AU2022203999A1 - Process for the recovery of a liquefied CO2 stream from an industrial waste gas and associated installation - Google Patents

Process for the recovery of a liquefied CO2 stream from an industrial waste gas and associated installation Download PDF

Info

Publication number
AU2022203999A1
AU2022203999A1 AU2022203999A AU2022203999A AU2022203999A1 AU 2022203999 A1 AU2022203999 A1 AU 2022203999A1 AU 2022203999 A AU2022203999 A AU 2022203999A AU 2022203999 A AU2022203999 A AU 2022203999A AU 2022203999 A1 AU2022203999 A1 AU 2022203999A1
Authority
AU
Australia
Prior art keywords
stream
gas stream
carbon dioxide
sub
liquefied
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.)
Pending
Application number
AU2022203999A
Inventor
Antoine BOULLET
Manuel JACQUES
Vincent Mathieu
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.)
Technip Energies France SAS
Original Assignee
Technip Energies France SAS
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 Technip Energies France SAS filed Critical Technip Energies France SAS
Publication of AU2022203999A1 publication Critical patent/AU2022203999A1/en
Pending legal-status Critical Current

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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0266—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • 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
    • F25J1/003—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
    • F25J1/0047—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 an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—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 an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant 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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/007—Primary atmospheric gases, mixtures thereof
    • F25J1/0072—Nitrogen
    • 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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/008—Hydrocarbons
    • F25J1/0085—Ethane; Ethylene
    • 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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/008—Hydrocarbons
    • F25J1/0087—Propane; Propylene
    • 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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/0095—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
    • F25J1/02—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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/50—Processes or apparatus using other separation and/or other processing means using absorption, i.e. with selective solvents or lean oil, heavier CnHm and including generally a regeneration step for the solvent or lean oil
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/04—Mixing or blending of fluids with the feed stream
    • 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
    • F25J2210/70—Flue or combustion exhaust 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • 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
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed 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
    • 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/80—Integration in an installation using carbon dioxide, e.g. for EOR, sequestration, refrigeration etc.
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • 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
    • F25J2270/12—External refrigeration with liquid vaporising 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
    • 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
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/80—Quasi-closed internal or closed external carbon dioxide refrigeration cycle
    • 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
    • F25J2270/88—Quasi-closed internal refrigeration or heat pump cycle, if not otherwise provided
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

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)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

Method for the recovery of a liquefied CO2 stream from an industrial waste gas and associated installation The method comprises introducing a waste gas (16) into a carbon dioxide capture unit (22) to form a gas stream (36) and compress it; drying the compressed gas stream (56); cooling the dry gas stream (62); partially expanding the liquefied and sub-cooled stream (30), and introducing the expanded stream (78) into an expansion column (34) to form an overhead gas stream (80) and the liquefied carbon dioxide flow (12), wherein a part (86) of the overhead gas stream (80) is injected into the industrial waste gas (16), and a second part (88) is injected into the gas stream (36), and in that a part (90) of the expanded stream (78) forms a reboiled stream (91) in the expansion column (34). Figure for the abstract: Figure 1 1/5 C"i ":I- C j co co co C\j co co r- C", m -T C\j co CliclC*11 Ocncm:,c:n 4 cn co CD C=) co r ------------ i LD co LLC=) co C\j C\J L ---- ------- J co I CY) Co ---------------- I r -------------------------- I LO cc\j LO C\j co LO "ZiC"i C\j LO LO C"i I LO LO co r m C=) CD co L --------------I C\j TI r, co co -------C\j C0 LO (.0 co C\j co L -------------- ------------i I : co co co co c6 T co co

