EP4453489A2 - Method for large hydrogen liquefaction system - Google Patents

Method for large hydrogen liquefaction system

Info

Publication number
EP4453489A2
EP4453489A2 EP22854223.9A EP22854223A EP4453489A2 EP 4453489 A2 EP4453489 A2 EP 4453489A2 EP 22854223 A EP22854223 A EP 22854223A EP 4453489 A2 EP4453489 A2 EP 4453489A2
Authority
EP
European Patent Office
Prior art keywords
liquefaction
precooling
hydrogen
cold
refrigerant
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP22854223.9A
Other languages
German (de)
French (fr)
Inventor
Michael A. Turney
Patrick Le Bot
Alain Guillard
Bobby Mon-Flan CHAN
Francois Fuentes
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.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP4453489A2 publication Critical patent/EP4453489A2/en
Pending legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J1/0005—Light or noble gases
    • F25J1/001—Hydrogen
    • 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"
    • F25J1/0035—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 gas expansion with extraction of work
    • F25J1/0037—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 gas expansion with extraction of work of a return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/005—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by expansion of a gaseous refrigerant stream with extraction of work
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/0062—Light or noble gases, mixtures thereof
    • F25J1/0067—Hydrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/007—Primary atmospheric gases, mixtures thereof
    • F25J1/0072—Nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—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
    • F25J1/0205—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 as a dual level SCR refrigeration cascade
    • 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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F25J1/0249—Controlling refrigerant inventory, i.e. composition or quantity
    • F25J1/025—Details related to the refrigerant production or treatment, e.g. make-up supply from feed gas itself
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0259—Modularity and arrangement of parts of the liquefaction unit and in particular of the cold box, e.g. pre-fabrication, assembling and erection, dimensions, horizontal layout "plot"
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0269—Arrangement of liquefaction units or equipments fulfilling the same process step, e.g. multiple "trains" concept
    • F25J1/027—Inter-connecting multiple hot equipments upstream of the cold box
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0269—Arrangement of liquefaction units or equipments fulfilling the same process step, e.g. multiple "trains" concept
    • F25J1/0271—Inter-connecting multiple cold equipments within or downstream of the cold box
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0269—Arrangement of liquefaction units or equipments fulfilling the same process step, e.g. multiple "trains" concept
    • F25J1/0271—Inter-connecting multiple cold equipments within or downstream of the cold box
    • F25J1/0272—Multiple identical heat exchangers in parallel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
    • F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
    • 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
    • F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
    • 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

