-07-03 | Statoil Asa | Process and Apparatus for the Liquefaction of Carbon Dioxide |
US20130036765A1 (en) * | 2010-04-29 | 2013-02-14 | Total S.A. | Process for treating a natural gas containing carbon dioxide |
WO2013171426A2 (fr) * | 2012-05-15 | 2013-11-21 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé et appareil de distillation à température subambiante |
US20140026612A1 (en) * | 2011-04-11 | 2014-01-30 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and Apparatus for Liquefying a CO2-Rich Gas |
FR2995985A1 (fr) | 2012-09-25 | 2014-03-28 | Air Liquide | Procede et appareil de separation d'un melange contenant du dioxyde de carbone par distillation cryogenique |
US20170363351A1 (en) * | 2014-12-11 | 2017-12-21 | L'Air Liquide, Société Anonyme pour I'Etude et I'Exploitation des Procédés Georges Claude | Method and apparatus for separating a feed gas containing at least 20 mol % of co2 and at least 20 mol % of methane, by partial condensation and/or by distillation |
FR3088416A1 (fr) * | 2018-11-08 | 2020-05-15 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede et appareil de liquefaction d'un courant gazeux contenant du dioxyde de carbone |
-
2021
- 2021-03-04 FR FR2102132A patent/FR3120427B1/fr active Active
-
2022
- 2022-02-28 EP EP22708161.9A patent/EP4302028A1/fr active Pending
- 2022-02-28 CA CA3210124A patent/CA3210124A1/fr active Pending
- 2022-02-28 JP JP2023550175A patent/JP2024509384A/ja active Pending
- 2022-02-28 KR KR1020237029500A patent/KR20230154423A/ko unknown
- 2022-02-28 WO PCT/EP2022/054998 patent/WO2022184646A1/fr active Application Filing
- 2022-02-28 AU AU2022230711A patent/AU2022230711A1/en active Pending
Patent Citations (7)
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US20080156035A1 (en) * | 2004-07-16 | 2008-07-03 | Statoil Asa | Process and Apparatus for the Liquefaction of Carbon Dioxide |
US20130036765A1 (en) * | 2010-04-29 | 2013-02-14 | Total S.A. | Process for treating a natural gas containing carbon dioxide |
US20140026612A1 (en) * | 2011-04-11 | 2014-01-30 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and Apparatus for Liquefying a CO2-Rich Gas |
WO2013171426A2 (fr) * | 2012-05-15 | 2013-11-21 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé et appareil de distillation à température subambiante |
FR2995985A1 (fr) | 2012-09-25 | 2014-03-28 | Air Liquide | Procede et appareil de separation d'un melange contenant du dioxyde de carbone par distillation cryogenique |
US20170363351A1 (en) * | 2014-12-11 | 2017-12-21 | L'Air Liquide, Société Anonyme pour I'Etude et I'Exploitation des Procédés Georges Claude | Method and apparatus for separating a feed gas containing at least 20 mol % of co2 and at least 20 mol % of methane, by partial condensation and/or by distillation |
FR3088416A1 (fr) * | 2018-11-08 | 2020-05-15 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede et appareil de liquefaction d'un courant gazeux contenant du dioxyde de carbone |
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ASPELUND ET AL: "Gas conditioning-The interface between CO"2 capture and transport", 20070616, vol. 1, no. 3, 16 June 2007 (2007-06-16), pages 343 - 354, XP022119495 * |
Also Published As
Publication number | Publication date |
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CA3210124A1 (fr) | 2022-09-09 |
JP2024509384A (ja) | 2024-03-01 |
KR20230154423A (ko) | 2023-11-08 |
EP4302028A1 (fr) | 2024-01-10 |
FR3120427B1 (fr) | 2023-03-31 |
FR3120427A1 (fr) | 2022-09-09 |
AU2022230711A1 (en) | 2023-09-07 |
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