Description

1/5
C"i ":I- Cj co co co C\j co co r- m C", C\j co -T Clicl C*1 Ocncm:,c:n C=) co CD 4 cn co r ------------ i LD co LL C=)
coC\j C\J coCY) IL---- Co ------- J ---------------- I r-------------------------- LO I cc\j LO C\j C"iC"i I C\LOj LOLO co"Zi LO com LO C=)CD r co C\j TI L --------------I r,co co -- ----- C\j C0LO I -- --- --i - (.0 - --- -- - - - -- co C\j - -- L -- -- co : co co co co c6 T coco
Australian Patents Act 1990
ORIGINAL COMPLETE SPECIFICATION STANDARD PATENT
Invention Title Process for the recovery of a liquefied C02 stream from an industrial waste gas and associated installation
The following statement is a full description of this invention, including the best method of performing it known to me/us:- la
The present invention relates to a method for recovering a liquefied carbon dioxide stream from an industrial waste gas, comprising the following steps: - introducing the industrial waste gas into a carbon dioxide capture unit to form a carbon dioxide-rich gas stream and a carbon dioxide-poor effluent stream; - compressing the gas stream in one or more compression stages to form a compressed gas stream; - drying the compressed gas stream to form a dry gas stream; - cooling, liquefying, and sub-cooling the dry gas stream to form a liquefied and sub cooled stream, - partially expanding the liquefied and sub-cooled stream to form an expanded stream comprising a liquid and a gaseous fraction, - introducing the expanded stream into an expansion column to form an overhead gas stream and recovering the liquefied carbon dioxide stream at the bottom of the column. Such a method is intended for use in an industrial waste gas recovery unit. Industrial gases are known to be mixtures of carbon dioxide C02, dioxygen 02, dihydrogen H 2, dinitrogen N 2 , water vapour H 2 0 and various impurities such as nitrogen oxides (NOx), sulphur oxides (SOx), carbon monoxide CO or hydrogen sulphide H 2 S, the proportions of which vary according to the type of industrial facility from which they originate. Among them, carbon dioxide C02 is one of the main greenhouse gases, whose release into the atmosphere is responsible for global warming. In order to reduce the environmental impact of industries, it is therefore necessary to minimise the release of industrial carbon dioxide into the atmosphere. One known technique is to capture the carbon dioxide emitted at industrial facilities and transport it to a geological site for storage, for example by burial in soil. This is known as trapping or sequestering carbon dioxide. The recovery of carbon dioxide from industrial waste gases, with a view to its sequestration, is thus an important issue for industrial players seeking to reduce their environmental impact. More globally, industrial carbon dioxide sequestration appears to be essential for achieving the climate and energy commitments set by various national and international agreements. The carbon dioxide in industrial gases is first purified, then compressed and liquefied for transport. One of the key steps in its recovery is the deoxygenation of the gas to remove the oxygen present in the industrial effluent. An 02 content typically less than or equal to 100 molar ppm is indeed necessary to avoid the formation of corrosive species which would damage the storage and/or transport equipment. The removal of oxygen is usually done in a so-called deoxygenation reactor wherein the oxygen is converted to water by reaction with hydrogen H 2 , in the presence of a catalyst. The water generated is then removed in a drying unit. However, a deoxygenation reactor represents a significant financial investment. In addition, its operation requires a regular supply of dihydrogen, which generates storage costs as well as on-site production or purchase costs. The presence of sulphur contaminants in the effluent to be treated is also likely to deteriorate the catalyst. A guard bed is then required to protect the catalyst, which leads to additional investment and operating costs. Finally, the use of pressurised hydrogen presents safety risks that require the use of special equipment by personnel and the implementation of procedures to ensure safe operation. FR 3 016 436 teaches a method for liquefying a C02 gas stream wherein impurities such as dihydrogen or nitrogen are removed by partial expansion of the liquefied gas. The installation described in Figure 2 does not allow the treatment of oxygen-rich effluents. The installation described in Figure 3 includes additional equipment with significant installation costs. In addition, some of the carbon dioxide is released into the atmosphere, thus limiting the rate of carbon dioxide recovery. CN209828305 describes a rectification tower for purifying carbon dioxide. The impurity-rich overhead gas stream is sent to a condenser to recover some of the evaporated C02. However, the installation requires significant investment and operating costs, especially for condensing the vapours at the top of the rectification column. In addition, some of the uncondensed carbon dioxide is released into the atmosphere. KR101153080 describes a method for liquefying carbon dioxide by partial expansion of liquefied gas. The entire overhead gas stream is recycled into the effluent to be treated. However, this method is not suitable for the treatment of oxygen-rich effluents. Indeed, the accumulation of oxygen in the installation would result in a pressure build-up in the installation. One aim of the invention is to obtain a method for recovering carbon dioxide from industrial waste gases in a very efficient and reliable way, while limiting the investment and operating costs of the method. In particular, the aim of the invention is to provide a method suitable for the treatment of industrial effluents with a high content of impurities, especially oxygen. To this end, the invention relates to a method wherein a first part of the overhead gas stream is injected into the industrial waste gas, prior to its introduction into the capture unit, and wherein a second part of the overhead gas stream is injected into the carbon dioxide rich gas stream, upstream of one of the compression stages, and wherein at least part of the liquid fraction of the expanded stream is heated to form a reboiled stream, the said reboiled stream then being injected into the expansion column. In particular, the method of the invention comprises a step wherein a liquid stream is withdrawn from the bottom of the expansion column and heated to form the reboiled stream, said reboiled stream then being injected into the expansion column. The method according to the invention may comprise one or more of the following features, taken alone or in any combination that is technically possible: - the industrial waste gas contains less than 50% by mass, preferably less than 40% by mass, more preferably 2 to 30% by mass, of carbon dioxide; - the carbon dioxide-rich gas stream has a carbon dioxide content of more than 90% by mass, preferably more than 95% by mass; - the first part of the overhead gas stream is at least 50%, preferably 70% to 95%, of the overhead gas stream; - at least part of the liquid fraction of the expanded stream, in particular the liquid stream drawn off at the bottom of the expansion column, is heated by heat exchange with the liquefied and sub-cooled stream; - prior to the partial expansion step, the liquefied and sub-cooled stream is separated into a first sub-stream and a second sub-stream, the first sub-stream then being partially expanded and introduced into the expansion column and the second sub-stream being placed in heat exchange relationship with the dry gas stream; - the overhead gas stream is placed in heat exchange relationship with the dry gas stream; - the overhead gas stream is mixed with the second sub-stream to form a common stream, the common stream then being placed in a heat exchange relationship with the dry gas stream and/or with the compressed gas stream, said common stream then being divided into a first part which is injected into the gas stream, upstream of one of the compression stages, and a second part which is injected into the industrial waste stream; - the method is devoid of a catalytic deoxygenation step, particularly between the compression step and the drying step; - at the capture unit, the industrial waste gas is brought into contact with a solvent capable of absorbing carbon dioxide; - the second part of the overhead gas stream has an 02 content of 0.1 to 1% by mass.
