EP3092453A2 - Method and device for the liquefaction of a gaseous co2 stream - Google Patents

Method and device for the liquefaction of a gaseous co2 stream

Info

Publication number
EP3092453A2
EP3092453A2 EP15701557.9A EP15701557A EP3092453A2 EP 3092453 A2 EP3092453 A2 EP 3092453A2 EP 15701557 A EP15701557 A EP 15701557A EP 3092453 A2 EP3092453 A2 EP 3092453A2
Authority
EP
European Patent Office
Prior art keywords
flow
liquid
phase separator
heat exchanger
cooled
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP15701557.9A
Other languages
German (de)
French (fr)
Other versions
EP3092453B1 (en
Inventor
Nicolas CHAMBRON
Benoît DAVIDIAN
Arthur Darde
Mathieu LECLERC
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Publication of EP3092453A2 publication Critical patent/EP3092453A2/en
Application granted granted Critical
Publication of EP3092453B1 publication Critical patent/EP3092453B1/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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"
    • F25J1/004—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
    • F25J1/003—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

Abstract

The invention relates to a device for the liquefaction of a gas flow containing at least 95 mol-% carbon dioxide, comprising at least a first compression stage (C3, C4) in which the feed gas flow (1) is compressed; means for condensing the compressed flow, formed by two in-series phase separators, in order to partially condense said flow and produce a liquid flow; a first heat exchanger (7); a second heat exchanger (9) which is a shell and tube heat exchanger; means for conveying at least part of the liquid flow into the tubes of the first heat exchanger; means for discharging, as a liquid product (11), a first part of the liquid cooled in the second exchanger, said part being subsequently expanded; a valve (V4); means for conveying a second part of the liquid cooled in the second exchanger, said second part being expanded in the valve and vaporised in the shell of the first exchanger in order to form a vaporised flow (15); and means (3A, 3B) for compressing at least part of the vaporised flow and mixing same with the feed gas flow.

