GB2609503A - Process for producing liquefied hydrogen - Google Patents

Process for producing liquefied hydrogen Download PDF

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Publication number
GB2609503A
GB2609503A GB2111396.4A GB202111396A GB2609503A GB 2609503 A GB2609503 A GB 2609503A GB 202111396 A GB202111396 A GB 202111396A GB 2609503 A GB2609503 A GB 2609503A
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United Kingdom
Prior art keywords
stream
hydrogen
heat exchanger
outlet
degc
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GB2111396.4A
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GB2609503B (en
Inventor
Frederick Skinner Geoffrey
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Gasconsult Ltd
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Gasconsult Ltd
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Priority to GB2111396.4A priority Critical patent/GB2609503B/en
Priority to CN202280048063.7A priority patent/CN117616243A/en
Priority to KR1020247003566A priority patent/KR20240045212A/en
Priority to PCT/GB2022/000065 priority patent/WO2023012443A1/en
Priority to AU2022324729A priority patent/AU2022324729A1/en
Publication of GB2609503A publication Critical patent/GB2609503A/en
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Publication of GB2609503B publication Critical patent/GB2609503B/en
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    • 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
    • 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
    • F25J1/006—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
    • F25J1/02—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
    • F25J1/0211—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 multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0219—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 multi-component refrigerant [MCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. using a deep flash recycle loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
    • F25J1/0224—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop in combination with an internal quasi-closed refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/82—Processes or apparatus using other separation and/or other processing means using a reactor with combustion or catalytic reaction
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/10—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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/90—Separating isotopes of a component, e.g. H2, O2

Abstract

A process for liquefying hydrogen gas comprising: providing a feed stream 1 at between 10 and 150 bar, cooling the gas to -150C to -210C in a first heat exchanger A, passing the said cooled hydrogen over a catalyst C which facilitates substantially complete conversion of its ortho-hydrogen content to parahydrogen, with provision of further cooling to between -210C and –250C, combining with a recycle stream 11, and passing the resulting stream 6, essentially comprising para-hydrogen, in the form of a gas or vapour to an expander machine E or turbine having an outlet stream consisting of vapour and liquid, separating the said outlet stream into vapour and liquid fractions in a separator F, the liquid fraction constituting the liquefied hydrogen product 7 of the process and recycling the vapour fraction by means of one or more compressors H, to form the recycle stream 11

Description

Description
Process for Producing Liquefied Hydrogen
Field of the Invention
The present invention relates to a method for liquefying hydrogen gas, in particular a method of liquefaction by means of a partially-liquefying expander machine or turbine.
Background
Liquefied hydrogen is a potential substitute for carbon-containing fuels. In addition to its current use in space applications, larger quantities of liquid hydrogen will be required in the future for use as fuel for aviation, shipping and other transportation purposes. A need for large-scale storage and transport of hydrogen in liquid form will develop as the use of hydrogen as a fuel increases.
As is well known, hydrogen at ambient temperature ("normal" hydrogen) exists as a mixture of two forms, 75% ortho-hydrogen and 25% para-hydrogen, while at liquid hydrogen temperatures circa -250 degC the equilibrium composition is almost completely para-hydrogen. Accordingly hydrogen liquefaction technology generally includes one or more stages of catalytic conversion at low temperatures in the range of -200 degC to -250 degC approximately, in which the ortho-hydrogen content of the incoming feed hydrogen is exothermically converted into para-hydrogen upstream of the final liquefaction step. In the absence of this catalysed conversion step, the ortho-hydrogen content of the liquefied hydrogen would slowly convert exothermically to para-hydrogen in the storage tank, with the result that most or all of the product would evaporate and be lost.
Existing and proposed hydrogen liquefaction processes generally comprise a step or steps of conversion of the ortho-hydrogen content of the feed gas into para-hydrogen, followed by a step or steps of liquefaction of the resulting para-hydrogen gas or vapour by means of indirect heat exchange with a colder fluid.
Helium is already used, and is proposed for future use, as the said colder fluid, due to its low boiling temperature range relative to hydrogen (helium -269 degC, hydrogen -253 deg at atmospheric pressure).
Helium is accordingly an excellent refrigerant for hydrogen liquefaction, but it is expensive, and its price is expected to rise with growth in use in hydrogen liquefaction and for other purposes. Also there may be logistical difficulties in replenishing a closed-circuit helium system in a large industrial plant following a significant leak or an accident of some kind.
So as to overcome these potential difficulties associated with use of helium, hydrogen itself may be considered for use as the colder fluid in the final heat exchange stages. As proposed by U GardeIla (doctoral dissertation, Technische Universitat MOnchen, 2018 and perhaps others), "normal" hydrogen, i.e. with content 75% ortho-hydrogen + 25% para-hydrogen, may be used in a closed refrigeration circuit, with only the quantity of hydrogen to be liquefied as product being passed over a catalyst for conversion of its orthohydrogen content into para-hydrogen.
The use of hydrogen as the cold-end refrigerant avoids the above-mentioned economic and practical objections to helium, but very small temperature differences are necessary in the coldest heat exchangers, and this may be difficult to arrange when the product hydrogen is required to be delivered at near-atmospheric pressure.
Summary of the Invention
The invention relates to the final stage of a process for liquefaction of hydrogen, in particular to the use of hydrogen as the refrigerating fluid Where pressures are stated anywhere in this application as "bar", these are bar absolute.
The term expander where used in this application describes a process duty only. More than one expander machine or rotor in series may be required for an individual process duty.
The invention, which has two aspects, has the aim of avoiding reliance on a final condensing heat exchanger with close temperature approaches, and of facilitating the production of liquid hydrogen at near-atmospheric pressures.
According to the first aspect of the invention, a final heat exchanger as described in prior art, typically requiring close temperature approaches of around 1 degC, in which hydrogen in the form of para-hydrogen is condensed by indirect heat exchanger with colder "normal" hydrogen, is replaced with an expander machine or turbine, having an outlet stream consisting of vapour and liquid. The expander outlet stream flows to a vapour-liquid separator, which may be integrated with a storage tank, in which the liquid fraction is separated to form the liquefied hydrogen product of the process, and the vapour fraction is re-compressed and recycled.
According to the second aspect of the invention, the extent of reconversion of para-hydrogen into ortho-hydrogen during the above-said re-compression and recycling steps is minimised by providing for the re-compressor to operate with one or more compression stages having cryogenic inlet temperatures.
Inevitably some back-conversion of para-hydrogen into ortho-hydrogen will take place during the said re-compressed and recycling steps, and provision is made for conversion of the resulting relatively small amount of ortho-hydrogen by means of a further body of catalyst located in a lower temperature region of the process.
The Applicant respectfully submits that the described combination of (1) production of liquid hydrogen in a partially liquefying para-hydrogen expander machine, and (2) recompression and recycle of the separated vapour fraction of the expander outlet stream at cryogenic temperature (so as to minimise reverse conversion of para-hydrogen into ortho-hydrogen) is both novel and inventive.
From the viewpoint of practical application in a hydrogen liquefaction plant in which hydrogen is used as the refrigerating fluid, use of the invention removes in the expander, in the form of mechanical work, the heat of condensation of the product hydrogen, thereby significantly reducing or eliminating the need for low temperature heat exchangers with small temperature approaches, and by compressing the recycled hydrogen at low temperature and hence increased density, reduces the power required for the hydrogen recycle compression and facilitates the use of a centrifugal hydrogen compressor.
Accordingly there is provided as follows a description of a process for liquefying hydrogen, illustrating the main aspects of the invention (reference is made to Drawing 1/3 and the equipment tags and stream numbers shown thereon): - providing a stream of pure hydrogen feed gas [1] at a pressure of between 10 bar and 150 bar; - cooling stream [1] in heat exchanger [A], having an outlet stream [2] with a temperature of between -150 degC and -210 degC; - admitting stream [2] to assembly [B] comprising a catalyst [C] for conversion of ortho-hydrogen to para-hydrogen having an outlet stream [3] and a heat exchanger [D] having an outlet stream [4], the said assembly [B] comprising multiples of catalyst [C] and heat exchanger [D], such that the composition of stream [4] is essentially para-hydrogen, with a temperature of between -210 degC and -250 degC; - providing a recycle stream of hydrogen [11] having a composition essentially of para-hydrogen and having the same pressure as stream [4]; - combining stream [4] and stream [11] to form stream [5]; - admitting stream [5] to an expander machine [E] having an outlet stream [6] with a pressure of between 10 bar and 1 bar and containing both liquid and vapour; - passing stream [6] to a vessel [F] wherein the liquid fraction stream [7], comprising the liquid hydrogen product from the process, is separated from the vapour fraction stream [8]; - providing vessel [F] with a catalyst which converts residual ortho-hydrogen in stream [6] into para-hydrogen; - reheating stream [8] in a heat exchanger [G] to form outlet stream [9], having a temperature of between -100 degC and -240 degC; -admitting stream [9] to a compressor [H]; - providing compressor [H] with an outlet stream [10] having a pressure between 10 bar and 150 bar; - cooling stream [10] in a heat exchanger [I], having as outlet stream the aforementioned stream [11].
Drawing 2/3 shows a version of Drawing 1/3 in which the catalyst in assembly [B] is incorporated in a hot passage of heat exchanger [D].
In a further aspect of the foregoing description, the expander machine [E] may be split into two or more stages in series, when in a particular use of the invention it is desirable for streams [4] and stream [11] to have different pressures or temperatures. In such a case one of the two said streams may be admitted to expander machine [E] at intermediate stage(s).
Moreover one or more additional heat exchangers may be introduced between stages of the said expander machine [E]; Embodiment of the Invention There is furthermore also provided a description of an embodiment of the invention (reference is made to Drawing 3/3 and the equipment tags and stream numbers shown thereon): providing a stream of pure hydrogen feed gas [21] at a pressure of between 10 bar and 150 bar; - cooling stream [21] in a hot passage of heat exchanger [a], having an outlet stream [22] with a temperature of between 0 degC to -150 degC; - further cooling stream [22] in a first hot passage of heat exchanger [b], having an outlet stream [23] with a temperature of between -150 degC and -210 degC; - admitting stream [23] to assembly [c] comprising a catalyst [d] for conversion of ortho-hydrogen to para-hydrogen with outlet stream [24] and a heat exchanger [e] provided with a first hot passage having an outlet stream [25], such that the composition of stream [25] is essentially para-hydrogen, with a temperature of between -210 degC and -250 degC; providing a recycle stream of hydrogen [35] having a composition essentially of para-hydrogen and having the same pressure as stream [25]; combining stream [25] and stream [35] to form stream [26]; admitting stream [26] to a first expander machine [f] having an outlet stream [27] with a pressure of between 10 bar and 1 bar and containing both liquid and vapour; passing stream [27] to a vessel [g] wherein the liquid fraction stream [28], comprising the liquid hydrogen product from the process, is separated from the vapour fraction stream [29]; providing vessel [g] with a catalyst which converts residual orthohydrogen in stream [27] into para-hydrogen; reheating stream [29] successively in a first cold passage of heat exchanger [e] to form outlet stream [30] and in a first cold passage of heat exchanger [b] to form outlet stream [31] having a temperature of between -100 degC and -240 degC; admitting stream [31] to compressor [h] as a first, lower pressure inlet stream; providing compressor [h] with a second, higher pressure inlet stream [39] having a composition essentially of para-hydrogen; providing compressor [h] with an outlet stream [32] having a pressure of between 10 bar and 150 bar; - cooling stream [32] in a second hot passage of heat exchanger [b], having an outlet stream [33] and the same temperature as stream [23]; - dividing stream [33] into two parts, stream [34] and stream [36]; - cooling stream [34] in a second hot passage of heat exchanger [e] having as its outlet stream the above-mentioned stream [35]; - passing stream [36] to a second expander machine [i], having an outlet stream [37] with a pressure of between 30 bar and 2 bar; - reheating stream [37] successively in a second cold passage of heat exchanger [e] to form outlet stream [38] and in a second cold passage of heat exchanger [b] to form the aforementioned outlet stream [39]; - providing a stream of refrigerant fluid [40], and passing said stream [40] through a cold passage of heat exchanger [a], haying an outlet stream [41]; - providing a stream of refrigerant fluid [42], and passing said stream [42] through a third cold passage of heat exchanger [b], having an outlet stream [43].