The invention also relates to an installation for recovering a liquefied carbon dioxide stream from an industrial waste gas, comprising: - a carbon dioxide capture unit for forming a carbon dioxide-rich gas stream and a carbon dioxide-poor effluent stream, the capture unit having an inlet for introducing industrial waste gas, - a compression unit for forming a compressed gas stream comprising an inlet for introducing the carbon dioxide-rich gas stream, - a drying unit for forming a dry gas stream, comprising an inlet for introducing the compressed gas stream, - a cooling and liquefaction unit for cooling, liquefying and sub-cooling the dry gas stream to form a liquefied and sub-cooled stream, the cooling and liquefaction unit comprising an inlet for introducing the dry gas stream, - a valve for partially expanding the liquefied and sub-cooled stream to form an expanded stream comprising a liquid fraction and a gaseous fraction, - an expansion column for forming an overhead gas stream and, at the bottom of the column, the liquefied carbon dioxide stream, the expansion column comprising an inlet for introducing the expanded stream and an outlet for recovering the overhead gas stream, wherein the outlet of the expansion column is connected to the inlet of the carbon dioxide capture unit and to the inlet of the compression unit so that a first part of the overhead gas stream is injected into the carbon dioxide-rich gas stream and a second part of the overhead gas stream is injected into the industrial waste gas, and in that the expansion column is connected to a seventh heat exchanger for forming a reboiled stream. The installation according to the invention may also be such that the seventh heat exchanger further comprises an inlet for the introduction of the liquefied and sub-cooled stream and a recovery outlet connected to the valve, so that the liquefied and sub-cooled stream undergoes a further cooling step by heat exchange with the reboiled stream. The invention will be better understood upon reading the following description, given only as an example, and with reference to the attached drawings, in which: Figure 1 is a block diagram showing a first installation for carrying out a method according to the invention. Figure 2 is a block diagram showing a second installation for carrying out a method according to the invention. Figure 3 is a block diagram showing a third installation for carrying out a method according to the invention. Figure 4 is a block diagram showing a fourth installation for carrying out a method according to the invention.
Figure 5 is a block diagram showing a fifth installation for carrying out a method according to the invention.
An installation 10 according to a first embodiment of the invention is schematically shown in Figure 1. The installation 10 is intended for the recovery of a flow 12 of liquefied carbon dioxide C02, and an effluent stream 14 from an industrial waste gas 16 by a method according to the invention. The installation 10 is connected upstream to an industrial installation 18 producing the raw industrial waste gas 16. The installation 10 is connected downstream to a carbon dioxide transport and/or sequestration installation 20. The industrial installation 18 is, for example, an incinerator, power plant or cement plant. The installation 10 comprises a carbon dioxide capture unit 22 for extracting carbon dioxide from the industrial waste gas 16, a compression unit 24, a drying unit 26 and a cooling and liquefaction unit 28 for producing a liquefied and sub-cooled stream 30. The installation 10 further comprises an expansion device, in this case a valve 32 for partially expanding the liquefied and sub-cooled stream 30 and an expansion column 34. The carbon dioxide capture unit 22 is intended to form a carbon dioxide-rich gas stream 36 and the carbon dioxide-poor effluent stream 14. The capture unit 22 has an inlet 38 for introducing industrial waste gas 16 and an outlet 40 for recovering the carbon dioxide-rich gas stream 36. The capture unit 22 comprises an absorber 42 for extracting carbon dioxide from the industrial waste gas 16 so as to form a carbon dioxide-poor effluent stream 14 over the absorber 42 and a carbon dioxide-rich liquid bottom stream 44. The capture unit 22 also includes a first heat exchanger 46 for heating the stream 44 to form a heated stream 47. The capture unit 22 also includes a regenerator 48 connected to the first heat exchanger 46. The regenerator 48 is designed to extract the carbon dioxide contained in the heated stream 47 in gaseous form, recovered at the outlet of the heat exchanger 46. Advantageously, the lower part of the regenerator 48 is connected to a second heat exchanger 50 intended to reboil a liquid stream 51 taken from the bottom of the regenerator 48.
The upper part of the regenerator 48 is connected to a third heat exchanger 52, which is connected to a phase separator 54. The assembly of the third heat exchanger 52 and the phase separator 54 is intended to form, on the one hand, at the head of the phase separator 54, the carbon dioxide-rich gas stream 36, and, on the other hand, at the bottom of the phase separator 54, a reflux flow 55 injected at the head of the regenerator 48. The compression unit 24 is designed to form a compressed gas stream 56 from the carbon dioxide-rich gas stream 36. The compression unit 24 has an inlet 58 for introducing the gas stream 36 and an outlet 60 for recovering the compressed gas stream 56. The compression unit 24 comprises one or more compression stages, preferably at least 3 compression stages. Each compression stage comprises at least one compressor, at least one heat exchanger for reducing the temperature of the compressed flow to create a liquid and a gaseous fraction, at least one bursting vessel for separating the liquid fraction from the gaseous fraction, after cooling. The liquid fractions are extracted from the installation 10. The final gas fraction is the compressed gas stream 56. The drying unit 26 is intended to form a dry gas stream 62 from the compressed gas stream 56. The drying unit 26 has an inlet 64 for introducing the compressed gas stream 56 and an outlet 65 for recovering the dry gas stream 62. The drying unit 26 comprises a drying module 66. The drying modules are well known to the skilled person and will therefore not be described further here. According to the invention, the drying unit 26 further comprises, between the inlet 64 and the drying module 66, a fourth heat exchanger 67 for pre-cooling the compressed gas stream 56. The cooling and liquefaction unit 28 is designed to cool, liquefy and sub-cool the dry gas stream 62 to form the liquefied and sub-cooled stream 30. The cooling and liquefaction unit 28 has an inlet 68 for the introduction of the dry gas stream 62 and an outlet 70 for the recovery of the liquefied and sub-cooled stream 30. The cooling and liquefaction unit 28 consists of a series of heat exchangers fed in series to progressively cool, liquefy and sub-cool the dry gas stream 62. In the installation shown in Figure 1, the cooling and liquefaction unit 28 comprises two heat exchangers 72 and 74. The fifth exchanger 72 is designed to be supplied with the dry gas stream 62 and to form an intermediate liquefied stream 69 at the outlet.
