US20160327333A1 - 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

Info

Publication number
US20160327333A1
US20160327333A1 US15/110,458 US201515110458A US2016327333A1 US 20160327333 A1 US20160327333 A1 US 20160327333A1 US 201515110458 A US201515110458 A US 201515110458A US 2016327333 A1 US2016327333 A1 US 2016327333A1
Authority
US
United States
Prior art keywords
flow
pressure
liquid
phase separator
heat exchanger
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.)
Abandoned
Application number
US15/110,458
Inventor
Nicolas Chambron
Arthur Darde
Benoît Davidian
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 US20160327333A1 publication Critical patent/US20160327333A1/en
Assigned to L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude reassignment L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: DARDE, ARTHUR, DAVIDIAN, BENOIT, CHAMBRON, Nicolas, LECLERC, Mathieu
Abandoned legal-status Critical Current

Links

Images

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
    • F25J1/003—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 and to a device for the liquefaction of a gaseous CO 2 stream.
  • the stream contains at least 95 mol % of CO 2 , indeed even at least 99 mol % of CO 2 .
  • the invention consists of a process which makes it possible to liquefy a CO 2 stream containing impurities (for example H 2 or N 2 ).
  • JP-A-64084087 It is known from JP-A-64084087 to liquefy a flow predominantly containing CO 2 by drying the flow to be liquefied in a dryer, by cooling it in order to partially liquefy it, by sending it to a first phase separator, by sending the liquid from the first phase separator to a second phase separator and by extracting the liquefied flow from the second phase separator.
  • the gas from the second phase separator is reheated and sent upstream of the dryer.
  • One aim of the present invention is to overcome the failings of the prior art. According to a subject-matter of the invention, there is provided a process for of a gas flow containing at least 95 mol %, indeed even at least 99 mol %, of carbon dioxide, in which:
  • the compressed flow is cooled in order to at least partially condense it in order to produce a liquid flow, by being cooled in a first heat exchanger other than the first heat exchanger in order to partially condense it, the partially condensed flow is reduced in pressure and sent to a first phase separator, a liquid from the first phase separator is reduced in pressure and then sent to a second phase separator and the liquid flow is withdrawn from the second phase separator,
  • a device for the liquefaction of a gas flow containing at least 95 mol %, indeed even at least 99 mol %, of carbon dioxide comprising at least a first compression stage in which the feed gas flow is compressed, means for condensing the compressed flow, in order to partially condense it in order to produce a liquid flow, a first heat exchanger, in which the compressed flow is cooled in order to partially condense it, means for reducing in pressure the partially condensed flow, a first phase separator into which the pressure-reduced flow is sent, means for reducing in pressure a liquid from a first phase separator, a second phase separator, means for sending the pressure-reduced 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 shell and tube heat exchanger, means for sending at least a part of the liquid flow into the tubes of the second heat exchanger, means for taking out, as liquid
  • the device :
  • the second heat exchanger is preferably the final subcooler of the device.
  • FIG. 1 illustrates a schematic representation of one embodiment of the present invention.
  • the process for the liquefaction of a flow 1 containing at least 95 mol %, indeed even at least 99 mol %, of carbon dioxide is carried out by cooling by indirect heat exchange with a cold source.
  • the feeding with CO 2 is carried out at interstage on a cycle compressor 3 , between stages 3 B and 3 C.
  • the final two stages 3 C, 3 D of this compressor 3 compress the flow 1 until a sufficient pressure is reached which makes it possible to condense the gas stream confronted with a cold source 5 available on site (for example ice-cold water) in a heat exchanger 7 .
  • a cold source 5 available on site (for example ice-cold water) in a heat exchanger 7 .
  • the first reduction in pressure in the valve V 1 will preferably take place at the inlet pressure of the final wheel 3 D of the cycle compressor 3 .
  • the gas 4 generated subsequent to the reduction in pressure of the liquid at the pressure-reduced equilibrium originating from the phase separator S 1 can be recycled upstream of the final wheel of the cycle compressor.
  • a second stage of reduction in pressure of the liquid from the phase separator S 1 in a second valve V 2 is preferably envisaged in order to reduce the pressure of the liquefied CO 2 , before entering the main exchanger 9 , thus making possible a CAPEX saving on this same exchanger.
  • the pressure-reduction pressure is chosen in order to make possible the recycling of a gas 6 from a second phase separator S 2 upstream of the penultimate compression wheel 3 C.
  • the stream of liquid CO 2 18 will enter a heat exchanger 9 in order to be strongly subcooled therein.
  • the liquid 18 is divided into two parts.
  • the part 11 is reduced in pressure in a valve V 3 in order to form a liquid product at a pressure required by the client, typically 7 bara.
  • a part 13 is evaporated against the liquid 18 in the heat exchanger 9 , after reduction in pressure in a valve V 4 .
  • the reduction in pressure in the valve V 4 brings the liquid up to reaching a temperature as close as possible to that of the triple point ( ⁇ 56.5° C.).
  • the vaporized low-pressure CO 2 15 is subsequently recycled to the first stages 3 A, 3 B of the cycle compressor 3 in order to ensure a liquefaction yield of 100%. It is mixed with the flow 1 between stages 3 B and 3 .
  • the heat exchanger 9 mentioned above will be an exchanger of shell and tube type, with the flow 18 to be cooled in the tubes and the liquid 13 , reduced in pressure to a pressure approximately that of the triple point, in the shell, in order to avoid any risk of accident, as a result of a possible icing up of this same stream (in particular in the case where the cycle compressor 3 , to which the vaporized liquid 15 will return, sucks too much and causes the pressure to fall below that of the triple point of CO 2 ).