Definitions

  • the present invention generally relates to a method and apparatus for producing liquid hydrogen, particularly in large quantities.
  • Hydrogen is a key molecule as a sustainable energy carrier. Liquefaction of hydrogen is key for its transportation and distribution to local markets.
  • Cold end refrigeration (20K to 80K) is achieved by turbo-expansion and/or isenthalpic expansion and/or vaporization of light gases such as H2, He, Ne, etc....
  • the primary refrigeration is from turbo-expansion due to its high efficiency; however, this equipment is limited in capacity due to the technology of expansion of low molecular weight gases. This is typically partially offset by use of multiple expanders in series or parallel (e.g., 2x50%, 3x33%, etc... ).
  • the limiting capacity constraint of the low molecular weight turbine is on the order to 10 to 30 times less than the limiting capacity constraint of other major process equipment.
  • a typical hydrogen liquefaction process may include a precooling section consisting of dual N2 expanders (1 warm and 1 cold N2 expanders) and cooling/liquefaction section consisting of H2 or He expanders.
  • a precooling section consisting of dual N2 expanders (1 warm and 1 cold N2 expanders)
  • cooling/liquefaction section consisting of H2 or He expanders.
  • a hydrogen liquefaction apparatus comprising a precooling zone and a cooling/liquefaction zone.
  • the precooling zone which comprises a plurality a precooling units, cools a H2 feed stream to a first intermediate temperature followed by cooling/liquefaction in the cooling/liquefaction zone.
  • the cooling/liquefaction zone comprises N units such that each unit receives at least a portion of the hydrogen stream, which is split from the precooling zone, wherein the number of Precooling units is less than N.
  • the intermediate temperature is in the range of 70K to 300K, and preferably in the range of 70K to 100K.
  • the precooling zone cools the H2 stream with a refrigerant comprising one or more of ammonia, mixed hydrocarbons, nitrogen or other know refrigerant.
  • the cooling/liquefaction zone cools the H2 steam with a refrigerant comprising one or more of hydrogen, helium, neon.
  • the number of units of the warm section is less than number of units of the colder section.
  • At least a portion of the low-pressure refrigerant stream(s) received from the cooling/liquefaction units is sent to a refrigerant precooling unit. At least a portion of the HP refrigerant stream is cooled against lower pressure return refrigerant stream(s).
  • a hydrogen liquefaction apparatus can include: a precooling cold box having a heat exchanger disposed therein, wherein the heat exchanger is configured to cool down a feed stream within the precooling cold box by indirect heat exchange between the feed stream and a precooling refrigerant; a plurality of liquefaction cold boxes in fluid communication with the precooling cold box, wherein each liquefaction cold box comprises its own heat exchanger, wherein each heat exchanger within the plurality of liquefaction cold boxes is configured to liquefy the feed stream by indirect heat exchange with a liquefaction refrigerant; a precooling refrigeration system configured to provide refrigeration to the precooling zone; and a liquefaction refrigeration system configured to provide the liquefaction refrigerant to the plurality of liquefaction cold boxes, wherein there are M total precooling cold boxes and N total liquefaction cold boxes, wherein M is less than N.
  • the liquefaction refrigeration system comprises a recycle compression system and an expansion system, wherein the recycle compression system is configured to compress the liquefaction refrigerant and the expansion system is configured to expand the liquefaction refrigerant;
  • the recycle compression system comprises one or more recycle compressors
  • liquefaction expansion system comprises one or more liquefaction expanders, wherein the one or more liquefaction expanders are arranged in parallel and/or series;
  • the liquefaction refrigerant is selected from the group consisting of hydrogen, neon, helium, and combinations thereof;
  • the liquefaction refrigerant comprises one or more of hydrogen, neon, and helium
  • the precooling system comprises a precooling refrigeration cycle
  • the precooling refrigerant is selected from the group consisting of nitrogen, argon ammonia, carbon monoxide, carbon dioxide, water, hydrocarbon, mixed hydrocarbons, fluorocarbons, and combinations thereof;
  • the precooling refrigerant comprises one or more of nitrogen, argon ammonia, carbon monoxide, carbon dioxide, water, hydrocarbon, mixed hydrocarbons, and fluorocarbons;
  • the liquefaction refrigeration system comprises a single, common recycle compression system
  • the apparatus can further include an intermediate cold box in fluid communication with the precooling cold box and the plurality of liquefaction cold boxes, wherein the intermediate cold box is disposed between the precooling cold box and the plurality of liquefaction cold boxes; and/or • the ratio of N total liquefaction cold boxes to M total precooling cold boxes is between 1.25 and 3.0 (1.25 ⁇ N/M ⁇ 3.0).
  • a liquefaction apparatus can include: a first cooling cold box configured to receive a feed stream at an initial temperature To and cool the feed stream to form a cooled feed stream at a cooled temperature Ti; a first precooling withdrawal line configured to remove the cooled feed stream from the first cooling cold box; a means for splitting the cooled feed stream, wherein the means for splitting the cooled feed stream are in fluid communication with the precooling withdrawal line, a plurality of secondary cold boxes in fluid communication with the means for splitting the cooled feed stream, wherein the plurality of secondary cold boxes are configured to receive the cooled feed stream from the means for splitting the cooled feed stream and liquefy the cooled feed stream therein to form a liquefied stream at a liquefaction temperature TL, wherein there are M total first cooling cold boxes and N total secondary cold boxes, wherein M is less than N.
  • each secondary cold box comprises its own heat exchanger(s), wherein each heat exchanger within the plurality of secondary cold boxes is configured to liquefy the cooled feed stream by indirect heat exchange with a liquefaction refrigerant;
  • the apparatus can further include: a liquefaction refrigeration system, the liquefaction refrigeration system comprising a recycle compression system and an expansion system, wherein the recycle compression system is configured to compress a liquefaction refrigerant and the expansion system is configured to expand the liquefaction refrigerant;
  • the apparatus can further include: a means for combining the liquefaction refrigerant, wherein the means for combining the liquefaction refrigerant is configured to receive the liquefaction refrigerant from a warm end of each of the plurality of secondary cold boxes via a plurality of pipes and then send the liquefaction refrigerant, after being combined, to the first cooling cold box via a first return line;
  • the apparatus can further include: a second precooling withdrawal line configured to remove the liquefaction refrigeration stream from a cold end of the first cooling cold box; and/or
  • a method for the liquefaction of hydrogen can include the steps of: precooling a hydrogen feed stream in a precooling cold box having a heat exchanger disposed therein to form a cooled hydrogen stream, wherein the heat exchanger is configured to cool down the feed stream within the precooling cold box by indirect heat exchange between the hydrogen feed stream and a precooling refrigerant; withdrawing the cooled hydrogen stream from the precooling cold box; and introducing the cooled hydrogen stream to a plurality of liquefaction cold boxes, wherein the cooled hydrogen stream liquefies within the plurality of liquefaction cold boxes by indirect heat exchange against a liquefaction refrigerant to form a product hydrogen stream in each of the plurality of liquefaction cold boxes, wherein the product hydrogen stream is in liquid form or pseudo-liquid
  • the liquefaction refrigeration system comprises a recycle compression system and an expansion system, wherein the recycle compression system is configured to compress the liquefaction refrigerant and the expansion system is configured to expand the liquefaction refrigerant;
  • the recycle compression system comprises one or more recycle compressors
  • liquefaction expansion system comprises one or more liquefaction expanders, wherein the one or more liquefaction expanders are arranged in parallel or series;
  • the liquefaction refrigerant is selected from the group consisting of hydrogen, neon, helium, and combinations thereof;
  • the liquefaction refrigerant comprises one or more of hydrogen, neon, and helium
  • the precooling system comprises a precooling refrigeration cycle
  • the precooling refrigerant is selected from the group consisting of nitrogen, argon, ammonia, carbon monoxide, carbon dioxide, water, hydrocarbon, mixed hydrocarbons, fluorocarbon and combinations thereof;
  • the precooling refrigerant comprises one or more of nitrogen, argon, ammonia, carbon monoxide, carbon dioxide, water, hydrocarbon, mixed hydrocarbons, and fluorocarbons;
  • the cold end refrigeration cycle comprises a single, common recycle compression system
  • the method can also include an intermediate cold box in fluid communication with the precooling cold box and the plurality of liquefaction cold boxes, wherein the intermediate cold box is disposed between the precooling cold box and the plurality of liquefaction cold boxes;
  • the temperature at a cold end of the precooling cold box is in the range of 30K to 25 OK;
  • the temperature at a warm end of the liquefaction zone is in the range of 3 OK to 150K;