The sixth exchanger 74 is designed to be supplied with the intermediate liquefied stream 69 and to form the liquefied and sub-cooled stream 30 at the outlet. The valve 32 is designed to partially expand the liquefied and sub-cooled stream 30 to form an expanded stream 78 comprising a liquid fraction and a gas fraction. The expansion column 34 is designed to separate the liquid and gaseous fractions of the expanded stream 78 to form an overhead gas stream 80, and at the bottom of the column, the liquefied carbon dioxide C02 flow 12. The expansion column 34 has an inlet 82 for introducing the expanded stream 78 and an outlet 84 for recovering the overhead gas stream 80. The recovery outlet 84 of the overhead gas stream 80 is connected to the inlet 58 of the compression unit 24 so that a first part 86 of the overhead gas stream 80 is injected into the carbon dioxide-rich gas stream 36 upstream of one of the compression stages. When the compression unit 24 comprises several compression stages, the recovery outlet 84 is connected to the inlet of one of the compression stages. The first part 86 of the gas overhead stream can thus be injected upstream of all compression stages or between two successive compression stages. The recovery outlet 84 of the overhead gas stream 80 is also connected to the inlet 38 of the capture unit 22 so that a second part 88 of the overhead gas stream 80 is injected into the industrial waste stream 16. The lower part of the expansion column 34 is also connected to a seventh heat exchanger 89 for reboiling a liquid stream 90 taken from the bottom of the expansion column 34. A reboiled stream 91 is thus recovered at the outlet of the seventh heat exchanger 89, before being injected into the lower part of the expansion column 34. The expansion column 34 thus has an outlet 92 for collecting the liquid stream 90 to be reboiled in the seventh heat exchanger 89 and an inlet 94 for introducing the reboiled stream 91 into the expansion column 34. Advantageously, the installation 10 further comprises a valve 96 for partially expanding the overhead gas stream 80. Preferably, the valve 96 is connected to the sixth heat exchanger 74 so that the partially expanded overhead gas stream 80 is heated there by heat exchange with the liquefied intermediate stream 69.
In all that follows, pressures are expressed in relative bars. The flows described in the installation are conflated with the pipes that carry them. The implementation of a first method according to the invention will now be described.
Initially, at least one industrial waste gas 16 from the industrial installation 18 is recovered. The industrial waste gas 16 typically comprises less than 50% by mass of carbon dioxide, preferably less than 40% by mass, more preferably from 2 to 30% by mass. The industrial waste gas 16 also typically comprises between 2% by weight and 10% by weight of oxygen, the remainder being impurities (H2 , NOx, SOx, CO, H 2 , ... ), nitrogen N 2 and water H 20. Preferably, the industrial waste gas 16 has a pressure of less than 15 bar, more preferably between 0 bar and 15 bar, advantageously between 0 bar and 10 bar, more advantageously between 0 bar and 8 bar, typically between 0 bar and 5 bar. Advantageously, the industrial residual gas 16 has a pressure of between 0 bar and 2 bar.
The industrial waste gas 16 is introduced into the carbon dioxide capture unit 22 and separated into the carbon dioxide-rich gas stream 36 and the carbon dioxide-poor effluent stream 14. For this purpose, the industrial waste gas 16 is first introduced into the absorber 42 through the inlet 38. Within the absorber 42, the industrial waste gas 16 is brought into contact with a solvent capable of absorbing carbon dioxide. Chemical absorption methods using solvents capable of absorbing carbon dioxide (such as amine, potassium carbonate or ammonia solutions) are well known to the skilled person and will not be further described here. Examples of amine solutions suitable for the invention are solutions composed of one or more of the following compounds: monoethanolamine, diethanolamine, N-methyldiethanolamine, piperazine, 2-Amino-2 methylpropan-1-ol, Bis(2-hydroxypropyl)amine, 1-methylpiperazine, dimethylaminoethanol. On contact with the industrial waste gas 16, the solvent absorbs the carbon dioxide present in the industrial waste gas 16 to form a bottom stream 44 consisting of the carbon dioxide-rich solvent, and at the head of the absorber 42, the carbon dioxide-poor effluent stream 14. The effluent stream 14 is then transferred to another treatment installation or released directly into the atmosphere. The effluent stream 14 typically comprises between 0.02% and 5% by volume of carbon dioxide C02. Preferably, the effluent stream 14 has an oxygen content ranging from 0.5 vol% to 12 vol%, more preferably from 2 vol% to 10 vol%. The bottom stream 44 consisting of the carbon dioxide-laden solvent is then fed into the first heat exchanger 46 where it is heated to a temperature above 80°C, preferably above 90°C, especially close to 100°C so that the carbon dioxide absorbed by the solvent is partially released in gaseous form. The heated stream 47 recovered at the outlet of the first heat exchanger 46 is two-phase and comprises a first liquid fraction comprising the charged solvent and a gaseous fraction comprising the released carbon dioxide. The heated stream 47 is then introduced into the regenerator 48. The gaseous fraction of the heated stream 47 then flows into the upper part of the regenerator 48, while the liquid fraction of the heated stream 47 flows into the lower part of the regenerator 48. The liquid stream 51 taken from the bottom of the regenerator 48 is then fed into the second heat exchanger 50 where it is heated so as to extract the carbon dioxide still absorbed by the solvent. The heated liquid stream 51 is then reintroduced into the regenerator 48 so that the released carbon dioxide migrates to the upper part of the regenerator 48. A liquid stream 98 consisting of the carbon dioxide-poor solvent is recovered at the bottom of the regenerator 48. The liquid stream 98 is then returned to the absorber 42 for recycling. Preferably, before being re-injected into the absorber 42, the liquid stream 98 is cooled in the first exchanger 46 by heat exchange with the bottom stream 44 from the absorber 42. The liquid stream 98 may also undergo an additional cooling step before injection into the absorber 42, for example by passing through an additional heat exchanger using an external refrigerant source. A gas stream 100 consisting of the gas phase extracted from the heated stream 47 is recovered at the top of the regenerator 48. The gas stream 100 is then passed to the third heat exchanger 52 for partial condensation and then to the phase separator 54 to separate the carbon dioxide-rich gas stream 36 from the condensate. The condensate is then returned to the regenerator 48 as the reflux stream 55. The gas stream 36 has a carbon dioxide content of at least 90% by weight, preferably more than 95% by weight, the remainder being impurities such as oxygen, nitrogen and water. The gas stream 36 typically has an 02 content of 1 to 200 ppm by mass. The gas stream 36 typically has an N 2 content of 10 to 1,000 ppm by mass. The gas stream 36 is then compressed and cooled to form the compressed gas stream 56 by passing through the compression unit 24 where it undergoes one or more cycles of compression, partial condensation and separation so as to remove the liquid aqueous phase generated. Preferably, the gas stream 36 undergoes at least three successive cycles of compression, condensation and separation.
