US20080245101A1 - Integrated Method and Installation for Cryogenic Adsorption and Separation for Producing Co2 - Google Patents

Integrated Method and Installation for Cryogenic Adsorption and Separation for Producing Co2 Download PDF

Info

Publication number
US20080245101A1
US20080245101A1 US11/910,959 US91095906A US2008245101A1 US 20080245101 A1 US20080245101 A1 US 20080245101A1 US 91095906 A US91095906 A US 91095906A US 2008245101 A1 US2008245101 A1 US 2008245101A1
Authority
US
United States
Prior art keywords
unit
gas
adsorption
cryogenic
stream
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
US11/910,959
Other languages
English (en)
Inventor
Richard Dubettier-Grenier
Vincent Gueret
Frederick Lockwood
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
Individual
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
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=36954598&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=US20080245101(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Priority claimed from FR0550906A external-priority patent/FR2884304A1/fr
Priority claimed from FR0552459A external-priority patent/FR2872890A3/fr
Application filed by Individual filed Critical Individual
Assigned to L'AIR LIQUIDE, SOCIETE ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE reassignment L'AIR LIQUIDE, SOCIETE ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: DUBETTIER-GRENIER, RICHARD, GUERET, VINCENT, LOCKWOOD, FREDERICK
Publication of US20080245101A1 publication Critical patent/US20080245101A1/en
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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/067—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation 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
    • B01D53/02—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 adsorption, e.g. preparative gas chromatography
    • B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/50—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"
    • F25J1/004—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
    • F25J1/006—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
    • 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
    • F25J1/0209—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 as at least a three level refrigeration cascade
    • F25J1/021—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 as at least a three level refrigeration cascade using a 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
    • F25J1/0221—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 the cold stored in an external cryogenic component in an open 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
    • 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
    • F25J3/0204—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 feed stream
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • 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
    • F25J3/0204—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 feed stream
    • F25J3/0223—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis 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
    • 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
    • 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
    • F25J3/04—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 for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04181—Regenerating the adsorbents
    • 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
    • F25J3/04—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 for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04612—Heat exchange integration with process streams, e.g. from the air gas consuming unit
    • 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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/062—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • 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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/0625—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/22—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40001—Methods relating to additional, e.g. intermediate, treatment of process gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/416—Further details for adsorption processes and devices involving cryogenic temperature treatment
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • 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
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • 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
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • F25J2205/70—Heating the adsorption vessel
    • 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
    • F25J2210/12—Refinery or petrochemical off-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
    • 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
    • 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
    • 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
    • F25J2220/84—Separating high boiling, i.e. less volatile components, e.g. NOx, SOx, H2S
    • 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
    • F25J2230/04—Compressor cooling arrangement, e.g. inter- or after-stage cooling or condensate removal
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/32—Compression of the product 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/80—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/80—Hot exhaust gas turbine combustion engine
    • F25J2240/82—Hot exhaust gas turbine combustion engine with waste heat recovery, e.g. in a combined cycle, i.e. for generating steam used in a Rankine 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/90—Hot gas waste turbine of an indirect heated gas for power generation
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
    • 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
    • F25J2260/02—Integration in an installation for exchanging heat, e.g. for waste heat 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
    • 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
    • F25J2270/04—Internal refrigeration with work-producing gas expansion 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
    • F25J2270/14—External refrigeration with work-producing gas expansion 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
    • F25J2270/60—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
    • F25J2270/90—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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/902—Details about the refrigeration cycle used, e.g. composition of refrigerant, arrangement of compressors or cascade, make up sources, use of reflux exchangers 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
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open 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
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/906—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by heat driven absorption chillers
    • 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
    • F25J2290/62—Details of storing a fluid in a tank
    • 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
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • the present invention relates to an integrated method of adsorption and cryogenic separation for separating CO 2 contained in a gas and to an installation for implementing such a method.
  • the prevalent technology for removing and/or recovering the CO 2 contained in industrial effluents is chemical absorption and, more particularly, scrubbing with amines (MDEA, MEA, etc.) which serve to produce pure low pressure CO 2 , typically having a CO 2 purity above 99%.
  • the chemical scrubbing methods have many limitations or drawbacks, that is: large quantity of steam required, sensitivity to oxygen, corrosion, high operating cost, solvent entrainment and, in general, releases of chemicals in non-negligible quantities, such as amines, ammonia, salts issuing from the amine regenerator, amine degeneration products, etc.
  • pressure swing adsorption like the VPSA (Vacuum Pressure Swing Adsorption), VSA (Vacuum Swing Adsorption) or PSA (Pressure Swing Adsorption) methods.
  • VPSA Vauum Pressure Swing Adsorption
  • VSA Vauum Swing Adsorption
  • PSA Pressure Swing Adsorption
  • VPSA unit a gas separation or purification unit using a cyclic adsorption method comprising at least one adsorption phase on an adsorbent at a pressure above 1.5 bar absolute, and a regeneration phase during which the pressure is lower than atmospheric pressure.
  • VSA unit a gas separation or purification unit using a cyclic method comprising at least one adsorption phase on an adsorbent solid at a pressure lower than 1.5 bar absolute, and a regeneration phase during which the pressure is lower than atmospheric pressure.
  • PSA unit a gas separation or purification unit using a cyclic method comprising at least one adsorption phase on an adsorbent solid at a pressure above 1.5 bar absolute, and a regeneration phase during which the pressure is equal to or higher than atmospheric pressure.
  • VPSA VPSA
  • VSA VSA
  • PSA VPSA