Description

Procédé et appareil de liquéfaction d'un courant de CQ2 gazeux La présente invention est relative à un procédé et à un appareil 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 method and an apparatus for liquefying a stream of gaseous C02. 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 CO2 stream containing impurities (for example H2, N2).
II 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 from JP-A-64084087 to liquefy a flow containing mainly CO2 by drying the flow rate to be liquefied in a dryer, cooling it to partially liquefy it, sending it to a first phase separator, sending the liquid from 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.
Un but de la présente invention est de pallier les défauts de l'art antérieur. Selon un objet de l'invention, il est prévu un procédé de d'un débit gazeux contenant au moins 95% mol. voire au moins 99% mol. de dioxyde de carbone dans lequel :  An object of the present invention is to overcome the defects of the prior art. According to one object of the invention, there is provided a method of a gas flow rate containing at least 95 mol%. at least 99% mol. of carbon dioxide in which:
a) le débit gazeux d'alimentation est comprimé dans au moins un premier étage de compression,  a) the feed gas flow rate is compressed in at least a first compression stage,
b) le débit comprimé est refroidi pour le condenser au moins partiellement pour produire un débit liquide, en étant refroidi dans un premier échangeur de chaleur autre que le premier échangeur de chaleur pour le condenser partiellement, le débit partiellement condensé est détendu et envoyé à un premier séparateur de phases , un liquide du premier séparateur de phases est détendu puis envoyé à un deuxième séparateur de phases et le débit liquide est soutiré du deuxième séparateur de phases.  b) the compressed flow rate is cooled to at least partially condense it to produce a liquid flow, being cooled in a first heat exchanger other than the first heat exchanger to partially condense it, the partially condensed flow is expanded and sent to a first phase separator, a liquid of the first phase separator is expanded and then sent to a second phase separator and the liquid flow is withdrawn from the second phase separator.
c) au moins une partie du débit liquide est refroidi dans les tubes d'un deuxième échangeur de chaleur qui est un échangeur de chaleur à tubes et à calandre  c) at least a portion of the liquid flow is cooled in the tubes of a second heat exchanger which is a tube and shell heat exchanger
d) une première partie du liquide refroidi dans le deuxième échangeur, ensuite détendue sert de produit liquide e) une deuxième partie (du liquide refroidi dans le deuxième échangeur ou d'un liquide produit en détendant et vaporisant partiellement ce liquide est détendue dans une vanne et se vaporise dans la calandre du premier échangeur pour former un débit vaporisé et d) a first part of the liquid cooled in the second exchanger, then relaxed serves as a liquid product e) a second portion (liquid cooled in the second heat exchanger or liquid produced by partially expanding and vaporizing the liquid is expanded in a valve and vaporizes in the shell of the first heat exchanger to form a vaporized flow and
f) au moins une partie du débit vaporisé est comprimée et mélangée avec le débit gazeux d'alimentation.  f) at least a portion of the vaporized flow is compressed and mixed with the feed gas flow.
Selon d'autres aspects facultatifs : According to other optional aspects:
- un gaz du premier séparateur de phases est mélangé avec le débit gazeux d'alimentation à une première pression.  a gas of the first phase separator is mixed with the gas supply flow at a first pressure.
- un gaz du deuxième séparateur de phases est mélangé avec le débit gazeux d'alimentation.  a gas of the second phase separator is mixed with the gas supply flow.
-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.  the gas of the second phase separator is mixed with the gas supply flow at a second pressure lower than the first pressure.
-le gaz du deuxième séparateur de phases est mélangé avec le débit gazeux d'alimentation en amont du premier étage de compression.  the gas of the second phase separator is mixed with the feed gas flow upstream of the first compression stage.
-le liquide du premier séparateur de phases n'est pas refroidi en amont de la détente  the liquid of the first phase separator is not cooled upstream of the trigger
- le deuxième échangeur est un sous-refroidisseur final.  the second exchanger is a final subcooler.
- le produit final n'est pas refroidi en aval du deuxième échangeur.  the final product is not cooled downstream of the second exchanger.
-aucune fraction du produit liquide n'est recyclée au premier étage de compression  -no fraction of the liquid product is recycled to the first stage of 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  the second part of the liquid cooled in the second exchanger is expanded in a valve and is heated only in the second heat exchanger to form a vaporized flow rate