  • the liquefaction method can include the steps of: introducing a feed stream into a pre-cooling cold box at an initial temperature To and cooling the feed stream therein to form a cooled feed stream at a cooled temperature Ti; withdrawing the cooled feed stream from the pre-cooling box using a first precooling withdrawal line; splitting the cooled feed stream into a first cooled feed stream and a second cooled feed stream; providing a plurality of subcooling boxes, wherein the plurality of subcooling cold boxes comprise a first subcooling cold box and a second subcooling cold box; introducing the first cooled feed stream into the first subcooling cold box under conditions effective for subcooling the first cooled feed stream to form a first product stream at a product temperature TL, wherein the first product stream is in liquid form or a pseudo-liquid form; introducing the second cooled feed stream into a second subcooling cold box under conditions effective for subcooling the second cooled feed stream to form a second product stream, wherein the second
  • each secondary cold box comprises its own heat exchanger, wherein each heat exchanger within the plurality of secondary cold boxes is configured to liquefy the feed stream by indirect heat exchanger with a liquefaction refrigerant;
  • the liquefaction method can also include: a liquefaction refrigeration system, the liquefaction refrigeration system comprising a recycle compression system and an expansion system, wherein the recycle compression system is configured to compress a liquefaction refrigerant and the expansion system is configured to expand the liquefaction refrigerant;
  • the liquefaction method can also include: a means for combining the liquefaction refrigerant, wherein the means for combining the liquefaction refrigerant is configured to receive the liquefaction refrigerant from a warm end of each of the plurality of secondary cold boxes via a plurality of pipes and then send the liquefaction refrigerant, after being combined, to the first cooling cold box via a first return line;
  • the liquefaction method can also include: a second precooling withdrawal line configured to remove the liquefaction refrigeration stream from the first cooling cold box;
  • the liquefaction method can also include: a means for splitting the liquefaction refrigeration stream, wherein the means for splitting the liquefaction refrigeration stream are in fluid communication with the second precooling withdrawal line; and/or
  • FIG. 1 is a process flow diagram of an embodiment of the prior art.
  • FIG. 2 is an embodiment of the prior art.
  • FIG. 3 provides an embodiment of the present invention.
  • FIG. 4 provides another embodiment of the present invention.
  • FIG. 5 provides yet another embodiment of the present invention.
  • Certain embodiments of the invention allow for a reduction in capital expenditures by reducing the number of precooling zones in a hydrogen liquefaction apparatus having a plurality of cold end liquefaction zones.
  • the hydrogen liquefaction apparatus can have N cold-end liquefaction zones while also having less than N (e.g., N-l, N- 2, N-3, etc... ) precooling zones.
  • prior art hydrogen liquefaction units use two identical trains la, lb running separately from each other.
  • Each train includes a precooling zone 10 and a liquefaction zone 5.
  • the refrigeration for the precooling zone 10 is provided by a closed loop refrigeration circuit 11, which is provided by compression 2, 4, 6, and expansion 5, 7 of a precooling refrigerant Refrigeration for the liquefaction zone 5 is provided by a second closed loop refrigeration circuit 13.
  • FIG. 2 provides a flow chart of a hydrogen liquefaction unit having five trains, with each train having six main sections: hydrogen compression, nitrogen compression, precooling, cooling, liquefaction, and storage. All of these identical trains would be run independently from each other (i.e., the operating conditions of each train have little to no bearing on the operating conditions of another train).
  • FIG. 3, which represents an embodiment of the present invention, provides a process flow diagram showing how a hydrogen liquefaction unit, which has two liquefaction zones 20, 25, can have a single precooling zone 10.
  • Refrigeration for the precooling zone 10 is provided by compression 2, 4, 6, and expansion 5, 7 of a precooling refrigerant that is configured to cool the hydrogen feed to a first intermediate temperature in the range of 70K to 300K, more preferably 70Kto 100K.
  • the precooling refrigerant can be ammonia, mixed hydrocarbons, nitrogen, or any other known refrigerant.
  • the hydrogen feed gas is split 17,19 and sent to two separate liquefaction zones 20, 25, wherein the hydrogen is condensed 23a, 23b and following removal of any non-condensed gases in gas liquid separator 39, the liquid hydrogen is ultimately sent to a hydrogen liquid storage tank 40.
  • the hydrogen can exit the heat exchanger in pseudo-liquid form.
  • pseudo-liquid form may include a supercritical fluid that is any substance at a temperature and pressure above its critical point, where distinct liquid and gas phases do not exist.
  • boil-off gas 42, 43 that is withdrawn from hydrogen liquid storage tank 40 can be rewarmed in one or both liquefaction zones before being combined and rewarmed more in the precooling zone 10.
  • the warmed boil-off gas can then be compressed 50 to become recycled boil-off gas 52, which can be fed into the hydrogen feed, and/or optionally, can provide make-up gas to the hydrogen recycle (not shown).
  • the cold end refrigerant 22, which was also cooled in the precooling zone 10, is withdrawn from the precooling zone 10 and then split into two streams 12, 14, wherein the cold end refrigerant is expanded in a set of turbines (15a, 15b), which preferably have different incoming temperatures, to provide cooling energy for the two liquefaction zones. After providing this cooling energy, the cold end refrigerant is withdrawn from a warm end of the liquefaction zone 20, 25, and further warmed in the precooling zone 10. After fully warming, the cold end refrigerant is then compressed 24 again as part of its refrigeration cycle.
  • each of the expansion turbines of the set of turbines (15a, 15b) can be two or more turbines in parallel.
  • the cold end refrigerant is not used to provide any precooling energy (e.g., the cold end refrigerant does not reenter the precooling zone 10 for rewarming, but instead enters a separate heat exchanger 30 to provide cooling to one portion of the cold end refrigerant). Rather, all of the precooling of the hydrogen feed stream is done by the precooling refrigerant in the closed loop refrigeration circuit 11. In this way, there is a set of simple standardized modular precooling exchanger(s) and cold box(s) and a separate set of complex custom exchangers and cold box(s). The custom complex set may also comprise most of the project specific complexities such as H2 Feed, purification, and precooling refrigeration cycle.
  • the refrigeration balance between the set of simple exchangers and the set of complex exchangers is made by adjusting the flow split of HP refrigerant between the simple and complex cores (as shown in figure) and/or by splitting one of the lower pressure refrigerant return streams between the simple and complex cores.
  • the number of simple exchangers/ cold boxes is independent of the number of complex exchangers/ cold boxes.
  • the hydrogen feed stream is again split into two 17, 19 and then further cooled and liquefied in multiple (in this embodiment two) liquefaction zones 20, 25.
  • the cold end refrigerant is split into two streams 31, 33, with one stream 31 being first cooled in the precooling zone 10 and the second stream 33 being cooled in a second heat exchanger 30.
  • This second heat exchanger does not include any cooling of the hydrogen feed stream, which thereby allows for greater flexibility of cooling temperatures in this second heat exchanger.
  • the cold end refrigerant 33 in this section could be cooled to a lower temperature than the cold end refrigerant 31 in the precooling zone.
  • the cold end temperature of the second heat exchanger can differ from the cold end temperature of the precooling zone.
  • the two cold end refrigerant streams can be mixed together before being split into two and sent to the two separate liquefaction zones.
  • the two streams used for liquefaction the hydrogen in the liquefaction zone should have substantially similar temperatures, thereby allowing identical trains to be used, which greatly reduces engineering design and fabrication costs, thereby reducing complexity. Therefore, the embodiment shown in FIG. 4 provides an advantage of being able to alter the temperature of the cold end refrigerant prior to introducing it to the hydrogen liquefaction unit without that temperature being directly tied to the hydrogen feed gas that is to be liquefied, and can provide the option for a modular (standardized package) for a portion of the precooling refrigeration system.
  • FIG. 4 does not show the boil-off gas recycle
  • those of ordinary skill in the art will recognize that the boil-off gas recycle shown in FIG. 3 can also be used with the embodiment shown in FIG. 4. Therefore, the lack of this element in FIG. 4 should not be interpreted to be limiting.
  • FIG. 5 provides a process flow chart in accordance with an embodiment of the present invention.
  • “Comprising” in a claim is an open transitional term which means the subsequently identified claim elements are a nonexclusive listing (i.e., anything else may be additionally included and remain within the scope of “comprising”). “Comprising” as used herein may be replaced by the more limited transitional terms “consisting essentially of and “consisting of’ unless otherwise indicated herein.
  • Providing in a claim is defined to mean furnishing, supplying, making available, or preparing something. The step may be performed by any actor in the absence of express language in the claim to the contrary a range is expressed, it is to be understood that another embodiment is from the one.
  • Optional or optionally means that the subsequently described event or circumstances may or may not occur.
  • the description includes instances where the event or circumstance occurs and instances where it does not occur.
  • Ranges may be expressed herein as from about one particular value, and/or to about another particular value. When such particular value and/or to the other particular value, along with all combinations within said range.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