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Carbon And Carbon Compounds (AREA)

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 in which the feed gas flow is compressed; means for condensing the compressed flow, formed by two in-series phase separators, in order to partially condense the flow and produce a liquid flow; a first heat exchanger; a second heat exchanger; a means for conveying at least part of the liquid flow into the tubes of the first heat exchanger; a means for discharging a first part of the liquid cooled in the second heat exchanger, a valve, a means for conveying as second part of the liquid cooled in the second exchanger, and a means for compressing at least part of the vaporized flow and mixing this with the fed gas flow.

Description

    CROSS REFERENCE TO RELATED APPLICATIONS
  • This application is a 371 of International PCT Application PCT/FR2015/050049 filed Jan. 9, 2015 which claims priority to French Patent Application No. 1450201 filed Jan. 10, 2014, the entire contents of which are incorporated herein by reference.
    • BACKGROUND
  • The present invention relates to a process and to a device for the liquefaction of a gaseous CO2 stream. The stream contains at least 95 mol % of CO2, indeed even at least 99 mol % of CO2.
    • SUMMARY
  • The invention consists of a process which makes it possible to liquefy a CO2 stream containing impurities (for example H2 or N2).
  • It is known from JP-A-64084087 to liquefy a flow predominantly containing CO2 by drying the flow to be liquefied in a dryer, by cooling it in order to partially liquefy it, by sending it to a first phase separator, by sending the liquid from the first phase separator to a second phase separator and by extracting the liquefied flow from the second phase separator. The gas from the second phase separator is reheated and sent upstream of the dryer.
  • This process does not make it possible to subcool the liquid produced, which proves to be of use when the liquid has to be used at a lower pressure than the liquefaction pressure.
  • One aim of the present invention is to overcome the failings of the prior art. According to a subject-matter of the invention, there is provided a process for of a gas flow containing at least 95 mol %, indeed even at least 99 mol %, of carbon dioxide, in which:
  • a) the feed gas flow is compressed in at least a first compression stage,
  • b) the compressed flow is cooled in order to at least partially condense it in order to produce a liquid flow, by being cooled in a first heat exchanger other than the first heat exchanger in order to partially condense it, the partially condensed flow is reduced in pressure and sent to a first phase separator, a liquid from the first phase separator is reduced in pressure and then sent to a second phase separator and the liquid flow is withdrawn from the second phase separator,
  • c) at least a portion of the liquid flow is cooled in the tubes of a second heat exchanger which is a shell and tube heat exchanger,
  • d) a first part of the liquid cooled in the second exchanger, subsequently reduced in pressure, acts as liquid product,
  • e) a second part of the liquid cooled in the second exchanger or of a liquid produced by reducing in pressure and partially vaporizing this liquid is reduced in pressure in a valve and is evaporated in the shell of the first exchanger in order to form a vaporized flow, and
  • f) at least a part of the vaporized flow is compressed and mixed with the feed gas flow.
  • According to other optional aspects:
      • a gas from the first phase separator is mixed with the feed gas flow at a first pressure,
      • a gas from the second phase separator is mixed with the feed gas flow,
      • the gas from the second phase separator is mixed with the feed gas flow at a second pressure lower than the first pressure,
      • the gas from the second phase separator is mixed with the feed gas flow upstream of the first compression stage,
      • the liquid from the first phase separator is not cooled upstream of the reduction in pressure,
      • 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 compression stage,
      • the second part of the liquid cooled in the second exchanger is reduced in pressure in a valve and is reheated solely in the second heat exchanger in order to form a vaporized flow.