Selon un autre objet de l'invention, il est prévu un appareil de liquéfaction d'un débit gazeux contenant au moins 95 mol.%, voire au moins 99% mol. de dioxyde de carbone comprenant au moins un premier étage de compression dans lequel le débit gazeux d'alimentation est comprimé, des moyens de condensation du débit comprimé, pour le condenser partiellement pour produire un débit liquide, un premier échangeur de chaleur , dans lequel le débit comprimé est refroidi pour le condenser partiellement, des moyens de détente du débit partiellement condensé, un premier séparateur de phases dans lequel le débit détendu est envoyé, des moyens pour détendre un liquide du premier séparateur de phases, un deuxième séparateur de phases, des moyens pour envoyer le liquide détendu au deuxième séparateur de phases et des moyens pour soutirer le débit liquide du deuxième séparateur de phases, un deuxième échangeur de chaleur (9) qui est un échangeur de chaleur à tubes et à calandre, des moyens pour envoyer au moins une partie du débit liquide dans les tubes du deuxième échangeur de chaleur, des moyens pour sortir comme produit liquide i) une première partie du liquide refroidi dans le deuxième échangeur, ensuite détendue, ou ii) une première partie d'un liquide produit en détendant et en vaporisant partiellement le liquide refroidi dans le deuxième échangeur, une vanne , des moyens pour envoyer une deuxième partie du liquide refroidi dans le deuxième échangeur ou d'un liquide produit en détendant et vaporisant partiellement ce liquide se détendre dans la vanne et se vaporiser dans la calandre du deuxième échangeur pour former un débit vaporisé et des moyens pour comprimer au moins une partie du débit vaporisé et la mélanger avec le débit gazeux d'alimentation. According to another object of the invention, there is provided an apparatus for liquefying a gas flow rate containing at least 95 mol% or even at least 99 mol%. carbon dioxide composition comprising at least a first compression stage in which the feed gas flow rate is compressed, compressed flow condensing means, for partially condensing it to produce a liquid flow, a first heat exchanger, wherein the compressed flow is cooled to partially condense it, partially condensed flow expansion means, a first phase separator in which the expanded flow is sent, means for expanding a liquid of the first phase separator, a second separator of phases, means for sending the expanded liquid to the second phase separator and means for withdrawing the liquid flow from the second phase separator, a second heat exchanger (9) which is a tube and shell heat exchanger, means to send at least a portion of the liquid flow into the tubes of the second heat exchanger, means for outputting as liquid product i) a first portion of the cooled liquid in the second exchanger, then expanded, or ii) a first part of a liquid produced by partially expanding and vaporizing the cooled liquid in the second heat exchanger, a valve, means for sending a second portion of the cooled liquid into the second heat exchanger or a liquid produced by partially expanding and vaporizing the liquid to relax in the valve and vaporize in the shell of the second heat exchanger to form a vaporized flow and means for compressing at least one Part of the vaporized flow and mix with the feed gas flow.
Selon d'autres aspects facultatifs, l'appareil :  According to other optional aspects, the apparatus:
- comprend des moyens pour envoyer un gaz du premier séparateur de phases en aval du premier étage de compression.  comprises means for sending a gas from the first phase separator downstream of the first compression stage.
-comprend des moyens pour envoyer un gaz du deuxième séparateur de phases en amont du premier étage de compression.  comprises means for sending a gas from the second phase separator upstream of the first compression stage.
- ne comprend pas de moyens de refroidissemeent entre le premier séparateur de phases et la vanne.  - Does not include cooling means between the first phase separator and the valve.
Le deuxième échangeur de chaleur est de préférence le dernier sous- refroidisseur de l'appareil.  The second heat exchanger is preferably the last subcooler of the apparatus.
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 FIG. 1, the liquefaction process of a flow rate 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 CO2 supply, as a function of 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. 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 CO2 thus condensed at high pressure will undergo a succession of detents in valves V1, V2, in order to self-cool by generating a gas. 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 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 stage of expansion of the liquid 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 CO2 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 1 1 est détendue dans une vanne V3 pour former un produit liquide à la pression requise par le client, typiquement 7bara. 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 1 1 is expanded in a valve V3 to form a liquid product at the pressure required by the customer, typically 7bara. 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 3, il est mélangé avec le débit 1 .  The vaporised low pressure CO2 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 3, 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 CO2).

Claims

Revendications claims
1 . Procédé de liquéfaction d'un débit gazeux contenant au moins 95% mol., voire au moins 99% mol. de dioxyde de carbone dans lequel : 1. Process for liquefying a gas flow rate containing at least 95 mol%, or even at least 99 mol%. of carbon dioxide in which:
a) le débit gazeux d'alimentation (1 ) est comprimé dans au moins un premier étage (3C, 3D) de compression,  a) the feed gas flow (1) is compressed in at least a first compression stage (3C, 3D),
b) le débit comprimé est refroidi pour le condenser au moins partiellement pour produire un débit liquide, en étant refroidi dans un premier échangeur de chaleur (7) autre que le premier échangeur de chaleur pour le condenser partiellement, le débit partiellement condensé est détendu et envoyé à un premier séparateur de phases (S1 ), un liquide du premier séparateur de phases est détendu puis envoyé à un deuxième séparateur de phases (S2) et le débit liquide est soutiré du deuxième séparateur de phases.  b) the compressed flow is cooled to at least partially condense to produce a liquid flow, cooled in a first heat exchanger (7) other than the first heat exchanger to partially condense it, the partially condensed flow is expanded and sent to a first phase separator (S1), a liquid of the first phase separator is expanded and then sent to a second phase separator (S2) and the liquid flow is withdrawn from the second phase separator.
c) au moins une partie du débit liquide est refroidi dans les tubes d'un deuxième échangeur de chaleur (9) qui est un échangeur de chaleur à tubes et à calandre  c) at least a portion of the liquid flow is cooled in the tubes of a second heat exchanger (9) which is a tube and shell heat exchanger
d) une première partie (1 1 ) du liquide refroidi dans le deuxième échangeur, ensuite détendue, sert de produit liquide  d) a first portion (1 1) of the cooled liquid in the second exchanger, then expanded, serves as a liquid product
e) une deuxième partie (13) du liquide refroidi dans le deuxième échangeur ou d'un liquide produit en détendant et vaporisant partiellement ce liquide est détendue dans une vanne (V4, V10) et se vaporise dans la calandre du premier échangeur pour former un débit vaporisé (15) et  e) a second portion (13) of the liquid cooled in the second heat exchanger or a liquid produced by partially expanding and vaporizing said liquid is expanded in a valve (V4, V10) and vaporizes in the shell of the first heat exchanger to form a vaporized flow (15) and
f) au moins une partie du débit vaporisé est comprimé et mélangé avec le débit gazeux d'alimentation.  f) at least a portion of the vaporized flow is compressed and mixed with the feed gas flow.
2. Procédé selon la revendication 1 dans lequel un gaz (4) du premier séparateur de phases (S1 ) est mélangé avec le débit gazeux d'alimentation à une première pression. 2. The method of claim 1 wherein a gas (4) of the first phase separator (S1) is mixed with the feed gas flow at a first pressure.
3. Procédé selon la revendication 1 ou 2 dans lequel un gaz (6) du deuxième séparateur de phases (S2) est mélangé avec le débit gazeux d'alimentation. 3. Method according to claim 1 or 2 wherein a gas (6) of the second phase separator (S2) is mixed with the feed gas flow.
4. Procédé selon la revendication 3 dans lequel le gaz (6) du deuxième séparateur de phases (S2) est mélangé avec le débit gazeux d'alimentation à une deuxième pression plus basse que la première pression. 4. The method of claim 3 wherein the gas (6) of the second phase separator (S2) is mixed with the gas supply flow at a second pressure lower than the first pressure.
5. Procédé selon la revendication 4 dans lequel le gaz du deuxième séparateur de phases (S2) est mélangé avec le débit gazeux d'alimentation en amont du premier étage de compression. 5. The method of claim 4 wherein the gas of the second phase separator (S2) is mixed with the feed gas flow upstream of the first compression stage.
6. Procédé selon l'une des revendications précédentes dans lequel le liquide (14) du premier séparateur de phases (S1 ) n'est pas refroidi en amont de la détente. 6. Method according to one of the preceding claims wherein the liquid (14) of the first phase separator (S1) is not cooled upstream of the trigger.
7. Procédé selon l'une des revendications précédentes dans lequel le deuxième échangeur de chaleur (9) est un sous-refroidisseur final. 7. Method according to one of the preceding claims wherein the second heat exchanger (9) is a final subcooler.
8. Procédé selon la revendication 7 dans lequel le produit final n'est pas refroidi en aval du deuxième échangeur. 8. The method of claim 7 wherein the final product is not cooled downstream of the second exchanger.
9. Appareil de liquéfaction d'un débit gazeux contenant au moins 95 mol.%, voire au moins 99% mol. de dioxyde de carbone comprenant au moins un premier étage de compression (C3,C4) dans lequel le débit gazeux d'alimentation (1 ) est comprimé, des moyens de condensation du débit comprimé, pour le condenser partiellement pour produire un débit liquide, un premier échangeur de chaleur (7) , dans lequel le débit comprimé est refroidi pour le condenser partiellement, des moyens de détente du débit partiellement condensé, un premier séparateur de phases (S1 ) dans lequel le débit détendu est envoyé, des moyens (V2) pour détendre un liquide du premier séparateur de phases, un deuxième séparateur de phases (S2), des moyens pour envoyer le liquide détendu au deuxième séparateur de phases et des moyens pour soutirer le débit liquide du deuxième séparateur de phases, un deuxième échangeur de chaleur (9) qui est un échangeur de chaleur à tubes et à calandre, des moyens pour envoyer au moins une partie du débit liquide dans les tubes du deuxième échangeur de chaleur, des moyens pour sortir comme produit liquide (1 1 ) une première partie du liquide refroidi dans le deuxième échangeur qui est ensuite détendue, , une vanne (V4, V10), des moyens pour envoyer une deuxième partie du liquide refroidi dans le deuxième échangeur se détendre dans la vanne et se vaporiser dans la calandre du deuxième échangeur pour former un débit vaporisé (15) et des moyens pour comprimer (3A,3B) au moins une partie du débit vaporisé et la mélanger avec le débit gazeux d'alimentation. 9. Apparatus for liquefying a gas flow rate containing at least 95 mol%, or even at least 99 mol%. carbon dioxide composition comprising at least a first compression stage (C3, C4) in which the feed gas flow (1) is compressed, condensing means of the compressed flow, to partially condense it to produce a liquid flow, a first heat exchanger (7), wherein the compressed flow rate is cooled to partially condense it, partially condensed flow expansion means, a first phase separator (S1) in which the expanded flow rate is fed, means (V2) for expanding a liquid of the first phase separator, a second phase separator (S2), means for sending the expanded liquid to the second phase separator and means for withdrawing the liquid flow of the second phase separator, a second heat exchanger (9) which is a tube and shell heat exchanger, means for sending at least a portion of the liquid flow into the tubes of the second heat exchanger their, means for outputting as a liquid product (1 1) a first portion of the cooled liquid in the second exchanger which is then expanded,, a valve (V4, V10), means for sending a second portion of the cooled liquid in the second exchanger relax in the valve and vaporize in the shell of the second heat exchanger to form a vaporized flow (15) and means for compressing (3A, 3B) at least a portion of the vaporized flow and mix it with the feed gas flow.
10. Appareil selon la revendication 9 comprenant des moyens pour envoyer un gaz du premier séparateur de phases en aval du premier étage de compression. Apparatus according to claim 9 comprising means for supplying gas from the first phase separator downstream of the first compression stage.
1 1 . Appareil selon la revendication 9 ou 10 comprenant des moyens pour envoyer un gaz du deuxième séparateur de phases en amont du premier étage de compression. 1 1. An apparatus according to claim 9 or 10 including means for supplying gas from the second phase separator upstream of the first compression stage.
12. Appareil selon l'une des revendications 9 à 1 1 ne comprenant pas de moyens de refroidissement entre le premier séparateur de phases et la vanne. 12. Apparatus according to one of claims 9 to 1 1 not comprising cooling means between the first phase separator and the valve.
13. Appareil selon l'une des revendications 9 à 12 dans lequel le deuxième échangeur de chaleur est le dernier sous-refroidisseur de l'appareil. 13. Apparatus according to one of claims 9 to 12 wherein the second heat exchanger is the last subcooler of the apparatus.
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