  • the basic dry composition of the component is the ratio, by mass or by volume, of the quantity of material of this component to the total quantity of material present, not including water molecules. Thus, if a stream containing, for example, 70% CO 2 also contains 10% water, the basic dry CO 2 content of the stream is about 78% (70%/90%);
  • the relative humidity of a gas is the ratio, in percentage, of the partial pressure of the water vapor effectively contained in the gas to the water vapor saturation pressure under the same pressure and temperature conditions, according to the usual definition;
  • the gas compositions issuing from the adsorption methods described in this document are mean compositions, averaged over a whole number of method cycles, the adsorption methods being cyclic methods;
  • the recovery yield of a compound of a separation unit is the ratio between the quantity of this compound entering the unit and the quantity of this compound leaving the unit in the desired product form.
  • the adsorption method is used in the iron and steel industry for deballasting gases issuing from processes of the DRI (Direct Reduced Iron) or COREX type.
  • the purge gas from the adsorption method which is CO 2 rich, that is, typically containing between 60 and 80% CO 2 , 25% CO and 5% N 2 , leaving this unit, is used as fuel gas because it still contains a significant quantity of CO.
  • the flue gases issuing from the combustion of this gas are discharged to the atmosphere.
  • the streams from a DRI unit are preferably decarbonated by a VPSA unit, as described in document U.S. Pat. No. 5,858,057 and U.S. Pat. No. 5,676,732.
  • the drawback of the flowcharts described in these documents is that the CO 2 obtained is not utilized or stored but is simply discharged to the atmosphere.
  • An adsorption unit is incapable of producing, on an economically acceptable basis or industrially, CO 2 in a purity higher than 90%, in particular a purity between 90 and 96%, and hence particularly even less in a purity higher than 96%, from a CO 2 poor feed gas, that is, often containing less than 45% CO 2 .
  • cryogenic CO 2 separation units including liquefiers, are only used to process gases having a concentration above 50%, preferably above 70% and generally above 90%, because the CO 2 recovery yield of these units declines sharply when the proportion of gas other than CO 2 increases, due to the physical properties of CO 2 mixtures with nitrogen, carbon monoxide, hydrogen, oxygen, methane, etc., and the triple point of CO 2 , which prevents falling to temperatures below ⁇ 50° C.
  • cryogenic unit means an industrial unit for cooling a fluid, for example CO 2 , in which at least one process fluid is cooled to a temperature lower than or equal to 0° C. and undergoes at least one partial condensation step.
  • This unit may, for example, produce CO 2 in gas, liquid or supercritical form.
  • a unit producing a liquid as a product is called a liquefier.
  • Document EP-A-341879 also describes a method for coproducing CO 2 and H 2 , in which a syngas issuing from an SMR followed by a shift reactor is sent to an H 2 PSA from which the offgas, which contains about 50% CO 2 , is sent to a CO 2 PSA.
  • This CO 2 PSA produces a second CO 2 enriched gas containing at least 98% CO 2 , which is sent to a cryogenic separation apparatus that produces a liquid containing at least 99.9% CO 2 .
  • the CO 2 PSA produces a CO 2 in a high purity (>98%), which culminates in an overall CO 2 recovery method that is underoptimized.
  • the interface between the H 2 PSA and the CO 2 PSA is described, the interface between the CO 2 PSA and the liquefier is not addressed, although it is a point that raises important problems between a cyclic process and a continuous process.
  • Document EP-B-0417922 describes a method for producing CO 2 from a gas that is relatively poor in CO 2 , which is first sent to adsorption drying beds and then to a distillation column. The incondensable compounds from the column are then sent to a PSA unit and the CO 2 rich gas issuing from this PSA is recycled to the inlet of the liquefier.
  • document GB-A-2174379 describes the use of a membrane instead of the PSA to separate the CO 2 from the stream of incondensables issuing from the column.
  • one object of the inventive method is to obtain, at minimum cost, a CO 2 recovery yield of about 90% and/or a CO 2 product purity meeting the specifications for geological disposal (aquifers, coal 30 seams, etc.) and/or the enhanced recovery of fossil fuels (EOR, ECBM, etc.).
  • the CO 2 purities desired for these applications are generally above about 89%, typically above 94%, and lower than about 99%.
  • One of the subjects of the invention is accordingly an integrated method using an adsorption unit coupled to a cryogenic unit, in which a feed gas containing CO 2 is sent to the adsorption unit where it is separated into a first CO 2 enriched stream and a first CO 2 depleted stream, the first CO 2 enriched stream being sent to the cryogenic unit where it is separated into a second CO 2 rich stream and a second CO 2 depleted stream, characterized in that the first CO 2 enriched stream issuing from the adsorption unit is first sent to gas homogenizing means for attenuating the cyclic variations of flow rates, pressure and/or composition of this first stream, inherent in the cyclic character of the adsorption unit, and then subjected to at least one intermediate compression step before entering the cryogenic unit, that is, upstream and/or prior to its entry into the cryogenic unit.
  • the gas homogenizing means for attenuating the cyclic variations of the stream issuing from the adsorption unit may be, for example, an intermediate storage unit, such as a vessel or reservoir, optionally maintained at a substantially constant pressure. More precisely, this intermediate gas storage unit may, for example, be a gas holder having a variable volume and at substantially constant pressure, or a vessel having a fixed volume equipped with a pressure control system for maintaining a substantially constant pressure.
  • one of the aspects of the present invention is the coupling of an adsorption unit and a cryogenic unit using a first gas homogenizing step for attenuating the cyclic variations of flow rates, compositions and/or pressures of the first CO 2 enriched stream issuing from the adsorption unit and a second intermediate compression step, these two steps being carried out between the adsorption separation step and the cryogenic separation step, that is between the adsorption unit and the cryogenic unit.
  • the homogenizing step serves to attenuate the cyclic variations of the stream issuing from the adsorption unit and can be carried out by using an intermediate gas storage unit or any other device suitable for performing this attenuation/homogenization function, and suitable for collecting all or part of the CO 2 enriched stream leaving the adsorption unit.
  • the adsorption unit therefore first carries out a “preseparation” of the CO 2 and the cryogenic unit then carries out the final separation of the CO 2 by means of various integration devices installed between the adsorption unit and the cryogenic unit.
  • gas homogenizing means or a device for attenuating the cyclic variations of the CO 2 enriched stream issuing from the adsorption unit (flow rate, composition, pressure, etc.) inherent in the cyclic operation of the adsorption unit, serves to ensure continuous operation of the compressor and of the cryogenic unit located downstream.
  • a system is thereby obtained coupling a cyclic batch process employed by the adsorption unit, and a continuous system employed by the cryogenic unit, with reduced process control means at the interface.
  • the two units can be easily uncoupled.
  • the fact of carrying out a compression up to at least 15 bar upstream of the cryogenic unit serves to guarantee the desired yields in the cryogenic unit on input gases containing between 40% and 95% CO 2 , thereby relaxing the constraints on the separation performance of the adsorption unit.
  • part of the incondensable gases issuing from the cryogenic unit is optionally recycled to the adsorption unit and therefore serves to relax the constraints on the separation performance of the cryogenic unit.
  • inventive method may further comprise one or more of the following features:
  • the first CO 2 enriched stream issuing from the adsorption unit has a pressure of less than 4 bar, preferably less than 2 bar, and a CO 2 content of between 40% and 95%, preferably between 60% and 85% and/or a relative humidity above 5%,
  • the second CO 2 rich stream issuing from the cryogenic separation unit has a CO 2 content above 80%, preferably above 90%, and even more preferably above 95%.
  • the first CO 2 enriched gas leaving the adsorption unit is sent to the gas homogenizing means for attenuating the cyclic variations in flow rate, composition and/or pressure of this gas, and is then subjected to the intermediate compression,
  • the gas homogenizing means is a mixing vessel or reservoir, for example a constant volume vessel with pressure control or a gas holder having a variable volume and substantially constant pressure,