The gas stream 36 is thus compressed to a pressure of more than 15 bar, advantageously less than 50 bar, and preferably between 20 bar and 45 bar. The compressed gas stream 56 recovered at the outlet 60 of the compression unit 24 typically has a temperature of 20°C to 50°C. The compressed gas stream 56 is then dried in the drying unit 26 to form the dry gas stream 62. Preferably, the compressed gas stream 56 is pre-cooled to a temperature of 10C to 50°C by passing through the fourth heat exchanger 67. Any aqueous liquid phase formed is then separated and discharged from the installation 10. Preferably, the compressed gas stream 56 is cooled in the fourth heat exchanger 67 by heat exchange with an external refrigerant fluid, preferably selected from ammonia, propane, ethylene, nitrogen and carbon dioxide. The compressed gas stream 56, possibly pre-cooled, is then dehydrated by passing through the drying module 66. The operation of the drying modules is well known to the skilled person and will not be described further here. The dry gas stream 62 typically has a residual water content of less than 500 ppm by volume, preferably from 10 ppm by volume to 500 ppm by volume. The dry gas stream 62 is then cooled, condensed and sub-cooled to a temperature below 10C, typically from -25°C to 10C to form the liquefied and sub-cooled stream 30. For this purpose, the dry gas stream 62 is introduced into the cooling and liquefaction unit 28 where it is gradually cooled by passing successively through the fifth exchanger 72 and the sixth exchanger 74. Preferably, the dehydrated gas stream 62 is cooled in the fifth heat exchanger 72 by heat exchange with an external refrigerant fluid, preferably selected from ammonia, propane, ethylene, nitrogen and carbon dioxide. In an advantageous embodiment, the gas stream 56 and the dry stream 62 are cooled by heat exchange with a single external refrigerant circulating in a closed cooling cycle 102. The external refrigerant then undergoes successive stages of compression and expansion. The intermediate liquefied stream 69, recovered at the outlet of the fifth heat exchanger 72, is then cooled at the sixth heat exchanger 74 to obtain the liquefied and sub cooled stream 30 at the outlet. Preferably, the liquefied intermediate stream 69 is cooled by heat exchange with the overhead stream 80 recovered from the expansion column 34, more preferably with the expanded overhead stream 80 recovered from the valve 96.
The liquefied and sub-cooled stream 30 is then expanded to a pressure of less than 25 bar relative, advantageously more than 5 bar relative, preferably 6 to 20 bar relative by passing through the valve 32. The expanded stream 78 then comprises a liquid and a gaseous fraction. The expanded stream 78 is then introduced into the expansion column 34 through the inlet 82. The liquid fraction of the expanded stream 78 flows into the lower part of the expansion column 34 while the gaseous fraction of the expanded stream 78 flows into the upper part of the expansion column. A liquid stream 90 is also taken from the bottom of the expansion column 34 and is heated in the seventh exchanger 89 to form a reboiled stream 91. The reboiled stream 91 is then reintroduced into the expansion column 34, preferably at the bottom of the expansion column 34. The reboiling of the liquid stream 90 thus allows the oxygen still dissolved in the liquefied carbon dioxide to be released in gaseous form. The temperature of the reboiled stream 91 is for example higher than -50°C, in particular between -50°C and -20°C The liquefied carbon dioxide flow 12 is then recovered from the bottom of the expansion column. The liquefied carbon dioxide flow 12 has a residual oxygen content of less than or equal to 100 molar ppm, preferably from 1 to 100 molar ppm. The overhead gas stream 80 consists of at least 90% by mass of carbon dioxide, preferably at least 95% by mass. The overhead gas stream 80 further comprises from 0.1 to 2% by mass of N 2 and from 0.1 to 1% by mass of oxygen. The overhead gas stream 80 has, at the outlet 84 of the expansion column 34, a pressure of less than 25 bar, advantageously greater than 5 bar, in particular between 6 bar and 20 bar; The overhead gas stream 80 is then reintroduced into the installation 10 for recycling. To do this, the overhead stream 80 is first relaxed by passing through the valve 96. Preferably, the overhead stream 80 is expanded to a pressure corresponding to the pressure of the gas stream 36 upstream of one of the compression stages of the compression unit 24. More preferably, the overhead stream 80 is expanded to a pressure corresponding to that of the stream entering the compression stage at which the first part 86 of the overhead stream is injected.
The expanded overhead gas stream 80 is then heated to a temperature above 250C and in particular between -25°C and 15°C by heat exchange with the liquefied intermediate stream 69, at the sixth exchanger 74. The overhead gas stream 80 is then divided into two parts 86, 88. The first part 86 of the overhead stream 80 is injected into the carbon dioxide-rich gas stream 36 upstream of the appropriate compression stage of the compression unit 24. In Figure 1, the compression unit 24 comprises a single compression stage. In this case, the first part 86 of the overhead stream 80 is injected into the gas stream 36 upstream of its introduction into the compression unit. Alternatively, and when the compression unit 24 comprises several compression stages, the first part 86 of the overhead stream 80 is injected into the gas stream 36 upstream of one of the compression stages. In particular, the first part 86 may be injected upstream of all compression stages or between two successive compression stages, typically between the outlet of one compression stage and the inlet of the next compression stage. The second part 88 of the overhead stream 80 is injected into the industrial waste stream 16, before it is introduced into the capture unit 22. Preferably, at least 50% of the overhead gas stream 80 is recycled into the carbon dioxide-rich gas stream 36, preferably from 70% to 95%. Preferably, at most 30% of the overhead gas stream 80 is recycled into the process stream 16. The reintroduction of the overhead stream 80 into the installation 10 allows the carbon dioxide present in the overhead stream 80 to be recovered. In particular, it increases the recovery rate of carbon dioxide. The recycling of the second part 88 of the overhead gas stream 80 to the capture unit 22 prevents and/or avoids the accumulation of incondensable impurities, essentially oxygen and nitrogen, in the installation 10, in particular in the compression unit 24, the drying unit 26, the cooling and liquefaction unit 28 or the expansion column 34. In particular, during the method of the invention, incondensable impurities, mainly consisting of carbon dioxide, are concentrated in the overhead gas stream 80. In order to avoid the accumulation of non-condensable impurities in the system, a small part of the overhead gas stream is then injected into the capture unit 22 via the second part 88 of the overhead gas stream 80, while the majority is recycled into the gas stream 36 via the first part 86 of the overhead gas stream 80. Uncondensable impurities returned to the capture unit 22 are then separated from the carbon dioxide at the absorber 42 and removed from the method in the effluent stream 14. The method of the invention thus makes it possible to prevent and/or avoid the accumulation of incondensable impurities, essentially oxygen and nitrogen, in the installation 10, without requiring the purging of any of the carbon dioxide.
Alternative installations and associated methods will now be described in relation to Figures 2, 3, 4 and 5. Only differences from the previously described installation and method are mentioned hereafter. A installation 110 according to a second embodiment of the invention is schematically shown in Figure 2. According to this second mode of implementation, the seventh heat exchanger 89 is integrated into the main chain of the installation 110 in such a way that the liquid flow 90 taken from the foot of the expansion column 34 is heated, at the level of the seventh heat exchanger 89, by heat exchange with the liquefied and sub-cooled stream 30. The seventh heat exchanger 89 thus comprises an inlet 112 for the introduction of the liquefied and sub-cooled stream 30, said inlet 112 being connected to the recovery outlet 70 of the cooling and liquefaction unit 28. The seventh heat exchanger 89 also includes an outlet 114 for recovering a secondary sub-cooled stream 116 obtained by cooling the liquefied and sub-cooled stream 30. The outlet 114 is connected to the valve 32 so that the secondary sub-cooled stream 116 is expanded before being introduced into the expansion column 34, analogous to what has been described above with reference to Figure 1. This second embodiment is advantageous in that it negates the need for external energy for reboiling the liquid stream 90, the energy being provided by thermal integration. It thus makes it possible to limit the operating costs of the method according to the invention.