A method and apparatus for the liquefaction of hydrogen is provided. The can include the steps of: precooling a hydrogen feed stream in a precooling cold box having a heat exchanger disposed therein to form a cooled hydrogen stream, wherein the heat exchanger is configured to cool down the feed stream within the precooling cold box by indirect heat exchange between the hydrogen feed stream and a precooling refrigerant; and withdrawing the cooled hydrogen stream from the precooling cold box; introducing the cooled hydrogen stream to a plurality of liquefaction cold boxes, wherein the cooled hydrogen stream liquefies within the plurality of liquefaction cold boxes by indirect heat exchange against a liquefaction refrigerant to form a product hydrogen stream in each of the plurality of liquefaction cold boxes, wherein the product hydrogen stream is in liquid form or pseudo-liquid form wherein there are M total precooling cold boxes and N total liquefaction cold boxes, wherein M is less than N.

Description

METHOD FOR LARGE HYDROGEN LIQUEFACTION SYSTM
CROSS REFERENCE OF RELATED APPLICATIONS
[0001] This application claims priority to U.S. Provisional Application Ser. No. 63,293,080 filed on December 22, 2021, which is hereby incorporated by reference in its entirety.
TECHNICAL FIELD
[0002] The present invention generally relates to a method and apparatus for producing liquid hydrogen, particularly in large quantities.
BACKGROUND OF THE INVENTION
[0003] Hydrogen is a key molecule as a sustainable energy carrier. Liquefaction of hydrogen is key for its transportation and distribution to local markets.
[0004] Hydrogen liquefaction processes require refrigeration over a very wide temperature range (20K to 300K). It is common to have separate dedicated refrigeration systems for the warm end (80K to 300K) and the cold end (20K to 80K) since the specific refrigeration demands and cost vary significantly with temperature. Regarding the warm temperature range (80K to 300K): referenced art exists using a) closed loop N2 cycle, b) vaporization of LIN from an ASU, c) mixed hydrocarbon refrigerant, and d) optionally pre-precooling to a first temperature (25 OK to 300K) using NHs and/or water. Regarding the cold temperature range (20K to 80K): referenced art exists using closed loop H2 cycle, He cycle, and/or Ne/He cycles.
[0005] It is known in the art that the largest equipment within the cold boxes are the heat exchangers (typically brazed aluminum). As shown in Table I, the required heat exchanger surface area (which is directly related to UA i.e., heat transfer coefficient x area) significantly decreases at colder temperatures. As a result, typical good engineering practice would be to design multiple modules split by temperature level (and different insulation types) and for each level of temperature to design multiple parallel trains according to heat exchange surface areas. Therefore, normal engineering work will consist of M precooling cold boxes and N liquefaction cold boxes with M >N. In the Table below, MR is mixed refrigerant, N2 is nitrogen, He is helium, Ne is neon, and H2 is hydrogen. Table I: Heat Exchanger Surface Area as a Function of Refrigerant Type
[0006] Cold end refrigeration (20K to 80K) is achieved by turbo-expansion and/or isenthalpic expansion and/or vaporization of light gases such as H2, He, Ne, etc.... The primary refrigeration is from turbo-expansion due to its high efficiency; however, this equipment is limited in capacity due to the technology of expansion of low molecular weight gases. This is typically partially offset by use of multiple expanders in series or parallel (e.g., 2x50%, 3x33%, etc... ). However, in the case of hydrogen liquefaction equipment, the limiting capacity constraint of the low molecular weight turbine is on the order to 10 to 30 times less than the limiting capacity constraint of other major process equipment.
[0007] A typical hydrogen liquefaction process may include a precooling section consisting of dual N2 expanders (1 warm and 1 cold N2 expanders) and cooling/liquefaction section consisting of H2 or He expanders. In this example, if one designs the LH2 liquefaction capacity for maximum utilization of the single warm and cold N2 turbine frames, then the resulting number of H2 or He turbine units is in the order of 10.
[0008] Therefore, there is a need for a process and apparatus for an arrangement, which allows for utilization of the larger capacities possible of other equipment.
BRIEF SUMMARY OF THE INVENTION
[0009] The present invention is directed to a device and a method and apparatus that satisfies at least one of these needs. [0010] A hydrogen liquefaction apparatus comprising a precooling zone and a cooling/liquefaction zone. The precooling zone, which comprises a plurality a precooling units, cools a H2 feed stream to a first intermediate temperature followed by cooling/liquefaction in the cooling/liquefaction zone. The cooling/liquefaction zone comprises N units such that each unit receives at least a portion of the hydrogen stream, which is split from the precooling zone, wherein the number of Precooling units is less than N. This is surprising and contrary to the conventional wisdom as discussed, supra, and shown in Table I.
[0011] In a first embodiment, the intermediate temperature is in the range of 70K to 300K, and preferably in the range of 70K to 100K. In one embodiment, the precooling zone cools the H2 stream with a refrigerant comprising one or more of ammonia, mixed hydrocarbons, nitrogen or other know refrigerant.
[0012] In another embodiment, the cooling/liquefaction zone cools the H2 steam with a refrigerant comprising one or more of hydrogen, helium, neon.
[0013] In another embodiment, there is an intermediate cooling zone where the hydrogen stream is cooled to a second intermediate temperature. Where the number of units of the warm section is less than number of units of the colder section. In optional embodiments, it is possible to include multiple levels of cooling, e.g., (1) water, (2) NH3 refrigerant, (3) mixed hydrocarbon refrigerant, (4) N2 refrigerant, and (5) H2 and/or He refrigerant.
[0014] In another embodiment, at least a portion of the low-pressure refrigerant stream(s) received from the cooling/liquefaction units is sent to a refrigerant precooling unit. At least a portion of the HP refrigerant stream is cooled against lower pressure return refrigerant stream(s).
[0015] In one embodiment, a hydrogen liquefaction apparatus can include: a precooling cold box having a heat exchanger disposed therein, wherein the heat exchanger is configured to cool down a feed stream within the precooling cold box by indirect heat exchange between the feed stream and a precooling refrigerant; a plurality of liquefaction cold boxes in fluid communication with the precooling cold box, wherein each liquefaction cold box comprises its own heat exchanger, wherein each heat exchanger within the plurality of liquefaction cold boxes is configured to liquefy the feed stream by indirect heat exchange with a liquefaction refrigerant; a precooling refrigeration system configured to provide refrigeration to the precooling zone; and a liquefaction refrigeration system configured to provide the liquefaction refrigerant to the plurality of liquefaction cold boxes, wherein there are M total precooling cold boxes and N total liquefaction cold boxes, wherein M is less than N.
[0016] In optional embodiments of the apparatus:
• the liquefaction refrigeration system comprises a recycle compression system and an expansion system, wherein the recycle compression system is configured to compress the liquefaction refrigerant and the expansion system is configured to expand the liquefaction refrigerant;
• there are M total recycle compression systems and/or N total liquefaction expansion systems;
• the recycle compression system comprises one or more recycle compressors;
• the one or more recycle compressors are arranged in parallel and/or series;
• liquefaction expansion system comprises one or more liquefaction expanders, wherein the one or more liquefaction expanders are arranged in parallel and/or series;
• the liquefaction refrigerant is selected from the group consisting of hydrogen, neon, helium, and combinations thereof;
• the liquefaction refrigerant comprises one or more of hydrogen, neon, and helium;
• the precooling system comprises a precooling refrigeration cycle;
• the precooling refrigerant is selected from the group consisting of nitrogen, argon ammonia, carbon monoxide, carbon dioxide, water, hydrocarbon, mixed hydrocarbons, fluorocarbons, and combinations thereof;
• the precooling refrigerant comprises one or more of nitrogen, argon ammonia, carbon monoxide, carbon dioxide, water, hydrocarbon, mixed hydrocarbons, and fluorocarbons;
• the liquefaction refrigeration system comprises a single, common recycle compression system;
• the apparatus can further include an intermediate cold box in fluid communication with the precooling cold box and the plurality of liquefaction cold boxes, wherein the intermediate cold box is disposed between the precooling cold box and the plurality of liquefaction cold boxes; and/or • the ratio of N total liquefaction cold boxes to M total precooling cold boxes is between 1.25 and 3.0 (1.25 < N/M < 3.0).
[0017] In another embodiment, a liquefaction apparatus can include: a first cooling cold box configured to receive a feed stream at an initial temperature To and cool the feed stream to form a cooled feed stream at a cooled temperature Ti; a first precooling withdrawal line configured to remove the cooled feed stream from the first cooling cold box; a means for splitting the cooled feed stream, wherein the means for splitting the cooled feed stream are in fluid communication with the precooling withdrawal line, a plurality of secondary cold boxes in fluid communication with the means for splitting the cooled feed stream, wherein the plurality of secondary cold boxes are configured to receive the cooled feed stream from the means for splitting the cooled feed stream and liquefy the cooled feed stream therein to form a liquefied stream at a liquefaction temperature TL, wherein there are M total first cooling cold boxes and N total secondary cold boxes, wherein M is less than N.
