EP3339605A1 - Procédé de compression d'un mélange de gaz comprenant néon - Google Patents

Procédé de compression d'un mélange de gaz comprenant néon Download PDF

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Publication number
EP3339605A1
EP3339605A1 EP16206671.6A EP16206671A EP3339605A1 EP 3339605 A1 EP3339605 A1 EP 3339605A1 EP 16206671 A EP16206671 A EP 16206671A EP 3339605 A1 EP3339605 A1 EP 3339605A1
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EP
European Patent Office
Prior art keywords
gas mixture
gas
hydrogen
stream
chamber
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.)
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Application number
EP16206671.6A
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German (de)
English (en)
Inventor
Umberto Cardella
Lutz Decker
Harald Klein
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.)
Linde GmbH
Technische Universitaet Muenchen
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Linde GmbH
Technische Universitaet Muenchen
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Application filed by Linde GmbH, Technische Universitaet Muenchen filed Critical Linde GmbH
Priority to EP16206671.6A priority Critical patent/EP3339605A1/fr
Priority to PCT/EP2017/084417 priority patent/WO2018115456A1/fr
Publication of EP3339605A1 publication Critical patent/EP3339605A1/fr
Withdrawn legal-status Critical Current

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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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
    • F25B9/006—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant containing more than one component
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D29/00—Details, component parts, or accessories
    • F04D29/08—Sealings
    • F04D29/10—Shaft sealings
    • F04D29/102—Shaft sealings especially adapted for elastic fluid pumps
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D29/00—Details, component parts, or accessories
    • F04D29/08—Sealings
    • F04D29/10—Shaft sealings
    • F04D29/102—Shaft sealings especially adapted for elastic fluid pumps
    • F04D29/104—Shaft sealings especially adapted for elastic fluid pumps the sealing fluid being other than the working fluid or being the working fluid treated
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D29/00—Details, component parts, or accessories
    • F04D29/08—Sealings
    • F04D29/10—Shaft sealings
    • F04D29/12—Shaft sealings using sealing-rings
    • F04D29/122—Shaft sealings using sealing-rings especially adapted for elastic fluid pumps
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D29/00—Details, component parts, or accessories
    • F04D29/08—Sealings
    • F04D29/10—Shaft sealings
    • F04D29/12—Shaft sealings using sealing-rings
    • F04D29/122—Shaft sealings using sealing-rings especially adapted for elastic fluid pumps
    • F04D29/124—Shaft sealings using sealing-rings especially adapted for elastic fluid pumps with special means for adducting cooling or sealing fluid
    • 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
    • F25J1/0007—Helium
    • 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
    • F25J1/0047—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
    • 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
    • F25J1/0065—Helium
    • 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
    • F25J1/0211—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
    • F25J1/0217—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 as at least a three level refrigeration cascade with at least one MCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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.
    • 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