In Figures 3, 4 and 5, the seventh heat exchanger 89 is integrated into the main chain of the installation by analogy with the installation 110 shown in Figure 2. Alternatively, and equivalently, the seventh heat exchanger 89 may consist of an external heat exchanger similar to that of the installation 10 shown in Figure 1 described above.
A installation 210 according to a third embodiment of the invention is schematically shown in Figure 3. According to this third embodiment, the outlet 70 for recovering the liquefied and sub-cooled stream 30 is connected on the one hand to the inlet 112 for introducing the seventh exchanger 89 (or directly to the valve 32 in the case where the seventh exchanger 89 is an external exchanger) and on the other hand to a valve 118 so that the second liquefied and sub-cooled stream 30 leaving the sixth exchanger 74 is divided into two sub flows 120, 122. A first sub-stream 120 is fed to the seventh exchanger 89 (or directly to the valve 32) and then undergoes all the steps described above in the context of the first embodiment. The first sub-stream 120 represents at least 70% of the liquefied and sub-cooled stream 30. The second sub-stream 122 is then expanded through the valve 118 to a pressure corresponding to the pressure of the gas stream 36 upstream of one of the compression stages of the compression unit 24. More preferably, the second sub-stream 122 is expanded to a pressure corresponding to that of the stream entering the compression stage at which the first part 86 of the overhead stream is injected. The relaxed second sub-stream 122 thus has a temperature below -25°C and in particular between -60°C and -30°C. The second sub-stream 122 is then heated in the sixth heat exchanger 74 by heat exchange with the liquefied intermediate stream 69. Preferably, all of the second sub-stream 122 is vaporised at the sixth heat exchanger 74. The second sub-stream 122 recovered from the sixth heat exchanger 74 is then injected into the carbon dioxide-rich gas stream 36 for recycling. The overhead gas stream 80 is also introduced into the sixth heat exchanger 74 to be heated by heat exchange with the liquefied intermediate stream 69, before being separated into the two parts 86, 88. Preferably, the second sub-stream 122 and the overhead gas stream 80 are introduced into the sixth heat exchanger 74 as separate streams. In particular, the second sub-stream 122 and the overhead gas stream 80 are not mixed either before or within the sixth heat exchanger 74. This third embodiment is advantageous in that it reduces the need for external coolant to operate the fifth heat exchanger 72. It thus makes it possible to limit the operating costs of the method according to the invention.
A installation 310 according to a fourth embodiment of the invention is schematically shown in Figure 4. The installation 310 is similar to the installation 210 of the second embodiment except that directly after being heated in the sixth heat exchanger 74, the overhead gas stream 80 and the second sub-stream 122 are immediately introduced into the fifth heat exchanger 72 where they are heated again by heat exchange with the dry gas stream 62.
The overhead gas stream 80 and the second sub-stream 122 are then introduced into the fourth heat exchanger 67 where they are heated again by heat exchange this time with the compressed gas stream 56. Preferably, the second sub-stream 122 and the overhead gas stream 80 are introduced into the fifth heat exchanger 72 and into the fourth heat exchanger 67 as separate streams. In particular, the second sub-stream 122 and the overhead gas stream 80 are not mixed either before or within the fifth heat exchanger 72 and/or the fourth heat exchanger 67. The heated overhead gas stream 80 recovered from the fourth heat exchanger 67 is then divided into two parts 86, 88 which are recycled back into the installation 310 by analogy with the methods described above. The second sub-stream 122 is then fully recycled in the installation 310 by injection into the carbon dioxide-rich gas stream 36 upstream of one of the compression stages of the compression unit 24. This fourth embodiment is advantageous in that it further reduces the need for external coolant, particularly for the operation of the fourth heat exchanger 67 and the fifth heat exchanger 72. It thus makes it possible to limit the operating costs of the method according to the invention.
An installation 410 according to a fifth embodiment of the invention is schematically shown in Figure 5. The installation 410 is similar to the installation 310 of the fourth embodiment shown in Figure 4 except that the overhead gas stream 80 recovered at the outlet 84 of the expansion column 34 is injected entirely into the second sub-stream 122, at the outlet of the valve 118, to form a common stream 412. The common stream 412 is then heated by passing successively through the sixth exchanger 74, the fifth exchanger 72 and the fourth exchanger 67 by analogy with the fourth embodiment. After passing through the sixth exchanger 74, the fifth exchanger 72 and the fourth exchanger 67, the common stream 412 is divided into two parts 414, 416. The first part 414 of the common stream 412 is injected into the carbon dioxide-rich gas stream 36 upstream of one of the compression stages of the compression unit 24. The second part 416 of the common stream 412 is injected into the industrial waste stream 16, before it is introduced into the capture unit 22. This fifth embodiment is advantageous in that it reduces the investment costs associated with the method of the invention.
The installation and the method according to the invention therefore allow the deoxygenation of C02 without the need for a deoxygenation reactor or a complex configuration dedicated to the purging of incondensables or a low temperature condenser. This gives the invention a competitive advantage in terms of capital expenditure (CAPEX). This deoxygenation of C02 is achieved efficiently without any requirement for a catalyst, or external utilities such as hydrogen or cold refrigerant. This gives the invention a competitive advantage in terms of capital expenditure (OPEX). The associated C02 emissions are also reduced, which is favourable for this type of method whose objective is to capture C02 for sequestration. As no catalyst is used, the method according to the invention is not sensitive to sulphur contaminants. No pressurised hydrogen is required in the method. This considerably reduces the risks in terms of safety requirements for the installation.
Furthermore, no direct venting to atmosphere of a C0 2-rich stream is necessary to avoid the accumulation of non-condensables (e.g. oxygen), which would lead to a pressure build-up. As a result, the C02 recovery rate is maximised.
Throughout this specification and the claims which follow, unless the context requires otherwise, the word "comprise", and variations such as "comprises" and "comprising", will be understood to imply the inclusion of a stated integer or step or group of integers or steps but not the exclusion of any other integer or step or group of integers or steps. The reference in this specification to any prior publication (or information derived from it), or to any matter which is known, is not, and should not be taken as an acknowledgment or admission or any form of suggestion that that prior publication (or information derived from it) or known matter forms part of the common general knowledge in the field of endeavor to which this specification relates.