Claims (3)

  1. Claims 1 A process for liquefying hydrogen gas comprising - providing a stream of pure hydrogen feed gas [1] at a pressure of between 10 bar and 150 bar; -cooling stream [1] in a hot passage of heat exchanger [A], having an outlet stream [2] with a temperature of between -150 degC and -210 degC; - admitting stream [2] to assembly [B] comprising a catalyst [C] for conversion of ortho-hydrogen to para-hydrogen with outlet stream [3] and a heat exchanger [D] having an outlet stream [4], the said assembly [B] comprising multiples of catalyst [C] and heat exchanger [D], such that the composition of stream [4] is essentially para-hydrogen, with a temperature of between -210 degC and -250 degC; - providing a recycle stream of hydrogen [11] having a composition essentially of para-hydrogen and having the same pressure as stream [4]; - combining stream [4] and stream [11] to form stream [5]; - admitting stream [5] to an expander machine [E] having an outlet stream [6] with a pressure of between 10 bar and 1 bar and containing both liquid and vapour; - passing stream [6] to a vessel [F] wherein the liquid fraction stream [7], comprising the liquid hydrogen product from the process, is separated from the vapour fraction stream [8]; - providing vessel [F] with a catalyst which converts residual ortho-hydrogen in stream [6] into para-hydrogen; - reheating stream [8] in a heat exchanger [G] to form outlet stream [9], having a temperature of between -100 degC and -240 degC; -admitting stream [9] to a compressor [H]; - providing compressor [H] with an outlet stream [10] having a pressure between 10 bar and 150 bar; - cooling stream [10] in a heat exchanger [I], having as outlet stream the aforementioned stream [11].
  2. 2.A process as claimed in Claim 1 in which the catalyst in assembly [B] is incorporated in a hot passage of heat exchanger [D].
  3. 3 A process as claimed in either preceding claim in which the expander machine [E] is split into stages in series, whereby streams [4] and stream [11] are admitted at different pressures; 4 A process as claimed in any preceding claim in which one or more additional heat exchangers are introduced between the stages of the said expander machine [E]; A process for liquefying hydrogen gas comprising - providing a stream of pure hydrogen feed gas [21] at a pressure of between 10 bar and 150 bar; - cooling stream [21] in a hot passage of heat exchanger [a], having an outlet stream [22] with a temperature of between 0 degC to -150 degC; - further cooling stream [22] in a first hot passage of heat exchanger [b], having an outlet stream [23] with a temperature of between -150 degC and -210 degC; - admitting stream [23] to assembly [c] comprising a catalyst [d] for conversion of ortho-hydrogen to para-hydrogen with outlet stream [24] and a heat exchanger [e] provided with a first hot passage having an outlet stream [25], the said assembly [c] comprising multiples of catalyst [d] and heat exchanger [e], such that the composition of stream [25] is essentially para-hydrogen, with a temperature of between -210 degC and -250 degC; - providing a recycle stream of hydrogen [35] having a composition essentially of para-hydrogen and having the same pressure as stream [25]; - combining stream [25] and stream [35] to form stream [26]; -admitting stream [26] to a first expander machine [1] having an outlet stream [27] with a pressure of between 10 bar and 1 bar and containing both liquid and vapour; - passing stream [27] to a vessel [g] wherein the liquid fraction stream [28], comprising the liquid hydrogen product from the process, is separated from the vapour fraction stream [29]; - providing vessel [g] with a catalyst which converts residual ortho-hydrogen in stream [27] into para-hydrogen; - reheating stream [29] successively in a first cold passage of heat exchanger [e] to form outlet stream [30] and in a first cold passage of heat exchanger [b] to form outlet stream [31] having a temperature of between -100 degC and -240 degC; -admitting stream [31] to compressor [h] as a first, lower pressure inlet stream; - providing compressor [h] with a second, higher pressure inlet stream [39] having a composition essentially of para-hydrogen; - providing compressor [h] with an outlet stream [32] having a pressure between 10 bar and 150 bar; - cooling stream [32] in a second hot passage of heat exchanger [b], having a outlet stream [33] and the same temperature as stream [23]; dividing stream [33] into two parts, stream [34] and stream [36]; - cooling stream [34] in a second hot passage of heat exchanger [e] having as its outlet stream the above-mentioned stream [35]; - passing stream [36] to a second expander machine [i], having an outlet stream [37] with a pressure of between 30 bar and 2 bar; - reheating stream [37] successively in a second cold passage of heat exchanger [e] to form outlet stream [38] and in a second cold passage of heat exchanger [b] to form the aforementioned outlet stream [39]; - providing a stream of refrigerant fluid [40], and passing said stream [40]; through a cold passage of heat exchanger [a], haying an outlet stream [41]; - providing a stream of refrigerant fluid [42], and passing said stream [42] through a third cold passage of heat exchanger [b], haying an outlet stream [43].
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KR1020247003566A KR20240045212A (en) 2021-08-06 2022-07-12 Liquefied hydrogen production method
PCT/GB2022/000065 WO2023012443A1 (en) 2021-08-06 2022-07-12 Process for producing liquefied hydrogen
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Citations (2)

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Publication number Priority date Publication date Assignee Title
US2937076A (en) * 1957-12-13 1960-05-17 Beech Aircraft Corp Process for the production of para liquid hydrogen
US20100272634A1 (en) * 2009-04-23 2010-10-28 Joseph Michael Schwartz Hydrogen liquefaction method and liquefier

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3375076A (en) * 1963-10-16 1968-03-26 Air Prod & Chem Liquefaction and conversion process
JP2004210597A (en) * 2003-01-06 2004-07-29 Toshiba Corp Waste-heat-using hydrogen/oxygen system and method for producing liquid hydrogen
GB0406615D0 (en) * 2004-03-24 2004-04-28 Air Prod & Chem Process and apparatus for liquefying hydrogen

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2937076A (en) * 1957-12-13 1960-05-17 Beech Aircraft Corp Process for the production of para liquid hydrogen
US20100272634A1 (en) * 2009-04-23 2010-10-28 Joseph Michael Schwartz Hydrogen liquefaction method and liquefier

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