Definitions

  • the present invention relates to a method for compressing and controlling a gas mixture for use in a cryogenic refrigeration cycle.
  • the invention relates to a method for compressing and controlling a refrigerant gas mixture comprising neon, for use in a cryogenic refrigeration cycle
  • Cryogenic cooling and liquefaction of hydrogen and helium is performed at very low temperatures below 30 K. Therefore, cryogenic refrigeration cycles for this purpose are restricted to the use of hydrogen, helium, neon and/or mixtures of these fluids.
  • a significant energy input is required in order to provide the cooling, and is mainly provided by the required gas compressors.
  • Conventional hydrogen and helium liquefaction plants or refrigerators use reciprocating piston compressors and/or rotary screw compressors to compress the coolants in a closed refrigeration cycle e.g. mainly hydrogen and/or helium. These machines are, however, restricted in volumetric flow and/or efficiency.
  • Hydrogen as a cryogenic coolant for a hydrogen liquefier is abundantly available and comparatively inexpensive. Due to the extremely low molecular mass of hydrogen, 2.02 g per mol, only a very small increase in pressure per turbo compressor stage can be achieved with conventional ambient temperature turbo compressors at conventional circumferential speeds (below 400 m/s). A correspondingly very high number of compressor stages of at least 15 stages would be required to provide the cooling for a hydrogen liquefier, which is technically and commercially highly unfavourable.
  • Helium has a higher molecular mass than hydrogen, about 4 g per mol, but is comparatively still very light. In the range of conventional maximum operating speeds, only low turbo compressor stage pressure ratios can thus be generated.
  • Neon as a cryogenic refrigerant is interesting due to the comparatively high molecular mass of nearly 20 g per mol. Neon can thus be efficiently compressed in turbo compressors near ambient temperature with an economically feasible number of turbo compressor stages. Neon as a potential refrigerant, however, is even more expensive than helium. Therefore, regular continuous leakage rates in the range of up to about 10 norm cubic meter per hour (Nm 3 /h) per turbo compressor stage, especially through the seals of conventional turbo compressors, must be strictly avoided in order to limit expensive inventory losses and to allow an economically practicable plant operation.
  • refrigerant mixtures particularly helium-neon and hydrogen-neon refrigerant mixtures
  • a molar mass above 7 g per mol have been proposed, particularly with a molar mass above 7 g per mol.
  • Helium-neon mixtures used as refrigerants for hydrogen liquefiers achieve a lower energy efficiency as coolants and are made of two extremely expensive gases (helium and neon) compared to pure hydrogen or hydrogen-neon mixtures.
  • Helium-neon gas mixtures thus require hermetically sealed turbo compressors in order to maintain commercially reasonable operating costs.
  • These hermetically sealed machines cannot be operated at high rotational speeds due to their special construction and are thus limited also in energy efficiency and feasible stage pressure ratio, requiring a relatively high number of compression stages and a high capital investment even for gases or gas mixtures with a relatively high molar mass.
  • a dry gas seal is a device for the sealing of a turbo compressor whose shaft is sealed against the housing with the use of a sealing gas.
  • Conventional dry gas seal turbo machines usually make use of a gas taken directly from the process refrigerant feed and/or nitrogen as external seal gas, since nitrogen is inert and inexpensive.
  • a leakage of nitrogen into the process refrigerant feed can be tolerated in most applications due to the freezing point of pure nitrogen being at 63 K and thus significantly below the typical operational temperature for general applications, in particular for LNG plants.
  • nitrogen as primary external seal gas
  • turbo compressors having for example single or double gas seals
  • hydrogen, helium, neon or a gas mixture of these can be used as sealing gases and can be supplied either directly from the process gas compressor or from an external source, particularly for cryogenic refrigeration cycles involving hydrogen, helium, neon or mixtures of these coolants e.g. in hydrogen or helium liquefiers/refrigerators.
  • Embodiments of the invention seek to provide an apparatus which overcome some or all of these problems.
  • a method for compressing a gas mixture comprising neon, in a closed-loop cycle comprising:
  • the gas mixture is also referred to as the first process fluid (or refrigerant), and the one gas seals are also referred to as the second/third/fourth process fluid.
  • the compression device may be a compressor.
  • the compression device may be a turbo compressor, preferably a radial (centrifugal) turbo compressor
  • the step of determining if there is a deviation may comprise evaluating whether the measured composition is above a predefined maximum value.
  • the step of determining if there is a deviation may comprise evaluating whether the measured composition is below a predefined minimum value.
  • the step of determining if there is a deviation may comprise evaluating whether the measured composition is outside a predefined range.
  • the gas mixture may comprise hydrogen.
  • the or at least one gas seal may comprise hydrogen.
  • the gas mixture may be a refrigerant mixture comprising or essentially consisting of hydrogen and neon.