Claims (17)

  1. THE CLAIMS DEFINING THE INVENTION ARE AS FOLLOWS: 1. A method for recovering a flow of liquefied carbon dioxide from an industrial waste gas , comprising the following steps: - introducing the industrial waste gas into a carbon dioxide capture unit to form a carbon dioxide-rich gas stream and a carbon dioxide-poor effluent stream; - compressing the gas stream in one or more compression stages to form a compressed gas stream; - drying the compressed gas stream to form a dry gas stream; - cooling, liquefying, and sub-cooling the dry gas stream to form a liquefied and sub cooled stream, - partially expanding the liquefied and sub-cooled stream to form an expanded stream comprising a liquid and a gaseous fraction, - introducing the expanded stream into an expansion column to form an overhead gas stream and recovering the liquefied carbon dioxide flow at the bottom of the column, characterised in that a first part of the overhead gas stream is injected into the industrial waste gas, before it is introduced into the capture unit, and in that a second part of the overhead gas stream is injected into the carbon dioxide-rich gas stream, upstream of one of the compression stages, and in that a liquid stream withdrawn at the bottom of the expansion column is heated to form a reboiled stream, said reboiled stream then being injected into the expansion column.
  2. 2. The method according to claim 1, wherein the industrial waste gas contains less than 50% by mass of carbon dioxide.
  3. 3. The method according to claim 2, wherein the industrial waste gas contains less than 40% by mass of carbon dioxide.
  4. 4. The method according to claim 3, wherein the industrial waste gas contains from 2% to 40% by mass of carbon dioxide.
  5. 5. The method according to any of the preceding claims, wherein the carbon dioxide-rich gas stream has a carbon dioxide content by mass of more than 90%.
  6. 6. The method according to claim 5, wherein the carbon dioxide-rich gas stream has a carbon dioxide content by mass of more than 95%.
  7. 7. The method according to any of the preceding claims, wherein the first part of the overhead gas stream is at least 50% of the overhead gas stream.
  8. 8. The method according to claim 7, wherein the first part of the overhead gas stream represents from 70% to 95% of the overhead gas stream.
  9. 9. The method according to any of the preceding claims, wherein the liquid stream is heated by heat exchange with the liquefied and sub-cooled stream.
  10. 10. The method according to any one of the preceding claims, wherein, prior to the partial expansion step, the liquefied and sub-cooled stream is separated into a first sub-stream and a second sub-stream , the first sub-stream then being partially expanded and introduced into the expansion column and the second sub-stream being placed in heat exchange relationship with the dry gas stream.
  11. 11. The method according to claim 10, wherein the overhead gas stream is placed in heat exchange relationship with the dry gas stream.
  12. 12. The method according to claim 10 or 11, wherein the overhead gas stream is mixed with the second sub-stream to form a common stream, the common stream then being placed in heat exchange relationship with the dry gas stream and/or with the compressed gas stream, said common stream then being divided into a first part which is injected into the gas stream, upstream of one of the compression stages, and a second part which is injected into the industrial waste stream.
  13. 13. The method according to any of the preceding claims, the method being devoid of a catalytic deoxygenation step.
  14. 14. The method according to any of the preceding claims, wherein at the capture unit the industrial waste gas is brought into contact with a solvent capable of absorbing carbon dioxide.
  15. 15. The method according to any of the preceding claims, wherein the second part of the overhead gas stream has an 02 content of 0.1 to 1% by weight.
  16. 16. An installation for recovering a flow of liquefied carbon dioxide from an industrial waste gas, comprising: - a carbon dioxide capture unit for forming a carbon dioxide-rich gas stream and a carbon dioxide-poor effluent stream, the capture unit having an inlet for introducing the industrial waste gas, - a compression unit for forming a compressed gas stream comprising an inlet for introducing the carbon dioxide-rich gas stream, - a drying unit for forming a dry gas stream, comprising an inlet for introducing the compressed gas stream, - a cooling and liquefaction unit for cooling, liquefying and sub-cooling the dry gas stream to form a liquefied and sub-cooled stream, the cooling and liquefaction unit comprising an inlet for introducing the dry gas stream, - a valve for partially expanding the liquefied and sub-cooled stream to form an expanded stream comprising a liquid fraction and a gaseous fraction,
    - an expansion column for forming an overhead gas stream and, at the bottom of the column, the liquefied carbon dioxide stream, the expansion column comprising an inlet for introducing the expanded stream and an outlet for recovering the overhead gas stream, wherein the outlet of the expansion column is connected to the inlet of the carbon dioxide capture unit and to the inlet of the compression unit so that a first part of the overhead gas stream is injected into the carbon dioxide-rich gas stream and a second part of the overhead gas stream is injected into the industrial waste gas , and in that the expansion column is connected to a seventh heat exchanger for forming a reboiled stream.
  17. 17. The installation according to claim 16, wherein the seventh heat exchanger further comprises an inlet for the introduction of the liquefied and sub-cooled stream and a recovery outlet connected to the valve, so that the liquefied and sub-cooled stream undergoes a further cooling step by heat exchange with the reboiled stream.
    52 40 10 14 100 54
    38 55 47 42 48 -18- 46 36 16 50 44
    98 51 28 1/5
    74 96 78 80 88 56 64 67 26 66 65 62 68 72 32 84 86 82 58 60 90 92 34 69 70 30 89
    91 -20- 24 94 12
    52 40 110 14 100 54
    38 55 47 42 48 -18- 46 36 16 50 44
    98 51 28 112 2/5
    74 70 96 89 114 116 78 80 88 67 26 66 65 56 64 32 62 68 72 84 86 82 58 60 92 34 69 30
    -20- 91 90 94 24 12
    52 40 210 14 100 54
    38 55 47 42 48 -18- 46 36 16 50 44
    98 51 74 28 96 89 114 116 78 80 3/5
    88 56 64 67 26 66 65 62 68 72 118 32 86 84 120 82 58 60 92 34 69 30
    -20- 70 122 112 91 90 94 24 12
    52 40 310 14 100 54
    38 55 47 42 48 -18- 46 36 16 50 44
    98 51 72 28 74 96 89 114 116 78 80 4/5
    88 67 56 64 26 118 32 66 62 84 120 86 65 68 82 58 60 92 34 69 30 70 -20- 122 112 91 90 94 24 12
    52 40 410 14 100 54
    38 55 47 42 48 -18- 46 36 16 50 44
    98 51 72 28 74 412 118 122 89 78 80 5/5
    416 56 64 67 66 116 32 26 62 84 120 65 68 82 414 58 60 92 34 69 30 70 -20- 112 91 114 94 24 90 12
AU2022203999A 2021-06-09 2022-06-09 Process for the recovery of a liquefied CO2 stream from an industrial waste gas and associated installation Pending AU2022203999A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP21305787.0 2021-06-09
EP21305787 2021-06-09