[0018] In optional embodiments of the apparatus:
• each secondary cold box comprises its own heat exchanger(s), wherein each heat exchanger within the plurality of secondary cold boxes is configured to liquefy the cooled feed stream by indirect heat exchange with a liquefaction refrigerant;
• the apparatus can further include: a liquefaction refrigeration system, the liquefaction refrigeration system comprising a recycle compression system and an expansion system, wherein the recycle compression system is configured to compress a liquefaction refrigerant and the expansion system is configured to expand the liquefaction refrigerant;
• the apparatus can further include: a means for combining the liquefaction refrigerant, wherein the means for combining the liquefaction refrigerant is configured to receive the liquefaction refrigerant from a warm end of each of the plurality of secondary cold boxes via a plurality of pipes and then send the liquefaction refrigerant, after being combined, to the first cooling cold box via a first return line;
• the apparatus can further include: a second precooling withdrawal line configured to remove the liquefaction refrigeration stream from a cold end of the first cooling cold box; and/or
• the apparatus can further include a means for splitting the liquefaction refrigeration stream, wherein the means for splitting the liquefaction refrigeration stream are in fluid communication with the second precooling withdrawal line. [0019] In yet another embodiment, a method for the liquefaction of hydrogen can include the steps of: precooling a hydrogen feed stream in a precooling cold box having a heat exchanger disposed therein to form a cooled hydrogen stream, wherein the heat exchanger is configured to cool down the feed stream within the precooling cold box by indirect heat exchange between the hydrogen feed stream and a precooling refrigerant; withdrawing the cooled hydrogen stream from the precooling cold box; and introducing the cooled hydrogen stream to a plurality of liquefaction cold boxes, wherein the cooled hydrogen stream liquefies within the plurality of liquefaction cold boxes by indirect heat exchange against a liquefaction refrigerant to form a product hydrogen stream in each of the plurality of liquefaction cold boxes, wherein the product hydrogen stream is in liquid form or pseudo-liquid form, wherein there are M total precooling cold boxes and N total liquefaction cold boxes, wherein M is less than N.
[0020] In optional embodiments of the method:
• the liquefaction refrigeration system comprises a recycle compression system and an expansion system, wherein the recycle compression system is configured to compress the liquefaction refrigerant and the expansion system is configured to expand the liquefaction refrigerant;
• there are M total recycle compression systems and N total liquefaction expansion systems;
• the recycle compression system comprises one or more recycle compressors;
• the one or more recycle compressors are arranged in parallel or series;
• liquefaction expansion system comprises one or more liquefaction expanders, wherein the one or more liquefaction expanders are arranged in parallel or series;
• the liquefaction refrigerant is selected from the group consisting of hydrogen, neon, helium, and combinations thereof;
• the liquefaction refrigerant comprises one or more of hydrogen, neon, and helium;
• the precooling system comprises a precooling refrigeration cycle;
• the precooling refrigerant is selected from the group consisting of nitrogen, argon, ammonia, carbon monoxide, carbon dioxide, water, hydrocarbon, mixed hydrocarbons, fluorocarbon and combinations thereof;
• the precooling refrigerant comprises one or more of nitrogen, argon, ammonia, carbon monoxide, carbon dioxide, water, hydrocarbon, mixed hydrocarbons, and fluorocarbons;
• the cold end refrigeration cycle comprises a single, common recycle compression system;
• the method can also include an intermediate cold box in fluid communication with the precooling cold box and the plurality of liquefaction cold boxes, wherein the intermediate cold box is disposed between the precooling cold box and the plurality of liquefaction cold boxes;
• the temperature at a cold end of the precooling cold box is in the range of 30K to 25 OK;
• the temperature at a warm end of the liquefaction zone is in the range of 3 OK to 150K; and/or
• the ratio of N total liquefaction cold boxes to M total precooling cold boxes is between 1.25 and 3.0 (1.25 < N/M < 3.0).
[0021] In another embodiment, the liquefaction method can include the steps of: introducing a feed stream into a pre-cooling cold box at an initial temperature To and cooling the feed stream therein to form a cooled feed stream at a cooled temperature Ti; withdrawing the cooled feed stream from the pre-cooling box using a first precooling withdrawal line; splitting the cooled feed stream into a first cooled feed stream and a second cooled feed stream; providing a plurality of subcooling boxes, wherein the plurality of subcooling cold boxes comprise a first subcooling cold box and a second subcooling cold box; introducing the first cooled feed stream into the first subcooling cold box under conditions effective for subcooling the first cooled feed stream to form a first product stream at a product temperature TL, wherein the first product stream is in liquid form or a pseudo-liquid form; introducing the second cooled feed stream into a second subcooling cold box under conditions effective for subcooling the second cooled feed stream to form a second product stream, wherein the second product stream is in liquid form or pseudo-liquid form; withdrawing the first and second product streams from the first and second subcooling cold boxes; and combining the first and second product streams into a final product stream.
[0022] In optional embodiments of the liquefaction method:
• each secondary cold box comprises its own heat exchanger, wherein each heat exchanger within the plurality of secondary cold boxes is configured to liquefy the feed stream by indirect heat exchanger with a liquefaction refrigerant; • the liquefaction method can also include: a liquefaction refrigeration system, the liquefaction refrigeration system comprising a recycle compression system and an expansion system, wherein the recycle compression system is configured to compress a liquefaction refrigerant and the expansion system is configured to expand the liquefaction refrigerant;
• the liquefaction method can also include: a means for combining the liquefaction refrigerant, wherein the means for combining the liquefaction refrigerant is configured to receive the liquefaction refrigerant from a warm end of each of the plurality of secondary cold boxes via a plurality of pipes and then send the liquefaction refrigerant, after being combined, to the first cooling cold box via a first return line;
• the liquefaction method can also include: a second precooling withdrawal line configured to remove the liquefaction refrigeration stream from the first cooling cold box;
• the liquefaction method can also include: a means for splitting the liquefaction refrigeration stream, wherein the means for splitting the liquefaction refrigeration stream are in fluid communication with the second precooling withdrawal line; and/or
• the feed stream consists essentially of hydrogen.
[0023] The foregoing has outlined rather broadly the features and technical advantages of the present invention in order that the detailed description of the invention that follows may be better understood. Additional features and advantages of the invention will be described hereinafter which form the subject of the claims of the invention. It should be appreciated by those skilled in the art that the conception and specific embodiment disclosed may be readily utilized as a basis for modifying or designing other structures for carrying out the same purposes of the present invention.
[0024] It should also be realized by those skilled in the art that such equivalent constructions do not depart from the spirit and scope of the invention as set forth in the appended claims. The novel features which are believed to be characteristic of the invention, both as to its organization and method of operation, together with further objects and advantages will be better understood from the following description when considered in connection with the accompanying figures. It is to be expressly understood, however, that the figures are provided for the purpose of illustration and description only and are not intended as a definition of the limits of the present invention. BRIEF DESCRIPTION OF THE DRAWINGS
[0025] For a more complete understanding of the present invention, reference is now made to the following descriptions taken in conjunction with the accompanying drawings, in which:
[0026] FIG. 1 is a process flow diagram of an embodiment of the prior art.
[0027] FIG. 2 is an embodiment of the prior art.
[0028] FIG. 3 provides an embodiment of the present invention.
[0029] FIG. 4 provides another embodiment of the present invention.
[0030] FIG. 5 provides yet another embodiment of the present invention.
DETAILED DESCRIPTION OF THE INVENTION
[0031] Certain embodiments of the invention allow for a reduction in capital expenditures by reducing the number of precooling zones in a hydrogen liquefaction apparatus having a plurality of cold end liquefaction zones. In certain embodiments, the hydrogen liquefaction apparatus can have N cold-end liquefaction zones while also having less than N (e.g., N-l, N- 2, N-3, etc... ) precooling zones.
[0032] As shown in FIG. 1, prior art hydrogen liquefaction units use two identical trains la, lb running separately from each other. Each train includes a precooling zone 10 and a liquefaction zone 5. In the case of FIG. 1, the refrigeration for the precooling zone 10 is provided by a closed loop refrigeration circuit 11, which is provided by compression 2, 4, 6, and expansion 5, 7 of a precooling refrigerant Refrigeration for the liquefaction zone 5 is provided by a second closed loop refrigeration circuit 13.