  • According to another subject matter of the invention, there is provided a device for the liquefaction of a gas flow containing at least 95 mol %, indeed even at least 99 mol %, of carbon dioxide, comprising at least a first compression stage in which the feed gas flow is compressed, means for condensing the compressed flow, in order to partially condense it in order to produce a liquid flow, a first heat exchanger, in which the compressed flow is cooled in order to partially condense it, means for reducing in pressure the partially condensed flow, a first phase separator into which the pressure-reduced flow is sent, means for reducing in pressure a liquid from a first phase separator, a second phase separator, means for sending the pressure-reduced 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 shell and tube heat exchanger, means for sending at least a part of the liquid flow into the tubes of the second heat exchanger, means for taking out, as liquid product, i) a first part of the liquid cooled in the second exchanger, subsequently reduced in pressure, or ii) a first part of a liquid produced by reducing in pressure and by partially vaporizing the liquid cooled in the second exchanger, a valve, means for sending a second part of the liquid cooled in the second exchanger or of a liquid produced by reducing in pressure and partially vaporizing this liquid to be reduced in pressure in the valve and to be vaporized in the shell of the second exchanger, in order to form a vaporized flow, and means for compressing at least a part of the vaporized flow and mixing it with the feed gas flow.
  • According to other optional aspects, the device:
      • comprises means for sending a gas from the first phase separator downstream of the first compression stage,
      • comprises means for sending a gas from the second phase separator upstream of the first compression stage,
      • does not comprise cooling means between the first phase separator and the valve.
  • The second heat exchanger is preferably the final subcooler of the device.
  • The invention will be described in a more detailed manner with reference to the FIGURE.
    • BRIEF DESCRIPTION OF THE DRAWING
  • For a further understanding of the nature and objects for the present invention, reference should be made to the following detailed description, taken in conjunction with the accompanying drawing, in which like elements are given the same or analogous reference numbers and wherein:
  • FIG. 1 illustrates a schematic representation of one embodiment of the present invention.
    •  DESCRIPTION OF PREFERRED EMBODIMENTS
  • In FIG. 1, the process for the liquefaction of a flow 1 containing at least 95 mol %, indeed even at least 99 mol %, of carbon dioxide is carried out by cooling by indirect heat exchange with a cold source. The feeding with CO2, as a function of its pressure, is carried out at interstage on a cycle compressor 3, between stages 3B and 3C.
  • The final two stages 3C, 3D of this compressor 3 compress the flow 1 until a sufficient pressure is reached which makes it possible to condense the gas stream confronted with a cold source 5 available on site (for example ice-cold water) in a heat exchanger 7.
  • The CO2 thus condensed at high pressure will undergo a succession of reductions in pressure in valves V1, V2 in order to be selfcooled by generation of a gas.
  • The first reduction in pressure in the valve V1 will preferably take place at the inlet pressure of the final wheel 3D of the cycle compressor 3. Thus, the gas 4 generated subsequent to the reduction in pressure of the liquid at the pressure-reduced equilibrium originating from the phase separator S1 can be recycled upstream of the final wheel of the cycle compressor.
  • A second stage of reduction in pressure of the liquid from 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 making possible a CAPEX saving on this same exchanger. Here again, the pressure-reduction pressure is chosen in order to make possible the recycling of a gas 6 from a second phase separator S2 upstream of the penultimate compression wheel 3C.
  • This sequence of reductions in pressure in the valves V1, V2 makes it possible to cool the liquefied CO 2 18 while limiting the OPEX impact by recycling as much as possible in the final compression stages.
  • Once partially reduced in pressure and cooled, the stream of liquid CO 2 18 will enter a heat exchanger 9 in order to be strongly subcooled therein. After subcooling, the liquid 18 is divided into two parts. The part 11 is reduced in pressure in a valve V3 in order to form a liquid product at a pressure required by the client, typically 7 bara. A part 13 is evaporated against the liquid 18 in the heat exchanger 9, after reduction in pressure in a valve V4. The reduction in pressure in the valve V4 brings the liquid up to reaching a temperature as close as possible to that of the triple point (−56.5° C.).
  • The vaporized low-pressure CO 2 15 is subsequently recycled to the first stages 3A, 3B of the cycle compressor 3 in order to ensure a liquefaction yield of 100%. It is mixed with the flow 1 between stages 3B and 3.
  • The heat exchanger 9 mentioned above will be an exchanger of shell and tube type, with the flow 18 to be cooled in the tubes and the liquid 13, reduced in pressure to a pressure approximately that of the triple point, in the shell, in order to avoid any risk of accident, as a result of a possible icing up of this same stream (in particular in the case where the cycle compressor 3, to which the vaporized liquid 15 will return, sucks too much and causes the pressure to fall below that of the triple point of CO2).