  • the first CO 2 depleted stream produced by the adsorption unit is expanded in a turbine which can provide refrigerating capacity to the cryogenic unit,
  • the first CO 2 poor gas produced by the adsorption unit is first cooled before being expanded in the turbine
  • At least part of the second CO 2 poor gas leaving the cryogenic unit is returned to the absorbtion unit, particularly either to the suction inlet of the compressor feeding the adsorption unit, or upstream of the adsorber(s) of the adsorption unit, or in the adsorbers during a repressurizing step, in cocurrent or countercurrent, or in the absorber(s) during an adsorption step,
  • At least part of the second CO 2 depleted gas leaving the cryogenic unit is expanded in a turbine and then recycled to the adsorption unit, either to the suction inlet of the feed compressor, or upstream of the adsorber(s), or in the adsorber(s) during a repressurizing step, in cocurrent or countercurrent, or in the adsorber(s) during an adsorption step,
  • the recycled gas is first heated by direct combustion of this gas (injection of air or enriched air) and/or by heating in a boiler preferably burning blast furnace gas and/or by exchange with a fluid from the steel plant, whose temperature is higher than 150° C. and/or by exchange with the first CO 2 enriched gas produced by the adsorption unit upstream of the cryogenic unit,
  • At least part of the second CO 2 poor gas leaving the cryogenic unit is used as fuel for heating the gas of the cryogenic unit, heating the regeneration heater of the cryogenic unit, for example drying by adsorption, and/or heating the first CO 2 poor gas from the adsorption unit, before or after expansion in an optional turbine, and/or heating a regeneration heater of an air separation unit and/or producing steam which can be used in the installation by the regeneration heater of the cryogenic unit and/or, one or more drive turbines of the machines and/or a refrigerating unit by absorption serving for example to cool the gas before the purifiers of the cryogenic unit and/or a heat exchanger heating the first CO 2 poor gas leaving the adsorption unit,
  • At least part of the first CO 2 poor gas leaving the adsorption unit is used as fuel to heat the regeneration heater, for example for drying beds, of the cryogenic unit and/or to produce steam which can be used in the installation by the regeneration heater and/or one or more drive turbines of the machines and/or a refrigerating unit by absorption serving for example to cool the gas before the purifiers of the cryogenic unit and/or a heat exchanger heating the first CO 2 poor gas leaving the adsorption unit,
  • the refrigerating unit of the cryogenic unit also serves to cool the gas entering the adsorption unit
  • the first CO 2 enriched gas leaving the adsorption unit is sent to a mixing vessel or reservoir before being introduced into the cryogenic unit,
  • the incondensable compounds leaving the cryogenic unit are sufficiently cooled to freeze CO 2 in the form of dry ice and to separate the CO 2 thereby frozen from the stream containing the incondensable compounds,
  • At least part of the CO 2 enriched stream compressed in the intermediate compression step is cooled to a temperature above 0° C., and the liquid part which condenses is preferably removed, for example in a phase separation device.
  • the invention also relates to an integrated installation for producing CO 2 from a feed gas containing CO 2 , comprising an adsorption unit for separating the gas containing CO 2 into a first CO 2 enriched stream and a first CO 2 depleted stream, the adsorption unit feeding a cryogenic unit with said first CO 2 enriched stream, and a cryogenic unit for separating the first CO 2 rich stream issuing from the adsorption unit into a second CO 2 rich stream and a second CO 2 poor stream, characterized in that the CO 2 enriched stream issuing from the adsorption unit has a CO 2 content of between 40 and 95% and in that it further comprises a gas homogenizing device or means suitable for attenuating the cyclic variations (flow rate, composition, pressure, etc.) of the CO 2 enriched stream issuing from the adsorption unit and intermediate compression means, arranged on the path of the first CO 2 enriched stream, between the adsorption unit and the cryogenic unit.
  • the CO 2 enriched stream issuing
  • the gas homogenizing means are arranged upstream of the compression means, that is between the adsorption unit and the compression means.
  • the installation of the invention optionally also comprises means for carrying out gas recyclings between the adsorption unit and the cryogenic unit, for example means for recycling at least part of the incondensable gases issuing from the cryogenic unit to the adsorption unit, particularly either at the suction inlet of the compressor feeding the adsorption unit, or upstream of the adsorber(s) of the adsorption unit, or in the adsorbers during a repressurizing step, in cocurrent or countercurrent, or in the adsorber(s) during an adsorption step, the recycles optionally passing through heating, combustion and expansion means.
  • gas recyclings between the adsorption unit and the cryogenic unit for example means for recycling at least part of the incondensable gases issuing from the cryogenic unit to the adsorption unit, particularly either at the suction inlet of the compressor feeding the adsorption unit, or upstream of the adsorber(s) of the adsorption unit, or in the adsorbers during a repressurizing
  • FIGS. 1 to 5 which illustrate embodiments of the invention.
  • FIGS. 6 and 7 which are diagrams of cryogenic units 9 suitable for being used in a method according to the invention.
  • FIG. 1 shows an adsorption unit 3 of the VPSA, VSA or PSA type fed with a feed gas 1 , also called gas to be processed, which contains, for example between 10 and 60% CO 2 , mixed with at least one other gas which may be N 2 , CO, H 2 , O 2 , CH 4 , Ar, H 2 O, etc.
  • This gas may, for example be a blast furnace gas containing on average for example 23% CO 2 , 23% CO, 50% N 2 and 4% H 2 , available at about 50° C. and 2 bar absolute, at a flow rate for example between 50 000 Nm 3 /h and 800 000 Nm 3 /h.
  • the gas 1 to be processed by the adsorption unit 3 is typically at a pressure between 1 and 10 bar absolute. This pressure is reached by optionally adding a compressor upstream of the adsorber(s) of the adsorption unit 3 .
  • the method of the present invention is an integrated method using, in series, an adsorption unit 3 coupled with a cryogenic unit 9 , the combination being optimized for producing CO 2 at minimum cost, with a CO 2 recovery yield of about 90% and/or a typical CO 2 product purity of about 90 to 99%, particularly by the passage of the CO 2 enriched gas issuing from the adsorption unit through a buffer vessel or reservoir 17 constituting all or part of the gas homogenizing means, and/or an intermediate compression, as described below.
  • the gas 1 to be processed is first sent to the adsorption unit 3 or to the adsorption units, in the case in which a plurality of adsorption units are employed, operating in parallel, where it is separated into a first CO 2 enriched stream 6 and a first CO 2 depleted stream 5 .
  • the first CO 2 enriched stream 6 is produced at lower than 4 bar, typically at lower than 2 bar, for example between 1 and 2 bar, and is then sent to the cryogenic unit 9 , without undergoing other separation steps, except optionally a recovery of part of the water it contains.
  • the first CO 2 enriched stream 6 leaving the adsorption unit 3 has a CO 2 content of between 40% and 95%, typically between 60% and 85%, a pressure of less than 4 bar, typically about 1 to 2 bar, and a relative humidity generally of at least 5%.
  • the step of attenuation of the cyclic variations in flow rate, composition, pressure, etc. 17 and the intermediate compression step 7 are carried out on the first CO 2 enriched stream 6 leaving the adsorption unit 3 , upstream of the cryogenic unit 9 , via one or more compressors or any other suitable gas compression device, placed between these two units 3 , 9 .
  • the gas homogenizing means or device for attenuating the cyclic variations 17 , placed on the path of the CO 2 enriched stream leaving the adsorption unit 3 , before its intermediate compression 7 is for example a constant volume vessel with pressure control or a gas holder having a variable volume and substantially constant pressure.
  • the pressure of this mixing vessel or reservoir is typically lower than 4 bar absolute, preferably lower than 2 bar absolute.
  • the intermediate compression step serves to raise the pressure of the CO 2 enriched gas issuing from the adsorption unit 3 and stored in the mixing vessel or reservoir 17 from a low pressure lower than 4 bar absolute to pressure levels compatible with an efficient cryogenic separation, that is to a pressure of above 15 bar, typically between 20 and 80 bar, in order to improve the CO 2 recovery yield in the cryogenic unit.