[0033] FIG. 2 provides a flow chart of a hydrogen liquefaction unit having five trains, with each train having six main sections: hydrogen compression, nitrogen compression, precooling, cooling, liquefaction, and storage. All of these identical trains would be run independently from each other (i.e., the operating conditions of each train have little to no bearing on the operating conditions of another train). [0034] FIG. 3, which represents an embodiment of the present invention, provides a process flow diagram showing how a hydrogen liquefaction unit, which has two liquefaction zones 20, 25, can have a single precooling zone 10. Refrigeration for the precooling zone 10 is provided by compression 2, 4, 6, and expansion 5, 7 of a precooling refrigerant that is configured to cool the hydrogen feed to a first intermediate temperature in the range of 70K to 300K, more preferably 70Kto 100K.
[0035] In one embodiment, the precooling refrigerant can be ammonia, mixed hydrocarbons, nitrogen, or any other known refrigerant.
[0036] Following the precooling zone, the hydrogen feed gas is split 17,19 and sent to two separate liquefaction zones 20, 25, wherein the hydrogen is condensed 23a, 23b and following removal of any non-condensed gases in gas liquid separator 39, the liquid hydrogen is ultimately sent to a hydrogen liquid storage tank 40. In certain embodiments, the hydrogen can exit the heat exchanger in pseudo-liquid form. As used herein, pseudo-liquid form may include a supercritical fluid that is any substance at a temperature and pressure above its critical point, where distinct liquid and gas phases do not exist.
[0037] In another optional embodiment, boil-off gas 42, 43 that is withdrawn from hydrogen liquid storage tank 40 can be rewarmed in one or both liquefaction zones before being combined and rewarmed more in the precooling zone 10. The warmed boil-off gas can then be compressed 50 to become recycled boil-off gas 52, which can be fed into the hydrogen feed, and/or optionally, can provide make-up gas to the hydrogen recycle (not shown).
[0038] The cold end refrigerant 22, which was also cooled in the precooling zone 10, is withdrawn from the precooling zone 10 and then split into two streams 12, 14, wherein the cold end refrigerant is expanded in a set of turbines (15a, 15b), which preferably have different incoming temperatures, to provide cooling energy for the two liquefaction zones. After providing this cooling energy, the cold end refrigerant is withdrawn from a warm end of the liquefaction zone 20, 25, and further warmed in the precooling zone 10. After fully warming, the cold end refrigerant is then compressed 24 again as part of its refrigeration cycle. As an optional embodiment, each of the expansion turbines of the set of turbines (15a, 15b) can be two or more turbines in parallel. [0039] FIG. 4 provides an alternate embodiment in which there is again a single precooling zone 10 for the hydrogen feed stream. In this embodiment, however, the cold end refrigerant is not used to provide any precooling energy (e.g., the cold end refrigerant does not reenter the precooling zone 10 for rewarming, but instead enters a separate heat exchanger 30 to provide cooling to one portion of the cold end refrigerant). Rather, all of the precooling of the hydrogen feed stream is done by the precooling refrigerant in the closed loop refrigeration circuit 11. In this way, there is a set of simple standardized modular precooling exchanger(s) and cold box(s) and a separate set of complex custom exchangers and cold box(s). The custom complex set may also comprise most of the project specific complexities such as H2 Feed, purification, and precooling refrigeration cycle.
[0040] The refrigeration balance between the set of simple exchangers and the set of complex exchangers is made by adjusting the flow split of HP refrigerant between the simple and complex cores (as shown in figure) and/or by splitting one of the lower pressure refrigerant return streams between the simple and complex cores. The number of simple exchangers/ cold boxes is independent of the number of complex exchangers/ cold boxes. Similarly, there may be a set of modular simple standardized liquefaction exchangers/cold boxes with integrated liquefaction refrigerant system such that the more complex, site specifics (such as H2 product subcooling and boil-off return) may be managed in a separate customized exchanger/ cold box.
[0041] As in FIG. 3, the hydrogen feed stream is again split into two 17, 19 and then further cooled and liquefied in multiple (in this embodiment two) liquefaction zones 20, 25. In FIG. 4, the cold end refrigerant is split into two streams 31, 33, with one stream 31 being first cooled in the precooling zone 10 and the second stream 33 being cooled in a second heat exchanger 30. This second heat exchanger does not include any cooling of the hydrogen feed stream, which thereby allows for greater flexibility of cooling temperatures in this second heat exchanger. For example, the cold end refrigerant 33 in this section could be cooled to a lower temperature than the cold end refrigerant 31 in the precooling zone. Put another way, the cold end temperature of the second heat exchanger can differ from the cold end temperature of the precooling zone.
[0042] Following the first cooling, the two cold end refrigerant streams can be mixed together before being split into two and sent to the two separate liquefaction zones. By combining the two cold end refrigerant streams together, the two streams used for liquefaction the hydrogen in the liquefaction zone should have substantially similar temperatures, thereby allowing identical trains to be used, which greatly reduces engineering design and fabrication costs, thereby reducing complexity. Therefore, the embodiment shown in FIG. 4 provides an advantage of being able to alter the temperature of the cold end refrigerant prior to introducing it to the hydrogen liquefaction unit without that temperature being directly tied to the hydrogen feed gas that is to be liquefied, and can provide the option for a modular (standardized package) for a portion of the precooling refrigeration system.
[0043] While FIG. 4 does not show the boil-off gas recycle, those of ordinary skill in the art will recognize that the boil-off gas recycle shown in FIG. 3 can also be used with the embodiment shown in FIG. 4. Therefore, the lack of this element in FIG. 4 should not be interpreted to be limiting.
[0044] FIG. 5 provides a process flow chart in accordance with an embodiment of the present invention. As can be seen, this embodiment includes five trains for the liquefaction unit. Therefore, in this embodiment, N=5. However, only one train for precooling is needed. This means that the embodiment shown includes four less precooling trains than the embodiments of the prior art. Therefore, embodiments of the present invention are able to produce the same amount of liquid hydrogen as the methods of the prior art, while doing so with less capital expenditures.
[0045] Although the present invention and its advantages have been described in detail, it should be understood that various changes, substitutions and alterations could be made herein without departing from the spirit and scope of the invention as defined by the appended claims. Moreover, the scope of the present application is not intended to be limited to the particular embodiments of the process, machine, manufacture, composition of matter, means, methods, and steps described in the specification. As one of ordinary skill in the art will readily appreciate from the disclosure of the present invention, processes, machines, manufacture, compositions of matter, means, methods, or steps, presently existing or later to be developed that perform substantially the same function or achieve substantially the same result as the corresponding embodiments described herein may be utilized according to the present invention. Accordingly, the appended claims are intended to include within their scope such processes, machines, manufacture, compositions of matter, means, methods, or steps. [0046] The present invention may suitably comprise, consist or consist essentially of the elements disclosed and may be practiced in the absence of an element not disclosed. Furthermore, if there is language referring to order, such as first and second, it should be understood in an exemplary sense and not in a limiting sense. For example, it can be recognized by those skilled in the art that certain steps can be combined into a single step or reversed in order.
[0047] The singular forms "a", "an", “own”, and "the" include plural referents, unless the context clearly dictates otherwise.
[0048] "Comprising" in a claim is an open transitional term which means the subsequently identified claim elements are a nonexclusive listing (i.e., anything else may be additionally included and remain within the scope of “comprising”). “Comprising” as used herein may be replaced by the more limited transitional terms "consisting essentially of and “consisting of’ unless otherwise indicated herein.
[0049] “Providing” in a claim is defined to mean furnishing, supplying, making available, or preparing something. The step may be performed by any actor in the absence of express language in the claim to the contrary a range is expressed, it is to be understood that another embodiment is from the one.
[0050] Optional or optionally means that the subsequently described event or circumstances may or may not occur. The description includes instances where the event or circumstance occurs and instances where it does not occur.
[0051] Ranges may be expressed herein as from about one particular value, and/or to about another particular value. When such particular value and/or to the other particular value, along with all combinations within said range.
[0052] All references identified herein are each hereby incorporated by reference into this application in their entireties, as well as for the specific information for which each is cited.

Claims

CLAIMS What is claimed is:
1. A method for the liquefaction of hydrogen, the method comprising the steps of: precooling a hydrogen feed stream in a precooling cold box having a heat exchanger disposed therein to form a cooled hydrogen stream, wherein the heat exchanger is configured to cool down the feed stream within the precooling cold box by indirect heat exchange between the hydrogen feed stream and a precooling refrigerant; withdrawing the cooled hydrogen stream from the precooling cold box; and introducing the cooled hydrogen stream to a plurality of liquefaction cold boxes, wherein the cooled hydrogen stream liquefies within the plurality of liquefaction cold boxes by indirect heat exchange against a liquefaction refrigerant to form a product hydrogen stream in each of the plurality of liquefaction cold boxes, wherein the product hydrogen stream is in liquid form or pseudo-liquid form, wherein there are M total precooling cold boxes and N total liquefaction cold boxes, wherein M is less than N, wherein the liquefaction refrigeration system comprises a recycle compression system and an expansion system, wherein the recycle compression system is configured to compress the liquefaction refrigerant and the expansion system is configured to expand the liquefaction refrigerant, wherein liquefaction expansion system comprises one or more liquefaction expanders, wherein the one or more liquefaction expanders are arranged in parallel or series, wherein the temperature at a cold end of the precooling cold box is in the range of 30K to 25 OK, wherein the temperature at a warm end of the liquefaction zone is in the range of 30K to 15 OK, wherein the liquefaction refrigerant comprises one or more of hydrogen, neon, and helium.
2. The method for the liquefaction of hydrogen as claimed in Claim 1, wherein there are M total recycle compression systems and N total liquefaction expansion systems.
3. The method for the liquefaction of hydrogen as claimed in Claim 1 , wherein the recycle compression system comprises one or more recycle compressors that are preferably arranged in parallel or series.
4. The method for the liquefaction of hydrogen as claimed in Claim 1, wherein the precooling system comprises a precooling refrigeration cycle.
5. The method for the liquefaction of hydrogen as claimed in Claim 1, wherein the precooling refrigerant comprises one or more of nitrogen, argon, ammonia, carbon monoxide, carbon dioxide, water, hydrocarbon, mixed hydrocarbons, and fluorocarbons.
6. The method for the liquefaction of hydrogen as claimed in Claim 1, wherein the cold end refrigeration cycle comprises a single, common recycle compression system.
7. The method for the liquefaction of hydrogen as claimed in Claim 1, further comprising an intermediate cold box in fluid communication with the precooling cold box and the plurality of liquefaction cold boxes, wherein the intermediate cold box is disposed between the precooling cold box and the plurality of liquefaction cold boxes.
8. The method for the liquefaction of hydrogen as claimed in Claim 1, wherein the ratio of N total liquefaction cold boxes to M total precooling cold boxes is between 1.25 and 3.0 (1.25 < N/M < 3.0).
9. A liquefaction method comprising the steps of: introducing a feed stream into a pre-cooling cold box at an initial temperature To and cooling the feed stream therein to form a cooled feed stream at a cooled temperature Ti; withdrawing the cooled feed stream from the pre-cooling box using a first precooling withdrawal line; splitting the cooled feed stream into a first cooled feed stream and a second cooled feed stream; providing a plurality of subcooling boxes, wherein the plurality of subcooling cold boxes comprise a first subcooling cold box and a second subcooling cold box introducing the first cooled feed stream into the first subcooling cold box under conditions effective for subcooling the first cooled feed stream to form a first product stream at a product temperature TL, wherein the first product stream is in liquid form or a pseudoliquid form; introducing the second cooled feed stream into a second subcooling cold box under conditions effective for subcooling the second cooled feed stream to form a second product stream, wherein the second product stream is in liquid form or pseudo-liquid form; withdrawing the first and second product streams from the first and second subcooling cold boxes; and combining the first and second product streams into a final product stream.
10. The liquefaction method as claimed in Claim 9, wherein each secondary cold box comprises its own heat exchanger, wherein each heat exchanger within the plurality of secondary cold boxes is configured to liquefy the feed stream by indirect heat exchanger with a liquefaction refrigerant.
11. The liquefaction method as claimed in Claim 10, further comprising a liquefaction refrigeration system, the liquefaction refrigeration system comprising a recycle compression system and an expansion system, wherein the recycle compression system is configured to compress a liquefaction refrigerant and the expansion system is configured to expand the liquefaction refrigerant.
12. The liquefaction method as claimed in Claim 10, further comprising a means for combining the liquefaction refrigerant, wherein the means for combining the liquefaction refrigerant is configured to receive the liquefaction refrigerant from a warm end of each of the plurality of secondary cold boxes via a plurality of pipes and then send the liquefaction refrigerant, after being combined, to the first cooling cold box via a first return line.
13. A hydrogen liquefaction apparatus comprising: a precooling cold box having a heat exchanger disposed therein, wherein the heat exchanger is configured to cool down a feed stream within the precooling cold box by indirect heat exchange between the feed stream and a precooling refrigerant; a plurality of liquefaction cold boxes in fluid communication with the precooling cold box, wherein each liquefaction cold box comprises its own heat exchanger, wherein each heat exchanger within the plurality of liquefaction cold boxes is configured to liquefy the feed stream by indirect heat exchange with a liquefaction refrigerant; a precooling refrigeration system configured to provide refrigeration to the precooling zone; and a liquefaction refrigeration system configured to provide the liquefaction refrigerant to the plurality of liquefaction cold boxes,
16 wherein there are M total precooling cold boxes and N total liquefaction cold boxes, wherein M is less than N, wherein the liquefaction refrigeration system comprises a recycle compression system and an expansion system, wherein the recycle compression system is configured to compress the liquefaction refrigerant and the expansion system is configured to expand the liquefaction refrigerant.
14. The hydrogen liquefaction apparatus as claimed in Claim 13, wherein there are M total recycle compression systems and/or N total liquefaction expansion systems.
15. The hydrogen liquefaction apparatus as claimed in Claim 13, wherein the recycle compression system comprises one or more recycle compressors.
16. The hydrogen liquefaction apparatus as claimed in Claim 15, wherein the one or more recycle compressors are arranged in parallel and/or series.
17. The hydrogen liquefaction apparatus as claimed in Claim 13, wherein liquefaction expansion system comprises one or more liquefaction expanders, wherein the one or more liquefaction expanders are arranged in parallel and/or series.
18. The hydrogen liquefaction apparatus as claimed in Claim 13, wherein the liquefaction refrigerant is selected from the group consisting of hydrogen, neon, helium, and combinations thereof.
19. The hydrogen liquefaction apparatus as claimed in Claim 13, wherein the liquefaction refrigerant comprises one or more of hydrogen, neon, and helium.
20. The hydrogen liquefaction apparatus as claimed in Claim 13, wherein the precooling system comprises a precooling refrigeration cycle.
21. The hydrogen liquefaction apparatus as claimed in Claim 13, wherein the precooling refrigerant is selected from the group consisting of nitrogen, argon ammonia, carbon monoxide, carbon dioxide, water, hydrocarbon, mixed hydrocarbons, fluorocarbons, and combinations thereof.
17
22. The hydrogen liquefaction apparatus as claimed in Claim 13, wherein the precooling refrigerant comprises one or more of nitrogen, argon ammonia, carbon monoxide, carbon dioxide, water, hydrocarbon, mixed hydrocarbons, and fluorocarbons.
23. The hydrogen liquefaction apparatus as claimed in Claim 13, wherein the liquefaction refrigeration system comprises a single, common recycle compression system.
24. The hydrogen liquefaction apparatus as claimed in Claim 13, further comprising an intermediate cold box in fluid communication with the precooling cold box and the plurality of liquefaction cold boxes, wherein the intermediate cold box is disposed between the precooling cold box and the plurality of liquefaction cold boxes.
25. The hydrogen liquefaction apparatus as claimed in Claim 13, wherein the ratio of N total liquefaction cold boxes to M total precooling cold boxes is between 1.25 and 3.0 (1.25 < N/M < 3.0).
26. A liquefaction apparatus comprising: a first cooling cold box configured to receive a feed stream at an initial temperature To and cool the feed stream to form a cooled feed stream at a cooled temperature Ti; a first precooling withdrawal line configured to remove the cooled feed stream from the first cooling cold box; a means for splitting the cooled feed stream, wherein the means for splitting the cooled feed stream are in fluid communication with the precooling withdrawal line; and a plurality of secondary cold boxes in fluid communication with the means for splitting the cooled feed stream, wherein the plurality of secondary cold boxes are configured to receive the cooled feed stream from the means for splitting the cooled feed stream and liquefy the cooled feed stream therein to form a liquefied stream at a liquefaction temperature TL, wherein there are M total first cooling cold boxes and N total secondary cold boxes, wherein M is less than N.
27. The liquefaction apparatus as claimed in Claim 26, wherein each secondary cold box comprises its own heat exchanger(s), wherein each heat exchanger within the plurality of secondary cold boxes is configured to liquefy the cooled feed stream by indirect heat exchange with a liquefaction refrigerant.
18
28. The liquefaction apparatus as claimed in Claim 27, further comprising a liquefaction refrigeration system, the liquefaction refrigeration system comprising a recycle compression system and an expansion system, wherein the recycle compression system is configured to compress a liquefaction refrigerant and the expansion system is configured to expand the liquefaction refrigerant.
29. The liquefaction apparatus as claimed in Claim 27, further comprising a means for combining the liquefaction refrigerant, wherein the means for combining the liquefaction refrigerant is configured to receive the liquefaction refrigerant from a warm end of each of the plurality of secondary cold boxes via a plurality of pipes and then send the liquefaction refrigerant, after being combined, to the first cooling cold box via a first return line.
30. The liquefaction apparatus as claimed in Claim 27, further comprising a second precooling withdrawal line configured to remove the liquefaction refrigeration stream from a cold end of the first cooling cold box.
31. The liquefaction apparatus as claimed in Claim 30, further comprising a means for splitting the liquefaction refrigeration stream, wherein the means for splitting the liquefaction refrigeration stream are in fluid communication with the second precooling withdrawal line.
19
EP22854223.9A 2021-12-22 2022-12-16 Method for large hydrogen liquefaction system Pending EP4453489A2 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US202163293080P 2021-12-22 2021-12-22
PCT/US2022/053257 WO2023121985A2 (en) 2021-12-22 2022-12-16 Method for large hydrogen liquefaction system