Claims (14)

1.-13. (canceled)
14. A process for the liquefaction of a gas flow containing at least 95 mol % of carbon dioxide, comprising:
a) compressing the feed gas flow in at least a first compression stage,
b) cooling the compressed flow in order to at least partially condense the compressed flow, thereby producing a liquid flow, the cooling being performed in a first heat exchanger in order to partially condense it, reducing the partially condensed flow in pressure thereby producing a first reduced pressure flow and sending the first reduced pressure flow to a first phase separator, reducing a liquid from the first phase separator in pressure thereby producing a second reduced pressure flow and then sending the second reduced pressure flow to a second phase separator and withdrawing the liquid flow from the second phase separator,
c) cooling at least a portion of the liquid flow removed from the second phase separator in the tubes of a second heat exchanger which is a shell and tube heat exchanger,
d) cooling a first part of the liquid cooled in the second exchanger, subsequently reducing the cooled first part in pressure, thereby producing a liquid product,
e) cooling a second part of the liquid cooled in the second exchanger or of a liquid produced by reducing in pressure and partially vaporizing the cooled second part by reducing the pressure in a valve and is evaporating the cooled second part in the shell of the first exchanger in order to form a vaporized flow, and
f) compressing at least a part of the vaporized flow and mixing the compressed vaporized flow with the feed gas flow.
15. The process of claim 14, in which a gas from the first phase separator is mixed with the feed gas flow at a first pressure.
16. The process of claim 14, wherein a gas from the second phase separator is mixed with the feed gas flow.
17. The process of claim 16, wherein the gas from the second phase separator is mixed with the feed gas flow at a second pressure lower than the first pressure.
18. The process of claim 17, wherein the gas from the second phase separator is mixed with the feed gas flow upstream of the first compression stage.
19. The process of claim 14, wherein the liquid from the first phase separator is not cooled upstream of the reduction in pressure.
20. The process of claim 14, wherein the second heat exchanger is a final subcooler.
21. The process of claim 20, wherein the final product is not cooled downstream of the second exchanger.
22. A device for the liquefaction of a gas flow containing at least 95 mol % of carbon dioxide, comprising at least a first compression stage in which the feed gas flow is compressed, a means for condensing the compressed flow, in order to partially condense it in order to produce a liquid flow, a first heat exchanger, in which the compressed flow is cooled in order to partially condense it, a means for reducing in pressure the partially condensed flow, a first phase separator into which the pressure-reduced flow is sent, a means for reducing in pressure a liquid from a first phase separator, a second phase separator, a means for sending the pressure-reduced liquid to the second phase separator and a means for withdrawing the liquid flow from the second phase separator, a second heat exchanger which is a shell and tube heat exchanger, a means for sending at least a part of the liquid flow into the tubes of the second heat exchanger, a means for taking out, as liquid product, a first part of the liquid cooled in the second exchanger, which is subsequently reduced in pressure, a valve, a means for sending a second part of the liquid cooled in the second exchanger to be reduced in pressure in the valve and to be vaporized in the shell of the second exchanger, in order to form a vaporized flow, and a means for compressing at least a part of the vaporized flow and mixing it with the feed gas flow.
23. The device of claim 22, further comprising a means for sending a gas from a first phase separator downstream of the first compression stage.
24. The device of claim 22, further comprising means for sending a gas from the second phase separator upstream of the first compression stage.
25. The device of claim 22, not comprising cooling means between the first phase separator and the valve.
26. The device of claim 22, wherein the second heat exchanger is the final subcooler of the device.
US15/110,458 2014-01-10 2015-01-09 Method and device for the liquefaction of a gaseous co2 stream Abandoned US20160327333A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR1450201 2014-01-10
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 (1)

Publication Number Publication Date
US20160327333A1 true US20160327333A1 (en) 2016-11-10

Family

ID=50473554

Family Applications (1)

Application Number Title Priority Date Filing Date
US15/110,458 Abandoned US20160327333A1 (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)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3088416A1 (en) * 2018-11-08 2020-05-15 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude PROCESS AND APPARATUS FOR LIQUEFACTING A GAS STREAM CONTAINING CARBON DIOXIDE
US11486638B2 (en) * 2019-03-29 2022-11-01 Carbon Capture America, Inc. CO2 separation and liquefaction system and method
US11635255B1 (en) 2022-04-08 2023-04-25 Axip Energy Services, Lp Liquid or supercritical carbon dioxide capture from exhaust gas