  • the compressed gas stream is separated into a second CO 2 rich stream 11 and a second CO 2 poor stream 10 .
  • the second CO 2 rich stream 11 leaving the cryogenic unit 9 has a CO 2 content above 80%, preferably at least 90% even more preferably at least 94%.
  • the first CO 2 enriched stream 6 leaving the adsorption unit 3 is then sent to the gas homogenizing means, then to one or more intermediate compression means or devices 7 , such as one or more compressors or any other device suitable for carrying out a gas compression, before being conveyed, via the line 8 , to a cryogenic unit 9 where it is condensed at least partially and at least once.
  • one or more intermediate compression means or devices 7 such as one or more compressors or any other device suitable for carrying out a gas compression
  • the first CO 2 enriched stream 6 issuing from the adsorption unit is therefore compressed to a pressure above 6 bar absolute, preferably above 20 bar absolute, typically between 20 and 80 bar and preferably between 30 and 50 bar, for a mean CO 2 content of the stream 6 of 40 to 95%, typically between 60 and 85% at the outlet of the adsorption unit 3 .
  • the cryogenic unit 9 which may, for example be a liquefier, produces a second CO 2 poor gas 10 and a second CO 2 rich gas 11 containing at least 80% CO 2 and preferably 90 to 99% CO 2 , or optionally even more than 99% CO 2 .
  • the CO 2 can then be stripped to produce a gas containing even purer CO 2 , for example in a stripping column (not shown) located downstream, before being sent to a user or storage site.
  • a stripping column not shown
  • the adsorption unit 3 further comprises one or more adsorbers operating in parallel, a system of valves and optionally one or more vacuum pumps in the case of a VPSA or VSA unit, a compressor of the gas to be processed, a CO 2 enriched gas storage vessel or reservoir, and/or a CO 2 depleted gas storage vessel or reservoir.
  • the cryogenic unit 9 may in particular comprise one or more gas prepurifiers, typically containing alumina or a molecular sieve, an active carbon or a silica gel, and their regeneration heater, a cold heat exchanger and optionally one or more condensers/reboilers, separator pots, distillation columns, compressors, devices for the catalytic removal or not of the CO 2 and hydrogen, mechanical or absorption refrigerating unit, and/or precooling device before the dryers.
  • gas prepurifiers typically containing alumina or a molecular sieve, an active carbon or a silica gel, and their regeneration heater, a cold heat exchanger and optionally one or more condensers/reboilers, separator pots, distillation columns, compressors, devices for the catalytic removal or not of the CO 2 and hydrogen, mechanical or absorption refrigerating unit, and/or precooling device before the dryers.
  • FIG. 2 differs from FIG. 1 only in that the first CO 2 depleted gas 5 is expanded in a turbine 12 .
  • the energy recovered on the turbine 12 can either serve to drive the compressor 7 , even partially with an auxiliary motor, or can be used to generate electricity.
  • the turbine 12 transfers part of its refrigerating capacity to the cryogenic unit 9 , via the line 13 .
  • FIG. 3 differs from FIG. 2 only in the incorporation of a cooler 14 upstream of the turbine 12 , which serves to transfer additional refrigerating capacity to the cryogenic unit 9 , by sending the gas expanded in the turbine 12 to a heat exchanger of the cryogenic unit 9 .
  • a cooler 14 upstream of the turbine 12 which serves to transfer additional refrigerating capacity to the cryogenic unit 9 , by sending the gas expanded in the turbine 12 to a heat exchanger of the cryogenic unit 9 .
  • the liquid CO 2 vaporizes in the cryogenic unit
  • most or even all of the refrigerating input issues from this latent heat.
  • a contribution, even a small one, to offset the heat losses may be necessary or desirable, and can accordingly be supplied by the expanded gas.
  • the purpose of the expansion is to produce energy rather than to supply refrigerating capacity to the cryogenic unit, it is then more advantageous to heat the stream to be expanded.
  • FIG. 4 shows another embodiment in which the second CO 2 poor stream 10 is divided into two auxiliary streams 10 A and 10 B.
  • One of these streams 10 A can serve as a purge, while the other 10 B is expanded in a turbine 22 and the resulting stream is then recycled upstream of the adsorption unit 3 .
  • the entire stream 10 can be recycled via the turbine 22 , which is equivalent to eliminating the line 10 A.
  • the expanded gas leaving the turbine 22 may optionally be sent to the adsorbers of the adsorption unit 3 during a repressurizing step or during an adsorption step.
  • the energy recovered at the shaft of the turbine 22 can either serve to generate electricity, or to drive a compressor.
  • the gas can thus be heated by direct combustion, by heating in a boiler, or by heat exchange with a fluid available on the site, for example the flue gases issuing from a Cowper stove.
  • FIG. 6 shows a first detailed example of a cryogenic unit 9 according to FIGS. 1 to 5 for separating a gas containing CO 2 by partial condensation.
  • the first CO 2 rich gas stream 6 that is having a CO 2 content of between 40% and 95%, typically between 60% and 85%, is conveyed by the line 8 (see FIG. 1 to 5 ) to the cryogenic unit 9 .
  • the gas can be compressed therein by an additional compressor 55 , particularly if it is desirable to slightly raise the pressure of the gas compressed in the intermediate compression unit 7 .
  • the compressed gas is then sent to a gas purifying device 33 which, for example, removes the impurities by adsorption through a radial or axial bed in order to prepurify (and/or dry) the CO 2 rich gas, before cooling it below ⁇ 10° C.
  • This purifier device 33 is periodically regenerated by a gas heated in a regeneration heater (not shown).
  • the purified gas recovered by the line 35 is then cooled in a heat exchanger 37 where it is partially condensed.
  • the condensed liquid phase 51 is separated from the gas phase 53 in a phase separator 45 .
  • the liquid part 51 is sent to a storage unit 49 after expansion in a pressure reducing valve 70 , while the gas part 53 is sent to a second heat exchanger 43 where it is partially condensed.
  • the partially condensed phase 54 is separated from the gas phase 61 in a phase separator 47 .
  • the liquid stream 57 withdrawn from the phase separator 47 is sent to the storage unit 49 , after expansion, here also in a pressure reducing valve 71 .
  • the gas stream 59 issuing from the storage unit 49 is sent successively to the heat exchangers 43 and 37 in order to utilize the refrigerating capacity it contains, before being recycled to the additional compression means 55 , if such means are present in the cryogenic unit 9 , or, in the absence thereof to an intermediate step of the intermediate compressor 7 located between the adsorption units 3 and the cryogenic unit 9 .
  • the stream 10 issuing from the phase separator 47 is also sent successively to the heat exchangers 43 and 37 in order to utilize the refrigerating capacity it contains.
  • the liquid product 11 containing at least 90% CO 2 is withdrawn from the storage unit 49 .
  • the refrigerating capacity for liquefaction in the heat exchangers 37 and 43 is supplied by two conventional refrigerating cycles 39 , 41 , which may optionally be coupled.
  • FIG. 7 shows a second example of a cryogenic unit 9 usable in the installations described in FIGS. 1 to 5 , which serves to carry out a purification and produce CO 2 at high pressure, that is up to about 60 bar, hence ready to be transported by gas lines.
  • the gas stream 8 having a CO 2 content of between 40% and 95%, typically between 60% and 85%, is compressed (at 55 ) then purified (at 33 ) and cooled in the heat exchanger 37 where it is partially condensed
  • the condensed phase 51 is separated from the gas phase 53 in a phase separator 45 .
  • the gas part 53 is sent to a second heat exchanger 43 where it is partially condensed.
  • the partially condensed phase 54 is separated from the gas phase in a phase separator 47 .
  • the liquid stream 57 withdrawn from the phase separator 47 is expanded and sent successively to the heat exchangers 43 and 37 in order to utilize the refrigerating capacity it contains.
  • the gas stream issuing from the phase separator 47 is sent successively to the heat exchangers 43 and 37 in order to utilize the refrigerating capacity it contains.
  • the liquid part 51 issuing from the first phase separator 45 is also expanded and sent successively to the heat exchangers 43 and 37 in order to utilize the refrigerating capacity it contains.
  • the streams 67 and 68 are then combined and compressed to a pressure necessary for transport by gas lines If the combined stream 69 is a two-phase stream, it is heated to make it completely gaseous before being sent to the compressor 73 , and then conveyed it via the line 11 .
  • This product stream, conveyed via the line 11 is formed of CO 2 having a purity of at least 90%, typically at least 90 to 96%.

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)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
US11/910,959 2005-04-08 2006-03-30 Integrated Method and Installation for Cryogenic Adsorption and Separation for Producing Co2 Abandoned US20080245101A1 (en)

Applications Claiming Priority (7)

Application Number Priority Date Filing Date Title
FR0550906 2005-04-08
FR0550906A FR2884304A1 (fr) 2005-04-08 2005-04-08 Procede integre d'absorption et de separation cryogenique pour la production de co2 et installation pour la mise en oeuvre du procede
FR0552459 2005-08-08
FR0552459A FR2872890A3 (fr) 2005-08-08 2005-08-08 Procede integre d'adsorption et de separation cryogenique pour la production de co2 et installation pour la mise en oeuvre du procede
FR0553219A FR2884305A1 (fr) 2005-04-08 2005-10-24 Procede de recuperation et liquefaction du co2 contenu dans un gaz pauvre en co2
FR0553219 2005-10-24
PCT/FR2006/050276 WO2006106253A2 (fr) 2005-04-08 2006-03-30 Procede et installation integres d'adsorption et de separation cryogenique pour la production de co2

Publications (1)

Publication Number Publication Date
US20080245101A1 true US20080245101A1 (en) 2008-10-09

Family

ID=36954598

Family Applications (1)

Application Number Title Priority Date Filing Date
US11/910,959 Abandoned US20080245101A1 (en) 2005-04-08 2006-03-30 Integrated Method and Installation for Cryogenic Adsorption and Separation for Producing Co2

Country Status (7)

Country Link
US (1) US20080245101A1 (de)
EP (2) EP1869385B1 (de)
AT (1) ATE441822T1 (de)
DE (1) DE602006008912D1 (de)
FR (1) FR2884305A1 (de)
PL (1) PL1869385T3 (de)
WO (1) WO2006106253A2 (de)

Cited By (34)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20080190117A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank and operation of the same
US20080295527A1 (en) * 2007-05-31 2008-12-04 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship with nitrogen generator and method of operating the same
US20090013717A1 (en) * 2007-07-11 2009-01-15 L'air Liquide, Societe Anonyme Our L'etude Et L'exploitation Des Procedes George Claude Process and apparatus for the separation of a gaseous mixture
US20090288447A1 (en) * 2008-05-22 2009-11-26 Alstom Technology Ltd Operation of a frosting vessel of an anti-sublimation system
US20090301108A1 (en) * 2008-06-05 2009-12-10 Alstom Technology Ltd Multi-refrigerant cooling system with provisions for adjustment of refrigerant composition
US20100024471A1 (en) * 2008-08-01 2010-02-04 Alstom Technology Ltd Method and system for extracting carbon dioxide by anti-sublimation at raised pressure
US20100050687A1 (en) * 2008-09-04 2010-03-04 Alstom Technology Ltd Liquefaction of gaseous carbon-dioxide remainders during anti-sublimation process
US20100122542A1 (en) * 2008-11-17 2010-05-20 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and apparatus for adjusting heating value of natural gas
WO2012004138A1 (fr) * 2010-07-06 2012-01-12 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Appareil integre de liquefaction de dioxyde de carbone et de stockage de dioxyde de carbone liquide et procede de regulation en pression de stockage d'un tel appareil
FR2972793A1 (fr) * 2011-03-16 2012-09-21 Air Liquide Procede et appareil de liquefaction d'un gaz riche en co2 contenant au moins une impurete legere
FR2972792A1 (fr) * 2011-03-16 2012-09-21 Air Liquide Procede et appareil de liquefaction de co2
FR2973864A1 (fr) * 2011-04-11 2012-10-12 Air Liquide Procede et appareil de liquefaction d'un gaz riche en co2
EP2574392A1 (de) * 2011-09-29 2013-04-03 General Electric Company Anlage und Methode um flüssiges oder festes Kohlendioxid herzustellen und Energie rückzugewinnen.
CN103097843A (zh) * 2010-07-14 2013-05-08 阿尔斯通技术有限公司 利用单级膨胀和用于高压蒸发的泵的co2节能制备
US20130118205A1 (en) * 2010-07-19 2013-05-16 Bp Alternative Energy International Limited Separation of a gas mixture
US20130167583A1 (en) * 2010-03-03 2013-07-04 Alstom Technology Ltd Method and installation for liquefying flue gas from combustion installations
CN103249464A (zh) * 2010-12-08 2013-08-14 乔治洛德方法研究和开发液化空气有限公司 由黑色冶金单元的废气生产富集二氧化碳的流体的方法和装置
KR20140031241A (ko) * 2011-03-30 2014-03-12 알스톰 테크놀러지 리미티드 냉동 시스템을 사용하는 극저온 ｃｏ₂ 분리
US9086188B2 (en) 2008-04-10 2015-07-21 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and system for reducing heating value of natural gas
US10170782B2 (en) * 2015-06-05 2019-01-01 Fuelcell Energy, Inc. High-efficiency fuel cell system with carbon dioxide capture assembly and method
US10203155B2 (en) 2010-12-23 2019-02-12 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and device for condensing a first fluid rich in carbon dioxide using a second fluid
US10519102B2 (en) * 2013-12-12 2019-12-31 Thyssenkrupp Ag Method for preparation of ammonia gas and CO2 for a urea synthesis process
WO2020012129A1 (fr) * 2018-07-11 2020-01-16 Engie Dispositif et procédé de liquéfaction d'un flux de dioxyde de carbone
US11149905B2 (en) 2019-10-03 2021-10-19 Saudi Arabian Oil Company Mobile natural gas storage and transportation unit based on adsorption
US11211625B2 (en) 2016-04-21 2021-12-28 Fuelcell Energy, Inc. Molten carbonate fuel cell anode exhaust post-processing for carbon dioxide
US11508981B2 (en) 2016-04-29 2022-11-22 Fuelcell Energy, Inc. Methanation of anode exhaust gas to enhance carbon dioxide capture
CN116761664A (zh) * 2021-01-29 2023-09-15 日立造船爱诺瓦公司 从含甲烷的气体中去除co2的方法
US11975969B2 (en) 2020-03-11 2024-05-07 Fuelcell Energy, Inc. Steam methane reforming unit for carbon capture
US12095129B2 (en) 2018-11-30 2024-09-17 ExxonMobil Technology and Engineering Company Reforming catalyst pattern for fuel cell operated with enhanced CO2 utilization
US12334607B2 (en) 2019-11-26 2025-06-17 ExxonMobil Technology and Engineering Company Fuel cell assembly with external manifold for parallel flow
US12347910B2 (en) 2019-11-26 2025-07-01 ExxonMobil Technology and Engineering Company Fuel cell power plant with a racked fuel cell module
US12355085B2 (en) 2018-11-30 2025-07-08 ExxonMobil Technology and Engineering Company Cathode collector structures for molten carbonate fuel cell
US12374703B2 (en) 2018-11-30 2025-07-29 ExxonMobil Technology and Engineering Company Flow field baffle for molten carbonate fuel cell cathode
WO2025172226A1 (fr) * 2024-02-16 2025-08-21 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de capture de co2 avec séparation par condensation partielle et/ou distillation et/ou solidification

Families Citing this family (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7819951B2 (en) † 2007-01-23 2010-10-26 Air Products And Chemicals, Inc. Purification of carbon dioxide
US7708804B2 (en) * 2007-07-11 2010-05-04 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for the separation of a gaseous mixture
US20090013868A1 (en) * 2007-07-11 2009-01-15 Arthur Darde Process and apparatus for the separation of a gaseous mixture
FR2918578B1 (fr) * 2007-07-13 2010-01-01 Air Liquide Procede de purification d'un gaz contenant du co2
CA2693994A1 (en) * 2007-07-25 2009-01-29 Bp Alternative Energy International Limited Separation of carbon dioxide and hydrogen
EP2023066A1 (de) * 2007-07-25 2009-02-11 BP Alternative Energy Holdings Limited Trennung von Kohlendioxid und Wasserstoff
EP2023067A1 (de) * 2007-07-25 2009-02-11 BP Alternative Energy Holdings Limited Trennung von Kohlendioxid und Wasserstoff
EP2149769A1 (de) * 2008-07-31 2010-02-03 BP Alternative Energy International Limited Trennung von Kohlendioxid und Wasserstoff
WO2010026057A1 (en) * 2008-09-04 2010-03-11 Alstom Technology Ltd. Liquefaction of gaseous carbon-dioxide remainders during anti-sublimation process
DE102008062497A1 (de) 2008-12-16 2010-06-17 Linde-Kca-Dresden Gmbh Verfahren und Vorrichtung zur Behandlung eines kohlendioxidhaltigen Gasstroms aus einer Großfeuerungsanlage
AU2010222763A1 (en) * 2009-03-09 2011-09-22 Bp Alternative Energy International Limited Separation of carbon dioxide and hydrogen
WO2011018620A2 (en) * 2009-08-12 2011-02-17 Bp Alternative Energy International Limited Separation of carbon dioxide from a mixture of gases
FR2952833A1 (fr) * 2009-11-20 2011-05-27 Air Liquide Integration d'une unite de production de fonte, une unite d'adsorption, une unite cryogenique et une turbine a gaz
ES2624271T3 (es) * 2010-04-21 2017-07-13 General Electric Technology Gmbh Método para separar dióxido de carbono de gas de humo de plantas de combustión
US20120174621A1 (en) * 2011-01-06 2012-07-12 General Electric Company Carbon dioxide liquefaction system
EP2873939B1 (de) 2013-11-19 2019-02-27 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Verfahren und Vorrichtung zur Herstellung von CO und CO2
FR3108524B1 (fr) * 2020-03-27 2023-03-31 Air Liquide Atténuation des variations de débit, de pression et de masse molaire sur l’effluent gazeux d’un PSA
EP4102163A1 (de) * 2021-06-09 2022-12-14 Technip Energies France Verfahren zur rückgewinnung eines verflüssigten co2-stroms aus einem industriellen abgas und entsprechende anlage
FR3145207B1 (fr) * 2023-01-19 2025-01-31 Air Liquide Procédé de liquéfaction d’un débit riche en dioxyde de carbone
FR3150579A1 (fr) 2023-06-28 2025-01-03 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de séparation d’un mélange contenant du CO2 par condensation partielle et/ou distillation
FR3153881A1 (fr) * 2023-10-06 2025-04-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de distillation d’un mélange de dioxyde de carbone, de monoxyde de carbone et d’azote
FR3155057B1 (fr) 2023-11-07 2026-01-02 Air Liquide Procédé et appareil de séparation d’un mélange gazeux contenant du dioxyde de carbone
FR3155720A1 (fr) 2023-11-24 2025-05-30 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de séparation du gaz résiduaire d’une unité de production de métal ferreux
WO2026046927A1 (en) 2024-08-26 2026-03-05 Ark Capture Solutions Sa Method and system for separating carbon dioxide from a flue gas stream

Citations (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4602477A (en) * 1985-06-05 1986-07-29 Air Products And Chemicals, Inc. Membrane-aided distillation for carbon dioxide and hydrocarbon separation
US4639257A (en) * 1983-12-16 1987-01-27 Costain Petrocarbon Limited Recovery of carbon dioxide from gas mixture
US4952223A (en) * 1989-08-21 1990-08-28 The Boc Group, Inc. Method and apparatus of producing carbon dioxide in high yields from low concentration carbon dioxide feeds
US5220797A (en) * 1990-09-28 1993-06-22 The Boc Group, Inc. Argon recovery from argon-oxygen-decarburization process waste gases
US5582029A (en) * 1995-10-04 1996-12-10 Air Products And Chemicals, Inc. Use of nitrogen from an air separation plant in carbon dioxide removal from a feed gas to a further process
US5676732A (en) * 1995-09-15 1997-10-14 Hylsa, S.A. De C.V. Method for producing direct reduced iron utilizing a reducing gas with a high content of carbon monoxide
US5858057A (en) * 1996-09-25 1999-01-12 Hylsa S.A. De C.V. Method for producing direct reduced iron with a controlled amount of carbon
US6035662A (en) * 1998-10-13 2000-03-14 Praxair Technology, Inc. Method and apparatus for enhancing carbon dioxide recovery
US6301927B1 (en) * 1998-01-08 2001-10-16 Satish Reddy Autorefrigeration separation of carbon dioxide
US20020073845A1 (en) * 2000-12-19 2002-06-20 Fluor Corporation Hydrogen and carbon dioxide coproduction
US6562103B2 (en) * 2001-07-27 2003-05-13 Uop Llc Process for removal of carbon dioxide for use in producing direct reduced iron
US20050155379A1 (en) * 2004-01-19 2005-07-21 Gershtein Vladimir Y. System for supply and delivery of carbon dioxide with different purity requirements
US20060254311A1 (en) * 2003-05-19 2006-11-16 Jean Billy Process and installation for supplying gaseous carbon monoxide and/or a gaseous mixture containing at least 10% carbon monoxide
US20080034790A1 (en) * 2003-11-10 2008-02-14 Patrick Le Bot Method And Installation For Enriching A Gas Stream With One Of The Components Thereof
US7493779B2 (en) * 2002-08-27 2009-02-24 Shell Oil Company Method of removing solid carbon dioxide
US7517390B2 (en) * 2005-03-01 2009-04-14 Linde Aktiengesellschaft Process for adsorber regeneration
US7617701B2 (en) * 2004-04-07 2009-11-17 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for providing a fluid mixture containing at least 10% carbon monoxide
US20100055021A1 (en) * 2005-01-25 2010-03-04 Guillaume Teixeira Method and system for producing carbon monoxide by cryogenic distillation
US7819951B2 (en) * 2007-01-23 2010-10-26 Air Products And Chemicals, Inc. Purification of carbon dioxide

Family Cites Families (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3349571A (en) * 1966-01-14 1967-10-31 Chemical Construction Corp Removal of carbon dioxide from synthesis gas using spearated products to cool external refrigeration cycle
US4270937A (en) * 1976-12-01 1981-06-02 Cng Research Company Gas separation process
JPS5520206A (en) * 1978-07-24 1980-02-13 Showa Tansan Kk Manufacture of saturated liquefied carbon dioxide
US4441900A (en) * 1982-05-25 1984-04-10 Union Carbide Corporation Method of treating carbon-dioxide-containing natural gas
GB8508002D0 (en) 1985-03-27 1985-05-01 Costain Petrocarbon Recovering carbon dioxide
JPS6484087A (en) * 1987-09-24 1989-03-29 Jgc Corp Manufacture of liquefied carbon dioxide
US4963339A (en) 1988-05-04 1990-10-16 The Boc Group, Inc. Hydrogen and carbon dioxide coproduction
GB9105478D0 (en) * 1991-03-15 1991-05-01 Air Prod & Chem Carbon dioxide and acid gas removal and recovery process for fossil fuel fired power plants
JPH04359785A (ja) * 1991-06-05 1992-12-14 Mitsubishi Heavy Ind Ltd 液体二酸化炭素の回収装置
JPH0699034A (ja) * 1992-09-21 1994-04-12 Chubu Electric Power Co Inc 燃焼排ガスからの二酸化炭素の液化分離回収法
JP2967166B2 (ja) * 1996-08-14 1999-10-25 工業技術院長 炭酸ガスの分離・回収方法
CA2294742C (en) * 1997-07-01 2005-04-05 Exxon Production Research Company Process for separating a multi-component gas stream containing at least one freezable component
EP0945163A1 (de) * 1997-10-09 1999-09-29 Gkss-Forschungszentrum Geesthacht Gmbh Ein Verfahren zur Trennung/Rückgewinnung von Gasen
US6070431A (en) 1999-02-02 2000-06-06 Praxair Technology, Inc. Distillation system for producing carbon dioxide
US7201019B2 (en) * 2004-11-19 2007-04-10 Praxair Technology, Inc. Light gas component separation from a carbon dioxide mixture

Patent Citations (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4639257A (en) * 1983-12-16 1987-01-27 Costain Petrocarbon Limited Recovery of carbon dioxide from gas mixture
US4602477A (en) * 1985-06-05 1986-07-29 Air Products And Chemicals, Inc. Membrane-aided distillation for carbon dioxide and hydrocarbon separation
US4952223A (en) * 1989-08-21 1990-08-28 The Boc Group, Inc. Method and apparatus of producing carbon dioxide in high yields from low concentration carbon dioxide feeds
US5220797A (en) * 1990-09-28 1993-06-22 The Boc Group, Inc. Argon recovery from argon-oxygen-decarburization process waste gases
US5676732A (en) * 1995-09-15 1997-10-14 Hylsa, S.A. De C.V. Method for producing direct reduced iron utilizing a reducing gas with a high content of carbon monoxide
US5582029A (en) * 1995-10-04 1996-12-10 Air Products And Chemicals, Inc. Use of nitrogen from an air separation plant in carbon dioxide removal from a feed gas to a further process
US5858057A (en) * 1996-09-25 1999-01-12 Hylsa S.A. De C.V. Method for producing direct reduced iron with a controlled amount of carbon
US6301927B1 (en) * 1998-01-08 2001-10-16 Satish Reddy Autorefrigeration separation of carbon dioxide
US6035662A (en) * 1998-10-13 2000-03-14 Praxair Technology, Inc. Method and apparatus for enhancing carbon dioxide recovery
US6500241B2 (en) * 2000-12-19 2002-12-31 Fluor Corporation Hydrogen and carbon dioxide coproduction
US20020073845A1 (en) * 2000-12-19 2002-06-20 Fluor Corporation Hydrogen and carbon dioxide coproduction
US6562103B2 (en) * 2001-07-27 2003-05-13 Uop Llc Process for removal of carbon dioxide for use in producing direct reduced iron
US7493779B2 (en) * 2002-08-27 2009-02-24 Shell Oil Company Method of removing solid carbon dioxide
US20060254311A1 (en) * 2003-05-19 2006-11-16 Jean Billy Process and installation for supplying gaseous carbon monoxide and/or a gaseous mixture containing at least 10% carbon monoxide
US20080034790A1 (en) * 2003-11-10 2008-02-14 Patrick Le Bot Method And Installation For Enriching A Gas Stream With One Of The Components Thereof
US20050155379A1 (en) * 2004-01-19 2005-07-21 Gershtein Vladimir Y. System for supply and delivery of carbon dioxide with different purity requirements
US7617701B2 (en) * 2004-04-07 2009-11-17 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for providing a fluid mixture containing at least 10% carbon monoxide
US20100055021A1 (en) * 2005-01-25 2010-03-04 Guillaume Teixeira Method and system for producing carbon monoxide by cryogenic distillation
US7517390B2 (en) * 2005-03-01 2009-04-14 Linde Aktiengesellschaft Process for adsorber regeneration
US7819951B2 (en) * 2007-01-23 2010-10-26 Air Products And Chemicals, Inc. Purification of carbon dioxide

Cited By (60)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20080190117A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank and operation of the same
US20080190352A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship and operation thereof
US10352499B2 (en) 2007-02-12 2019-07-16 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and operation of the same
US20090211262A1 (en) * 2007-02-12 2009-08-27 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship having lng circulating device
US8943841B2 (en) 2007-02-12 2015-02-03 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank ship having LNG circulating device
US8820096B2 (en) 2007-02-12 2014-09-02 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and operation of the same
US10508769B2 (en) 2007-02-12 2019-12-17 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and operation of the same
US11168837B2 (en) 2007-02-12 2021-11-09 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and operation of the same
US20080295527A1 (en) * 2007-05-31 2008-12-04 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship with nitrogen generator and method of operating the same
US20090013717A1 (en) * 2007-07-11 2009-01-15 L'air Liquide, Societe Anonyme Our L'etude Et L'exploitation Des Procedes George Claude Process and apparatus for the separation of a gaseous mixture
US9109831B2 (en) 2007-07-11 2015-08-18 AIR LIQUIDE GLOBAL E&C SOLUTIONS US Inc. Process and apparatus for the separation of a gaseous mixture
US9086188B2 (en) 2008-04-10 2015-07-21 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and system for reducing heating value of natural gas
US20090288447A1 (en) * 2008-05-22 2009-11-26 Alstom Technology Ltd Operation of a frosting vessel of an anti-sublimation system
US20090301108A1 (en) * 2008-06-05 2009-12-10 Alstom Technology Ltd Multi-refrigerant cooling system with provisions for adjustment of refrigerant composition
US8163070B2 (en) 2008-08-01 2012-04-24 Wolfgang Georg Hees Method and system for extracting carbon dioxide by anti-sublimation at raised pressure
US20100024471A1 (en) * 2008-08-01 2010-02-04 Alstom Technology Ltd Method and system for extracting carbon dioxide by anti-sublimation at raised pressure
US20100050687A1 (en) * 2008-09-04 2010-03-04 Alstom Technology Ltd Liquefaction of gaseous carbon-dioxide remainders during anti-sublimation process
US20100122542A1 (en) * 2008-11-17 2010-05-20 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and apparatus for adjusting heating value of natural gas
KR101473679B1 (ko) 2010-03-03 2014-12-17 알스톰 테크놀러지 리미티드 연소 설비로부터의 연도 가스를 액화하기 위한 방법 및 설비
CN103229012A (zh) * 2010-03-03 2013-07-31 阿尔斯通技术有限公司 用于液化来自燃烧设备的烟道气的方法和设备
US20130167583A1 (en) * 2010-03-03 2013-07-04 Alstom Technology Ltd Method and installation for liquefying flue gas from combustion installations
US9777961B2 (en) * 2010-03-03 2017-10-03 General Electric Technology Gmbh Method and installation for liquefying flue gas from combustion installations
AU2011222674B2 (en) * 2010-03-03 2015-08-20 General Electric Technology Gmbh Method and installation for liquefying flue gas from combustion installations
WO2012004138A1 (fr) * 2010-07-06 2012-01-12 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Appareil integre de liquefaction de dioxyde de carbone et de stockage de dioxyde de carbone liquide et procede de regulation en pression de stockage d'un tel appareil
FR2962518A1 (fr) * 2010-07-06 2012-01-13 Air Liquide Appareil integre de liquefaction de dioxyde de carbone et de stockage de dioxyde de carbone liquide et procede de regulation en pression de stockage d’un tel appareil
CN103097843A (zh) * 2010-07-14 2013-05-08 阿尔斯通技术有限公司 利用单级膨胀和用于高压蒸发的泵的co2节能制备
US20130118205A1 (en) * 2010-07-19 2013-05-16 Bp Alternative Energy International Limited Separation of a gas mixture
CN103249464A (zh) * 2010-12-08 2013-08-14 乔治洛德方法研究和开发液化空气有限公司 由黑色冶金单元的废气生产富集二氧化碳的流体的方法和装置
KR101829088B1 (ko) * 2010-12-08 2018-02-13 레르 리키드 쏘시에떼 아노님 뿌르 레드 에렉스뿔라따시옹 데 프로세데 조르즈 클로드 철-야금 유닛의 폐가스로부터 이산화탄소 농축 유체를 생성하기 위한 방법 및 장치
CN103249464B (zh) * 2010-12-08 2016-01-20 乔治洛德方法研究和开发液化空气有限公司 由黑色冶金单元的废气生产富集二氧化碳的流体的方法和装置
US10203155B2 (en) 2010-12-23 2019-02-12 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and device for condensing a first fluid rich in carbon dioxide using a second fluid
CN103797321A (zh) * 2011-03-16 2014-05-14 乔治洛德方法研究和开发液化空气有限公司 用于co2的液化的方法和设备
WO2012123690A3 (fr) * 2011-03-16 2015-08-13 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de liquefaction de co2
FR2972793A1 (fr) * 2011-03-16 2012-09-21 Air Liquide Procede et appareil de liquefaction d'un gaz riche en co2 contenant au moins une impurete legere
FR2972792A1 (fr) * 2011-03-16 2012-09-21 Air Liquide Procede et appareil de liquefaction de co2
CN103827614A (zh) * 2011-03-30 2014-05-28 阿尔斯通技术有限公司 使用致冷系统的低温co2分离
KR101583261B1 (ko) 2011-03-30 2016-01-08 알스톰 테크놀러지 리미티드 냉동 시스템을 사용하는 극저온 ｃｏ₂ 분리
AU2012235841B2 (en) * 2011-03-30 2015-10-01 General Electric Technology Gmbh Cryogenic CO2 separation using a refrigeration system
KR20140031241A (ko) * 2011-03-30 2014-03-12 알스톰 테크놀러지 리미티드 냉동 시스템을 사용하는 극저온 ｃｏ₂ 분리
FR2973864A1 (fr) * 2011-04-11 2012-10-12 Air Liquide Procede et appareil de liquefaction d'un gaz riche en co2
WO2012140350A3 (fr) * 2011-04-11 2015-01-22 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de liquefaction d'un gaz riche en co2
CN104136870A (zh) * 2011-04-11 2014-11-05 乔治洛德方法研究和开发液化空气有限公司 用于使富co2气体液化的方法和设备
EP2574392A1 (de) * 2011-09-29 2013-04-03 General Electric Company Anlage und Methode um flüssiges oder festes Kohlendioxid herzustellen und Energie rückzugewinnen.
US10519102B2 (en) * 2013-12-12 2019-12-31 Thyssenkrupp Ag Method for preparation of ammonia gas and CO2 for a urea synthesis process
US10170782B2 (en) * 2015-06-05 2019-01-01 Fuelcell Energy, Inc. High-efficiency fuel cell system with carbon dioxide capture assembly and method
US11949135B2 (en) 2016-04-21 2024-04-02 Fuelcell Energy, Inc. Molten carbonate fuel cell anode exhaust post-processing for carbon dioxide capture
US11211625B2 (en) 2016-04-21 2021-12-28 Fuelcell Energy, Inc. Molten carbonate fuel cell anode exhaust post-processing for carbon dioxide
US11508981B2 (en) 2016-04-29 2022-11-22 Fuelcell Energy, Inc. Methanation of anode exhaust gas to enhance carbon dioxide capture
FR3083854A1 (fr) * 2018-07-11 2020-01-17 Engie Dispositif et procede de liquefaction d'un flux de dioxyde de carbone
WO2020012129A1 (fr) * 2018-07-11 2020-01-16 Engie Dispositif et procédé de liquéfaction d'un flux de dioxyde de carbone
US12374703B2 (en) 2018-11-30 2025-07-29 ExxonMobil Technology and Engineering Company Flow field baffle for molten carbonate fuel cell cathode
US12355085B2 (en) 2018-11-30 2025-07-08 ExxonMobil Technology and Engineering Company Cathode collector structures for molten carbonate fuel cell
US12095129B2 (en) 2018-11-30 2024-09-17 ExxonMobil Technology and Engineering Company Reforming catalyst pattern for fuel cell operated with enhanced CO2 utilization
US11149905B2 (en) 2019-10-03 2021-10-19 Saudi Arabian Oil Company Mobile natural gas storage and transportation unit based on adsorption
US12347910B2 (en) 2019-11-26 2025-07-01 ExxonMobil Technology and Engineering Company Fuel cell power plant with a racked fuel cell module
US12334607B2 (en) 2019-11-26 2025-06-17 ExxonMobil Technology and Engineering Company Fuel cell assembly with external manifold for parallel flow
US11975969B2 (en) 2020-03-11 2024-05-07 Fuelcell Energy, Inc. Steam methane reforming unit for carbon capture
CN116761664A (zh) * 2021-01-29 2023-09-15 日立造船爱诺瓦公司 从含甲烷的气体中去除co2的方法
WO2025172226A1 (fr) * 2024-02-16 2025-08-21 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de capture de co2 avec séparation par condensation partielle et/ou distillation et/ou solidification
FR3159432A1 (fr) * 2024-02-16 2025-08-22 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de capture de CO2 avec séparation par condensation partielle et/ou distillation et/ou solidification

Also Published As

Publication number Publication date
WO2006106253A2 (fr) 2006-10-12
WO2006106253A3 (fr) 2006-12-14
EP1869385B1 (de) 2009-09-02
EP1869385A2 (de) 2007-12-26
PL1869385T3 (pl) 2010-01-29
EP2056051A1 (de) 2009-05-06
ATE441822T1 (de) 2009-09-15
FR2884305A1 (fr) 2006-10-13
DE602006008912D1 (de) 2009-10-15

Similar Documents

Publication Publication Date Title
US20080245101A1 (en) Integrated Method and Installation for Cryogenic Adsorption and Separation for Producing Co2
CN104428614B (zh) 用于分离含有二氧化碳、水和至少一种轻质杂质的流的包括低温下的分离步骤的设备和方法
EP2167891B1 (de) Vorrichtung und verfahren zur trennung einer gasförmigen mischung
CN102497917B (zh) 用于生产至少一种具有低co2含量的气体和至少一种具有高co2含量的流体的方法
US7927573B2 (en) Multi-stage process for purifying carbon dioxide and producing acid
CN115069057B (zh) 一种低温精馏提纯回收二氧化碳的方法
CA2922891C (en) Hybrid membrane and adsorption-based system and process for recovering co2 from flue gas and using combustion air for adsorbent regeneration
US20090013868A1 (en) Process and apparatus for the separation of a gaseous mixture
CA2922887C (en) Hybrid membrane and adsorption-based system and process for recovering co2 from flue gas and using combustion air for adsorbent regeneration
CN101460801A (zh) 二氧化碳纯化方法
CN114206472A (zh) 采用热优化的热闪蒸溶剂再生的通过吸附处理气体的方法
FR2872890A1 (fr) Procede integre d'adsorption et de separation cryogenique pour la production de co2 et installation pour la mise en oeuvre du procede
US9206795B2 (en) Process and apparatus for drying and compressing a CO2-rich stream
CN204325448U (zh) 用于处理非铁矿石的装置
CN114459236A (zh) 一种大幅节能的水泥窑烟气碳捕集方法
FR2884304A1 (fr) Procede integre d'absorption et de separation cryogenique pour la production de co2 et installation pour la mise en oeuvre du procede
KR20260012712A (ko) 부분 응축 및/또는 증류를 통해 co2를 분리하기 위한 방법 및 장치
JP2026040347A (ja) 煙道ガスを利用して低コストで高純度液体窒素及び高純度液体二酸化炭素を同時に生産するためのシステム及び方法
CN121060226A (zh) 基于膜分离与多级吸附的石灰窑尾气二氧化碳回收提纯系统及方法
CN120720815A (zh) 利用污氮气高效提纯制取高纯氮气工艺

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:DUBETTIER-GRENIER, RICHARD;GUERET, VINCENT;LOCKWOOD, FREDERICK;REEL/FRAME:020823/0886

Effective date: 20071004

STCB Information on status: application discontinuation

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