Publications (1)

Publication Number Publication Date
AU2022203999A1 true AU2022203999A1 (en) 2023-01-05

Family

ID=76483254

Family Applications (1)

Application Number Title Priority Date Filing Date
AU2022203999A Pending AU2022203999A1 (en) 2021-06-09 2022-06-09 Process for the recovery of a liquefied CO2 stream from an industrial waste gas and associated installation

Country Status (2)

Country Link
EP (1) EP4102163A1 (en)
AU (1) AU2022203999A1 (en)

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2884305A1 (en) * 2005-04-08 2006-10-13 Air Liquide Carbon dioxide separating method for iron and steel industry, involves receiving flow enriched in carbon dioxide from absorption unit, sending it towards homogenization unit and subjecting carbon dioxide to intermediate compression stage
US8911535B2 (en) * 2010-10-06 2014-12-16 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Carbon dioxide removal process
FR2968575A1 (en) * 2010-12-08 2012-06-15 Air Liquide PROCESS AND APPARATUS FOR PRODUCING CARBON DIOXIDE ENRICHED FLUID FROM A WASTE GAS OF AN IRONWORK UNIT
KR101153080B1 (en) 2011-10-11 2012-06-04 한국가스공사연구개발원 Carbon dioxide liquefaction process
FR3016436B1 (en) 2014-01-10 2019-05-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude METHOD AND APPARATUS FOR LIQUEFACTING A GASEOUS CO2 CURRENT
EP3318829B1 (en) * 2016-11-04 2022-05-11 General Electric Technology GmbH System and method for producing liquid carbon dioxide
CN209828305U (en) 2018-12-17 2019-12-24 新疆誉州气体制造有限公司 Rectifying tower for purifying carbon dioxide

Also Published As

Publication number Publication date
EP4102163A1 (en) 2022-12-14

Similar Documents

Publication Publication Date Title
US8080090B2 (en) Process for feed gas cooling in reboiler during CO2 separation
US7850763B2 (en) Purification of carbon dioxide
US7819951B2 (en) Purification of carbon dioxide
US8268050B2 (en) CO2 separation apparatus and process for oxy-combustion coal power plants
US8088196B2 (en) Purification of carbon dioxide
US4977745A (en) Method for the recovery of low purity carbon dioxide
US4305733A (en) Method of treating natural gas to obtain a methane rich fuel gas
US7124605B2 (en) Membrane/distillation method and system for extracting CO2 from hydrocarbon gas
US9109831B2 (en) Process and apparatus for the separation of a gaseous mixture
US7766999B2 (en) Process for vaporizing the product CO2 at two different pressures during CO2 separation
US20110132034A1 (en) Two stage process for producing purified gas
WO2007073201A1 (en) An energy efficient process for removing and sequestering co2 from energy process plants exhaust gas
US20090299122A1 (en) Process for producing a purified hydrocarbon gas
US20080196583A1 (en) Process for recycling of top gas during co2 separtion
CN112393527A (en) LNG flash steam recovery method and system
AU2022203999A1 (en) Process for the recovery of a liquefied CO2 stream from an industrial waste gas and associated installation
JP2005509831A (en) Helium production method and helium production apparatus
Shah Carbon dioxide (CO2) compression and purification technology for oxy-fuel combustion
US20090299120A1 (en) Process for producing purified gas
CN214009705U (en) LNG flash distillation vapour recovery system
CN117887496A (en) Dehydration decarburization coupling carbon capturing system and method by low-temperature methanol washing one-step method
Ha CO2 separation apparatus and process for oxy-combustion coal power plants
Shabbir Low BTU Gas Monetisation Technology Commercial Evaluation
AU2007201677A1 (en) Configurations and methods for improved acid gas removal
Linde et al. Process for separation of CO2 from CO2 containing gases