Families Citing this family (2)

* 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
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

Citations (5)

* 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
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
US20080156035A1 (en) * 2004-07-16 2008-07-03 Statoil Asa Process and Apparatus for the Liquefaction of Carbon Dioxide
US20120118010A1 (en) * 2009-07-24 2012-05-17 Jonathan Alec Forsyth Separation of carbon dioxide and hydrogen
WO2012140369A2 (en) * 2011-04-14 2012-10-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for liquefying a gas or cooling a feed gas at supercritical pressure

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6484087A (en) 1987-09-24 1989-03-29 Jgc Corp Manufacture of liquefied carbon dioxide
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
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
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
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

Patent Citations (5)

* 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
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
US20080156035A1 (en) * 2004-07-16 2008-07-03 Statoil Asa Process and Apparatus for the Liquefaction of Carbon Dioxide
US20120118010A1 (en) * 2009-07-24 2012-05-17 Jonathan Alec Forsyth Separation of carbon dioxide and hydrogen
WO2012140369A2 (en) * 2011-04-14 2012-10-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for liquefying a gas or cooling a feed gas at supercritical pressure

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3088416A1 (en) * 2018-11-08 2020-05-15 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude PROCESS AND APPARATUS FOR LIQUEFACTING A GAS STREAM CONTAINING CARBON DIOXIDE
US11486638B2 (en) * 2019-03-29 2022-11-01 Carbon Capture America, Inc. CO2 separation and liquefaction system and method
US11635255B1 (en) 2022-04-08 2023-04-25 Axip Energy Services, Lp Liquid or supercritical carbon dioxide capture from exhaust gas

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
EP3092453A2 (en) 2016-11-16
FR3016436B1 (en) 2019-05-10
EP3092453B1 (en) 2018-06-13

Similar Documents

Publication Publication Date Title
US20160327333A1 (en) Method and device for the liquefaction of a gaseous co2 stream
AU2012324797B2 (en) Multi nitrogen expansion process for LNG production
US20170038137A1 (en) Method for the production of liquefied natural gas and nitrogen
TWI390167B (en) Method and apparatus for liquefying a natural gas stream
US20130118204A1 (en) Integrated liquid storage
US11549747B2 (en) Cryogenic air separation apparatus
RU2009144777A (en) NATURAL GAS LIQUID METHOD
JP6429867B2 (en) Integrated cascade process for vaporization and recovery of residual LNG in floating tank applications
RU2486131C2 (en) Method of producing helium
KR20190110431A (en) Nitrogen production method and nitrogen production apparatus
US20120198883A1 (en) Method for cooling a single-component or multi-component stream
WO2015110779A2 (en) Lng production process
AU2015388393B2 (en) Natural gas production system and method
US9791209B2 (en) System and process for liquefying natural gas
US10508244B2 (en) Method for removing nitrogen from a hydrocarbon-rich fraction
US20180142950A1 (en) Lng integration with cryogenic unit
KR101675878B1 (en) Device and method for re-liquefying BOG
JP7291472B2 (en) Nitrogen gas production equipment
WO2016103296A1 (en) Refrigeration device
WO2017006074A1 (en) Process for producing liquefied natural gas
US20160003526A1 (en) Methods and apparatuses for liquefying hydrocarbon streams
CN107429967B (en) Plant for liquefying nitrogen using recovery of cold energy obtained from the evaporation of liquefied natural gas
JPH0914830A (en) Oxygen and nitrogen liquefying device
US11359858B2 (en) Method for liquefying ammonia
KR101686513B1 (en) Device and method for BOG re-liquefaction

Legal Events

Date Code Title Description
AS Assignment

Owner name: L'AIR LIQUIDE, SOCIETE ANONYME POUR L'ETUDE ET L'E

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:CHAMBRON, NICOLAS;DARDE, ARTHUR;DAVIDIAN, BENOIT;AND OTHERS;SIGNING DATES FROM 20170308 TO 20170512;REEL/FRAME:043041/0876

STPP Information on status: patent application and granting procedure in general

Free format text: ADVISORY ACTION MAILED

STPP Information on status: patent application and granting procedure in general

Free format text: DOCKETED NEW CASE - READY FOR EXAMINATION

STPP Information on status: patent application and granting procedure in general

Free format text: NON FINAL ACTION MAILED

STPP Information on status: patent application and granting procedure in general

Free format text: FINAL REJECTION MAILED

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION