EP3092453B1 - Method and device for the liquefaction of a gaseous co2 stream - Google Patents

Method and device for the liquefaction of a gaseous co2 stream Download PDF

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Publication number
EP3092453B1
EP3092453B1 EP15701557.9A EP15701557A EP3092453B1 EP 3092453 B1 EP3092453 B1 EP 3092453B1 EP 15701557 A EP15701557 A EP 15701557A EP 3092453 B1 EP3092453 B1 EP 3092453B1
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European Patent Office
Prior art keywords
liquid
phase separator
flow
cooled
heat exchanger
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EP15701557.9A
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German (de)
French (fr)
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EP3092453A2 (en
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Nicolas CHAMBRON
Benoît DAVIDIAN
Arthur Darde
Mathieu LECLERC
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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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
    • 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
    • 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
    • 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
    • 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
    • F25J1/0203—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 a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
    • F25J1/0208—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 a single-component refrigerant [SCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop
    • 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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • 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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • 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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
    • 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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0294—Multiple compressor casings/strings in parallel, e.g. split arrangement
    • 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
    • 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
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • 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 for liquefying a current of gaseous CO 2 .
  • the current contains at least 95 mol% of CO2 or at least 99 mol% of CO2.
  • the invention consists of a process for liquefying a CO 2 stream containing impurities (for example H2, N2).
  • JP-A-64084087 it is known to JP-A-64084087 to liquefy a flow containing mainly CO 2 by drying the flow rate to be liquefied in a drier, by cooling it to partially liquefy it, by sending it to a first phase separator, by sending the liquid of the first phase separator to a second phase separator and extracting the liquefied flow of the second phase separator.
  • the gas of the second phase separator is reheated and sent upstream of the dryer.
  • This process does not allow the liquid produced to be subcooled, which is useful when the liquid is to be used at a pressure lower than the liquefaction pressure.
  • An object of the present invention is to overcome the defects of the prior art.
  • the liquefaction process of a flow 1 containing at least 95 mol%, or even at least 99 mol% of carbon dioxide is carried out by cooling by indirect heat exchange with a cold source.
  • the supply of CO 2 depending on its pressure, is made inter-stage of a cycle compressor 3, between the stages 3B and 3C.
  • the last two stages 3C, 3D of this compressor 3 compress the flow rate 1 until a sufficient pressure is obtained to condense the gaseous flow in front of the cold source 5 available on site (for example ice-cold water) in a heat exchanger of heat 7.
  • the first expansion in the valve V1 is preferentially done at the inlet pressure of the last 3D wheel of the cycle compressor 3.
  • the gas generated 4 following expansion of the relaxed equilibrium liquid from the phase separator S1 can be recycled upstream of the last wheel of the cycle compressor.
  • a second step of expansion of the liquid 14 of the phase separator S1 in a second valve V2 is preferably envisaged in order to reduce the pressure of the liquefied CO2, before entering the main exchanger 9, thus enabling a CAPEX gain on the same exchanger .
  • the expansion pressure is chosen to allow the recycling of a gas 6 of a second phase separator S2 upstream of the penultimate compression wheel 3C.
  • valves V1, V2 make it possible to cool the liquefied CO 2 while limiting the OPEX impact by recycling as much as possible in the last stages of compression.
  • the liquid CO2 stream 18 will enter a heat exchanger 9 to be strongly subcooled therein. After subcooling the liquid 18 is divided into two parts. Part 11 is expanded in a valve V3 to form a liquid product at the pressure required by the customer, typically 7 bara. A part 13 vaporizes against the liquid 18 in the heat exchanger 9, after expansion in a valve V4. The expansion in valve V4 brings the liquid up to a temperature as close as possible to that of the triple point (-56.5 ° C).
  • the CO 2 low vapor pressure 15 is then recycled to the first stages 3A, 3B of the cycle compressor 3 to ensure a liquefaction efficiency of 100%. Between stages 3B and 3C, it is mixed with flow 1.
  • the heat exchanger 9 mentioned above will be a tube and shell type heat exchanger (in English "Shell and Tubes"), with the flow 18 to be cooled in the tubes and the expanded liquid 13 at a pressure close to that of the triple point in the calender, in order to avoid any risk of accident, following a possible ice setting of this same current (especially in the case where the cycle compressor 3, in which will return the vaporized liquid 15, aspires too much and drop the pressure below that of the triple point of CO 2 ).

Description

La présente invention est relative à un procédé de liquéfaction d'un courant de CO2 gazeux. Le courant contient au moins 95% mol de CO2, voire au moins 99% mol de CO2.The present invention relates to a process for liquefying a current of gaseous CO 2 . The current contains at least 95 mol% of CO2 or at least 99 mol% of CO2.

L'invention consiste en un procédé permettant de liquéfier un courant de CO2 contenant des impuretés (par exemple H2, N2).The invention consists of a process for liquefying a CO 2 stream containing impurities (for example H2, N2).

Il est connu de JP-A-64084087 de liquéfier un débit contenant majoritairement du CO2 en séchant le débit à liquéfier dans un sécheur, en le refroidissant pour le liquéfier partiellement, en l'envoyant dans un premier séparateur de phases, en envoyant le liquide du premier séparateur de phases à un deuxième séparateur de phases et en extrayant le débit liquéfié du deuxième séparateur de phases. Le gaz du deuxième séparateur de phases est réchauffé et envoyé en amont du sécheur.It is known to JP-A-64084087 to liquefy a flow containing mainly CO 2 by drying the flow rate to be liquefied in a drier, by cooling it to partially liquefy it, by sending it to a first phase separator, by sending the liquid of the first phase separator to a second phase separator and extracting the liquefied flow of the second phase separator. The gas of the second phase separator is reheated and sent upstream of the dryer.

Ce procédé ne permet pas de sous-refroidir le liquide produit, ce qui se révèle utile quand le liquide doit être utilisé à une pression plus basse que la pression de liquéfaction.This process does not allow the liquid produced to be subcooled, which is useful when the liquid is to be used at a pressure lower than the liquefaction pressure.

US2008/173585 , US6301927 et US2013/340472 décrivent des procédés selon le préambule de la revendication 1. US2008 / 173585 , US6301927 and US2013 / 340472 describe methods according to the preamble of claim 1.

Un but de la présente invention est de pallier les défauts de l'art antérieur.An object of the present invention is to overcome the defects of the prior art.

Selon un objet de l'invention, il est prévu un procédé selon la revendication 1..According to one object of the invention, there is provided a method according to claim 1.

Selon d'autres aspects facultatifs :

  • un gaz du premier séparateur de phases est mélangé avec le débit gazeux d'alimentation à une première pression.
  • un gaz du deuxième séparateur de phases est mélangé avec le débit gazeux d'alimentation.
  • le gaz du deuxième séparateur de phases est mélangé avec le débit gazeux d'alimentation à une deuxième pression plus basse que la première pression.
  • le gaz du deuxième séparateur de phases est mélangé avec le débit gazeux d'alimentation en amont du premier étage de compression.
  • le liquide du premier séparateur de phases n'est pas refroidi en amont de la détente
  • le deuxième échangeur est un sous-refroidisseur final.
  • le produit final n'est pas refroidi en aval du deuxième échangeur.
  • aucune fraction du produit liquide n'est recyclée au premier étage de compression
  • la deuxième partie du liquide refroidi dans le deuxième échangeur est détendue dans une vanne et se réchauffe uniquement dans le deuxième échangeur de chaleur pour former un débit vaporisé
According to other optional aspects:
  • a gas of the first phase separator is mixed with the feed gas flow at a first pressure.
  • a gas of the second phase separator is mixed with the feed gas flow.
  • the gas of the second phase separator is mixed with the supply gas flow at a second pressure lower than the first pressure.
  • the gas of the second phase separator is mixed with the feed gas flow upstream of the first compression stage.
  • the liquid of the first phase separator is not cooled upstream of the trigger
  • the second exchanger is a final subcooler.
  • the final product is not cooled downstream of the second exchanger.
  • no fraction of the liquid product is recycled to the first stage of compression
  • the second portion of the cooled liquid in the second heat exchanger is expanded in a valve and heats only in the second heat exchanger to form a vaporized flow rate

L'invention sera décrite de manière plus détaillée en se référant à la figure.The invention will be described in more detail with reference to the figure.

Dans la figure 1, le procédé de liquéfaction d'un débit 1 contenant au moins 95% mol, voire au moins 99% mol de dioxyde de carbone s'effectue par refroidissement par échange de chaleur indirect avec une source froide. L'alimentation en CO2, en fonction de sa pression, est faite en inter-étage d'un compresseur de cycle 3, entre les étages 3B et 3C.In the figure 1 , the liquefaction process of a flow 1 containing at least 95 mol%, or even at least 99 mol% of carbon dioxide is carried out by cooling by indirect heat exchange with a cold source. The supply of CO 2 , depending on its pressure, is made inter-stage of a cycle compressor 3, between the stages 3B and 3C.

Les deux derniers étages 3C, 3D de ce compresseur 3 compriment le débit 1 jusqu'à atteindre une pression suffisante permettant de condenser le courant gazeux en face de la source froide 5 disponible sur site (par exemple de l'eau glacée) dans un échangeur de chaleur 7.The last two stages 3C, 3D of this compressor 3 compress the flow rate 1 until a sufficient pressure is obtained to condense the gaseous flow in front of the cold source 5 available on site (for example ice-cold water) in a heat exchanger of heat 7.

Le CO2 ainsi condensé à haute pression va subir une succession de détentes dans des vannes V1, V2, afin de s'auto-refroidir par génération d'un gaz.The CO 2 thus condensed at high pressure will undergo a succession of detents in valves V1, V2, in order to self-cool by generating a gas.

La première détente dans la vanne V1 se fera préférentiellement à la pression d'entrée de la dernière roue 3D du compresseur de cycle 3. Ainsi, le gaz généré 4 suite à la détente du liquide à l'équilibre détendu provenant du séparateur de phases S1 peut être recyclé en amont de la dernière roue du compresseur de cycle.The first expansion in the valve V1 is preferentially done at the inlet pressure of the last 3D wheel of the cycle compressor 3. Thus, the gas generated 4 following expansion of the relaxed equilibrium liquid from the phase separator S1 can be recycled upstream of the last wheel of the cycle compressor.

Une seconde étape de détente du liquide 14 du séparateur de phases S1 dans une seconde vanne V2 est préférentiellement envisagée afin de réduire la pression du CO2 liquéfié, avant d'entrée dans l'échangeur principal 9, permettant ainsi un gain CAPEX sur ce même échangeur. Là encore, la pression de détente est choisie afin de permettre le recyclage d'un gaz 6 d'un deuxième séparateur de phases S2 en amont de l'avant dernière roue 3C de compression.A second step of expansion of the liquid 14 of the phase separator S1 in a second valve V2 is preferably envisaged in order to reduce the pressure of the liquefied CO2, before entering the main exchanger 9, thus enabling a CAPEX gain on the same exchanger . Again, the expansion pressure is chosen to allow the recycling of a gas 6 of a second phase separator S2 upstream of the penultimate compression wheel 3C.

Cette succession de détentes dans les vannes V1, V2 permet de refroidir le CO2 liquéfié 18 tout en limitant l'impact OPEX en recyclant le plus possible dans les derniers étages de compressions.This succession of detents in the valves V1, V2 makes it possible to cool the liquefied CO 2 while limiting the OPEX impact by recycling as much as possible in the last stages of compression.

Une fois partiellement détendu et refroidi, le courant de CO2 liquide 18 va entrer dans un échangeur de chaleur 9 afin d'y être fortement sous-refroidi. Après sous-refroidissement le liquide 18 est divisé en deux parties. La partie 11 est détendue dans une vanne V3 pour former un produit liquide à la pression requise par le client, typiquement 7 bara. Une partie 13 se vaporise contre le liquide 18 dans l'échangeur de chaleur 9, après détente dans une vanne V4. La détente dans la vanne V4 amène le liquide jusqu'à atteindre une température la plus proche possible de celle du point triple (-56.5°C).Once partially expanded and cooled, the liquid CO2 stream 18 will enter a heat exchanger 9 to be strongly subcooled therein. After subcooling the liquid 18 is divided into two parts. Part 11 is expanded in a valve V3 to form a liquid product at the pressure required by the customer, typically 7 bara. A part 13 vaporizes against the liquid 18 in the heat exchanger 9, after expansion in a valve V4. The expansion in valve V4 brings the liquid up to a temperature as close as possible to that of the triple point (-56.5 ° C).

Le CO2 basse pression vaporisé 15 est ensuite recyclé aux premiers étages 3A, 3B du compresseur de cycle 3 afin d'assurer un rendement de liquéfaction de 100%. Entre les étages 3B et 3C, il est mélangé avec le débit 1.The CO 2 low vapor pressure 15 is then recycled to the first stages 3A, 3B of the cycle compressor 3 to ensure a liquefaction efficiency of 100%. Between stages 3B and 3C, it is mixed with flow 1.

L'échangeur de chaleur 9 mentionné ci-dessus sera un échangeur de type à tubes et à calandre (en anglais « Shell and Tubes »), avec le débit 18 à refroidir dans les tubes et le liquide détendu 13 à une pression proche de celle du point triple dans la calandre, afin d'éviter tout risque d'accident, suite à une éventuelle prise en glace de ce même courant (notamment dans le cas où le compresseur de cycle 3, dans lequel va retourner le liquide vaporisé 15, aspire trop et fasse chuter la pression en dessous de celle du point triple du CO2).The heat exchanger 9 mentioned above will be a tube and shell type heat exchanger (in English "Shell and Tubes"), with the flow 18 to be cooled in the tubes and the expanded liquid 13 at a pressure close to that of the triple point in the calender, in order to avoid any risk of accident, following a possible ice setting of this same current (especially in the case where the cycle compressor 3, in which will return the vaporized liquid 15, aspires too much and drop the pressure below that of the triple point of CO 2 ).

Claims (8)

  1. Method for liquefaction of a gas flow containing at least 95% mol., even at least 99% mol. of carbon dioxide wherein:
    a) the supply gas flow (1) is compressed in at least one first compression stage (3C, 3D),
    b) the compressed flow is cooled to partially condense it to produce a liquid flow, by being cooled in a first heat exchanger (7) other than a second heat exchanger to partially condense it, the partially condensed flow is expanded and sent to a first phase separator (S1), a liquid from the first phase separator is expanded then sent to a second phase separator (S2) and the liquid flow is extracted from the second phase separator, characterised in that:
    c) at least one part of the liquid flow is cooled in the tubes of the second heat exchanger (9) which is a heat exchanger with tubes and a grille
    d) a first part (11) of the liquid cooled in the second exchanger, is then expanded and is used as a liquid product
    e) a second part (13) of the liquid cooled in the second exchanger is expanded in a valve (V4, V10) to bring the liquid to a temperature and a pressure close to the triple point of the cooled liquid and is vaporised in the grille of the second exchanger to form a vaporised flow (15) and
    f) at least one part of the vaporised flow is compressed and mixed with the supply gas flow.
  2. Method according to claim 1, wherein the gas (4) from the first phase separator (S1) is mixed with the supply gas flow at a first pressure.
  3. Method according to claim 1 or 2, wherein a gas (6) from the second phase separator (S2) is mixed with the supply gas flow.
  4. Method according to claim 3, wherein a gas (6) from the second phase separator (S2) is mixed with the supply gas flow at a second pressure, lower than the first pressure.
  5. Method according to claim 4 wherein the gas (6) from the second phase separator (S2) is mixed with the supply gas flow upstream of the first compression stage (3C).
  6. Method according to one of the preceding claims, wherein the liquid (14) from the first phase separator (S1) is not cooled upstream of it being expanded.
  7. Method according to one of the preceding claims, wherein the second heat exchanger (9) is a final sub-cooler.
  8. Method according to claim 7, wherein the final product is not cooled downstream of the second exchanger (9).
EP15701557.9A 2014-01-10 2015-01-09 Method and device for the liquefaction of a gaseous co2 stream Active EP3092453B1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR1450201A FR3016436B1 (en) 2014-01-10 2014-01-10 METHOD AND APPARATUS FOR LIQUEFACTING A GASEOUS CO2 CURRENT
PCT/FR2015/050049 WO2015104510A2 (en) 2014-01-10 2015-01-09 Method and device for the liquefaction of a gaseous co2 stream

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EP3092453B1 true EP3092453B1 (en) 2018-06-13

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CN108895765A (en) * 2018-05-22 2018-11-27 中石化宁波工程有限公司 A kind of co 2 liquefaction device and liquifying method
FR3088416B1 (en) * 2018-11-08 2020-12-11 Air Liquide METHOD AND APPARATUS FOR LIQUEFACTION OF A GAS CURRENT CONTAINING CARBON DIOXIDE
WO2020205750A1 (en) * 2019-03-29 2020-10-08 Bright Energy Storage Technologies, Llp Co2 separation & liquefaction system and method
AU2022203999A1 (en) 2021-06-09 2023-01-05 Technip Energies France Process for the recovery of a liquefied CO2 stream from an industrial waste gas and associated installation
US11635255B1 (en) 2022-04-08 2023-04-25 Axip Energy Services, Lp Liquid or supercritical carbon dioxide capture from exhaust gas

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WO2015104510A2 (en) 2015-07-16
FR3016436A1 (en) 2015-07-17
CN106415173A (en) 2017-02-15
WO2015104510A3 (en) 2015-12-10
CN106415173B (en) 2019-09-27
US20160327333A1 (en) 2016-11-10
EP3092453A2 (en) 2016-11-16
FR3016436B1 (en) 2019-05-10

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