Publications (2)

Publication Number Publication Date
EP3092453A2 true EP3092453A2 (en) 2016-11-16
EP3092453B1 EP3092453B1 (en) 2018-06-13

Family

ID=50473554

Family Applications (1)

Application Number Title Priority Date Filing Date
EP15701557.9A Active EP3092453B1 (en) 2014-01-10 2015-01-09 Method and device for the liquefaction of a gaseous co2 stream

Country Status (5)

Country Link
US (1) US20160327333A1 (en)
EP (1) EP3092453B1 (en)
CN (1) CN106415173B (en)
FR (1) FR3016436B1 (en)
WO (1) WO2015104510A2 (en)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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

Family Cites Families (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4778497A (en) * 1987-06-02 1988-10-18 Union Carbide Corporation Process to produce liquid cryogen
JPS6484087A (en) 1987-09-24 1989-03-29 Jgc Corp Manufacture of liquefied carbon dioxide
US5141543A (en) * 1991-04-26 1992-08-25 Air Products And Chemicals, Inc. Use of liquefied natural gas (LNG) coupled with a cold expander to produce liquid nitrogen
AU745739B2 (en) * 1998-01-08 2002-03-28 Satish Reddy Autorefrigeration separation of carbon dioxide
US5974829A (en) * 1998-06-08 1999-11-02 Praxair Technology, Inc. Method for carbon dioxide recovery from a feed stream
GB2416389B (en) * 2004-07-16 2007-01-10 Statoil Asa LCD liquefaction process
US7850763B2 (en) * 2007-01-23 2010-12-14 Air Products And Chemicals, Inc. Purification of carbon dioxide
CN100565060C (en) * 2007-04-28 2009-12-02 重庆大山燃气设备有限公司 A kind of method of natural gas liquefaction and device thereof
CN102959352B (en) * 2009-07-24 2016-07-06 英国备选能源国际有限公司 Carbon dioxide and the separation of hydrogen
CN101666573B (en) * 2009-09-21 2011-06-08 华北电力大学 CO2 separation and compression integrated method
FR2972792B1 (en) * 2011-03-16 2017-12-01 L'air Liquide Sa Pour L'etude Et L'exploitation Des Procedes Georges Claude METHOD AND APPARATUS FOR CO2 LIQUEFACTION
FR2974167B1 (en) * 2011-04-14 2015-11-06 Air Liquide METHOD AND APPARATUS FOR LIQUEFACTING A GAS
CN102269509B (en) * 2011-07-14 2013-10-09 华北电力大学 CO2 compression and liquefaction system combined with waste heat driven refrigeration
KR101153103B1 (en) * 2011-10-11 2012-06-04 한국가스공사연구개발원 Carbon dioxide re-liquefaction process

Also Published As

Publication number Publication date
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
FR3016436B1 (en) 2019-05-10
EP3092453B1 (en) 2018-06-13

Similar Documents

Publication Publication Date Title
EP3092453B1 (en) Method and device for the liquefaction of a gaseous co2 stream
TWI379986B (en) System to cold compress an air stream using natural gas refrigeration
TWI424870B (en) Method and installation for liquefying flue gas from combustion installations
CA2828179C (en) Method and apparatus for the liquefaction of co2
WO2007042662A2 (en) Method for treating a liquefied natural gas stream obtained by cooling using a first refrigerating cycle and related installation
FR3030026B1 (en) METHOD AND APPARATUS FOR SEPARATING A FUEL GAS CONTAINING AT LEAST 20% MOL. OF CO2 AND AT LEAST 20% MOL OF METHANE, BY PARTIAL CONDENSATION AND / OR BY DISTILLATION
CA2832096C (en) Method and apparatus for liquefying a co2-rich gas
GB2522421A (en) LNG production process
RU2018136794A (en) METHOD AND SYSTEM OF LIQUIDATION OF RAW MATERIAL GAS FLOW
TW201144703A (en) Method and installation for liquefying flue gas from combustion installations
US20190185332A1 (en) Synthesis of ammonia with internal cooling circuit
FR2974167A1 (en) METHOD AND APPARATUS FOR LIQUEFACTING A GAS
EP2938414B1 (en) Method and apparatus for separating a carbon dioxide-rich gas
FR2967485A1 (en) Installation for purifying gaseous flow containing carbon dioxide, comprises a first unit to compress the gaseous flow, a heat exchanger to cool compressed gaseous flow, a distillation column to separate carbon dioxide, and separator pots
FR2956478A1 (en) Method for separating air by cryogenic distillation, involves compressing part of released nitrogen flow from pressure until another pressure and sending part of flow to purification unit at former pressure to regenerate purification unit
EP3058296B1 (en) Method for denitrogenation of natural gas with or without helium recovery
FR3090832A1 (en) Method and apparatus for separating a feed stream comprising at least CO2 as well as at least one light compound
CN107429967B (en) Plant for liquefying nitrogen using recovery of cold energy obtained from the evaporation of liquefied natural gas
FR3058785A1 (en) METHOD FOR AIR SEPARATION BY CRYOGENIC DISTILLATION USING GAS RELAXATION
KR101686513B1 (en) Device and method for BOG re-liquefaction
WO2013114020A2 (en) Method and device for condensing or pseudocondensing a gas
FR2987755A1 (en) Method for separating gas containing carbon dioxide and e.g. component, lighter than carbon dioxide by distillation, involves sending part of vaporized liquid to reboiler tank, and returning vaporized part of liquid to distillation column

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20160810

AK Designated contracting states

Kind code of ref document: A2

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

AX Request for extension of the european patent

Extension state: BA ME

DAX Request for extension of the european patent (deleted)
GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: GRANT OF PATENT IS INTENDED

INTG Intention to grant announced

Effective date: 20180104

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE PATENT HAS BEEN GRANTED

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

Free format text: NOT ENGLISH

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

Ref country code: AT

Ref legal event code: REF

Ref document number: 1008921

Country of ref document: AT

Kind code of ref document: T

Effective date: 20180615

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

Free format text: LANGUAGE OF EP DOCUMENT: FRENCH

REG Reference to a national code

Ref country code: DE

Ref legal event code: R096

Ref document number: 602015012201

Country of ref document: DE

REG Reference to a national code

Ref country code: NL

Ref legal event code: FP

REG Reference to a national code

Ref country code: NO

Ref legal event code: T2

Effective date: 20180613

REG Reference to a national code

Ref country code: LT

Ref legal event code: MG4D

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BG

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180913

Ref country code: ES

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: CY

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: LT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: FI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: SE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: RS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: HR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180914

Ref country code: LV

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

REG Reference to a national code

Ref country code: AT

Ref legal event code: MK05

Ref document number: 1008921

Country of ref document: AT

Kind code of ref document: T

Effective date: 20180613

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: RO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: SK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: CZ

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: PL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: EE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: AT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: IS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20181013

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SM

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: IT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

REG Reference to a national code

Ref country code: DE

Ref legal event code: R097

Ref document number: 602015012201

Country of ref document: DE

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed

Effective date: 20190314

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: SI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MC

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20190109

REG Reference to a national code

Ref country code: BE

Ref legal event code: MM

Effective date: 20190131

REG Reference to a national code

Ref country code: IE

Ref legal event code: MM4A

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20190131

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20190131

Ref country code: CH

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20190131

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20190109

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: TR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

Ref country code: PT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20181015

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: HU

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT; INVALID AB INITIO

Effective date: 20150109

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180613

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NO

Payment date: 20230123

Year of fee payment: 9

Ref country code: FR

Payment date: 20230124

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 20230119

Year of fee payment: 9

Ref country code: DE

Payment date: 20230123

Year of fee payment: 9

P01 Opt-out of the competence of the unified patent court (upc) registered

Effective date: 20230523

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20240119

Year of fee payment: 10

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20240119

Year of fee payment: 10

Ref country code: GB

Payment date: 20240123

Year of fee payment: 10