Publications (1)

Publication Number Publication Date
EP4453489A2 true EP4453489A2 (en) 2024-10-30

Family

ID=85172657

Family Applications (1)

Application Number Title Priority Date Filing Date
EP22854223.9A Pending EP4453489A2 (en) 2021-12-22 2022-12-16 Method for large hydrogen liquefaction system

Country Status (7)

Country Link
US (1) US20230194159A1 (en)
EP (1) EP4453489A2 (en)
JP (1) JP7746584B2 (en)
KR (1) KR20240122526A (en)
AU (1) AU2022418513B2 (en)
CA (1) CA3241196A1 (en)
WO (1) WO2023121985A2 (en)

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3180709A (en) * 1961-06-29 1965-04-27 Union Carbide Corp Process for liquefaction of lowboiling gases
JPS59134479A (en) * 1983-01-20 1984-08-02 株式会社神戸製鋼所 Device for liquefying and refrigerating helium
US9435583B2 (en) * 2006-09-22 2016-09-06 Shell Oil Company Method and apparatus for liquefying a hydrocarbon stream
WO2008081018A2 (en) * 2007-01-04 2008-07-10 Shell Internationale Research Maatschappij B.V. Method and apparatus for liquefying a hydrocarbon stream
US20180038642A1 (en) * 2016-08-05 2018-02-08 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process integration of a gas processing unit with liquefaction unit
FR3108390B1 (en) * 2020-03-23 2022-11-25 Air Liquide Hydrogen refrigeration plant and process
CN113446815B (en) * 2021-09-01 2021-11-12 杭州制氧机集团股份有限公司 Hydrogen liquefaction equipment adopting mixed refrigeration and using method thereof

Also Published As

Publication number Publication date
AU2022418513B2 (en) 2026-03-05
JP7746584B2 (en) 2025-09-30
JP2024543656A (en) 2024-11-21
AU2022418513A1 (en) 2024-08-01
CA3241196A1 (en) 2023-06-29
WO2023121985A2 (en) 2023-06-29
WO2023121985A3 (en) 2023-08-10
US20230194159A1 (en) 2023-06-22
KR20240122526A (en) 2024-08-12

Similar Documents

Publication Publication Date Title
US20230009727A1 (en) Method for large hydrogen liquefaction system
US7143606B2 (en) Combined air separation natural gas liquefaction plant
JP7488093B2 (en) Liquefied hydrogen production facility
AU2019202814B2 (en) Method and system for cooling a hydrocarbon stream using a gas phase refrigerant
EP3561421B1 (en) Improved method and system for cooling a hydrocarbon stream using a gas phase refrigerant
US10520225B2 (en) Refrigeration and/or liquefaction device using selective pre-cooling, and corresponding method
US20200041201A1 (en) Refrigeration and/or liquefaction device, and associated method
AU2017203215B2 (en) Liquefaction method and system
KR20230074241A (en) Process for producing liquid hydrogen
AU2007310940B2 (en) Method and apparatus for liquefying hydrocarbon streams
CN119790273A (en) Cryogenic gas cooling system and method
US20240393041A1 (en) Installation and method for the liquefaction of hydrogen
KR100991859B1 (en) Fluid Cooling System and Fluid Cooling Method Using the Same
AU2022418513B2 (en) Method for large hydrogen liquefaction system
CN117190624A (en) A hydrogen liquefaction system with dual-phase expansion refrigeration
WO2005080892A1 (en) Liquefying hydrogen
AU2022429663B2 (en) Process for precooling hydrogen for liquefaction with supplement liquid nitrogen
US20230272971A1 (en) Single mixed refrigerant lng production process
CN212481844U (en) Air separation plant
AU2024291367A1 (en) Installation and method for producing a cryogenic fluid
KR20260012584A (en) High efficiency hydrogen liquefaction system and hydrogen liquefaction process using the same
CN120777841A (en) Hydrogen liquefaction system

Legal Events

Date Code Title Description
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: UNKNOWN

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

Free format text: STATUS: THE INTERNATIONAL PUBLICATION HAS BEEN MADE

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

Free format text: ORIGINAL CODE: 0009012

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

Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE

17P Request for examination filed

Effective date: 20240722

AK Designated contracting states

Kind code of ref document: A2

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

DAV Request for validation of the european patent (deleted)
DAX Request for extension of the european patent (deleted)
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

17Q First examination report despatched

Effective date: 20260213