  • the gas mixture may be a refrigerant mixture comprising or essentially consisting of helium and neon.
  • the gas mixture may comprise or essentially consist of hydrogen and neon.
  • the gas mixture may have a molecular mass in the range of 3.88 g*mol -1 to 13 g*mol -1
  • the gas mixture may have a molecular mass in the range of 6.5 g*mol -1 to 11.2 g*mol -1 .
  • the step of adjusting at least one process parameter may comprise adjusting the temperature and/or the pressure of said gas mixture.
  • the step of adjusting at least one process parameter may comprise adjusting the temperature and/or pressure of said compressed gas mixture.
  • the step of adjusting at least one process parameter may comprise adjusting the compression performance of the compression device.
  • the step of adjusting at least one process parameter may comprise adjusting the compression ratio of the compression device.
  • the step of adjusting at least one process parameter may comprise adjusting the pressure ratios at the inlet and/or outlet of the compression device (11) in order to adapt the operating point to the changing gas mixture composition.
  • the method may also include passing partial stream(s) of the compressed gas mixture through at least one turbo expander.
  • the step of adjusting the at least one process parameter may comprise adjusting the pressure ratios at the inlet and/or outlet of the or each turbo expander in order to adapt the operating point to the changing gas mixture composition.
  • the step of adjusting the at least one process parameter may comprise adjusting the cycle process temperature at an outlet of the or the coldest turbo expander.
  • the cycle process temperature may be adjusted by manipulating the high/low gas pressure levels of the refrigeration cycle.
  • the step of adjusting at least one process parameter may comprise adapting the pressure ratio of the refrigeration cycle (HP to LP) as a function of the measured gas mixture composition.
  • the method may also include passing a partial stream of the compressed gas mixture through at least one turbo expander.
  • the step of adjusting the at least one process parameter may comprise varying a cycle process temperature at an outlet of the or the coldest turbo expander.
  • the method may also include passing a first partial stream of the compressed gas mixture through a first turbo expander.
  • the method may also include passing a second partial stream of the compressed gas mixture through a second turbo expander.
  • the step of adjusting the at least one process parameter may comprise adjusting the cycle process temperature at the outlet of the coldest turbo expander.
  • the step of adjusting the at least one process parameter may comprise controlling at least one of the compressor operating speeds of the compression device.
  • the step of measuring a composition of the gas mixture may include measuring the volumetric fraction of at least one constituent of the gas mixture.
  • the measurement of the composition may be performed before compression of the gas mixture in the compression device.
  • the measurement of the composition may be taken after compression of the gas mixture in the compression device.
  • the composition of the gas mixture may be measured using any suitable gas analysing device for example. a gas chromatograph.
  • the step of adjusting of said process parameter is performed automatically.
  • the step of determining if there is a deviation may include generating a data signal relating to the measured gas composition and conveying this signal to a control device.
  • the step of determining if there is a deviation may be carried out by a control device.
  • the control device determine the required adjustment at least one process parameter and convey a control signal to adjust the at least one process parameter.
  • the step of adjusting the composition of the gas mixture in the cycle may comprise extracting a partial, high pressure stream from said compressed gas.
  • the step of adjusting the composition of the gas mixture in the cycle may comprise separating the partial stream into a mainly liquid phase and a mainly vapour phase.
  • the step of separating the partial stream may include passing the partial stream through a phase separator to produce the mainly liquid phase and the mainly vapour phase.
  • the step of separating the partial stream may include passing the vapour phase through a second phase separator or second phase separator phase.
  • the gas mixture may comprise neon and hydrogen, such that the step of separating the partial stream involves separation into a mainly liquid neon phase and a mainly vapour hydrogen phase.
  • the partial stream may also be cooled (for example in a Joule-Thomson valve or other suitable device) prior to the separation step.
  • the partial stream may be extracted (or drawn off) continuously or intermittently.
  • a control device such as a valve, may be provided to control the partial flow (draw off).
  • the method according to claim 9, wherein the method also includes passing the partial stream(s) of the compressed gas mixture through at least one turbo expander; and wherein the high pressure partial stream is extracted from a high pressure end of one turbo expander. In other words the high pressure partial stream may be extracted immediately upstream of the turbo expander.
  • the gas mixture may comprise hydrogen and neon, such that the mainly liquid phase of the partial stream comprises mainly neon and the mainly vapour phase of the partial stream comprises mainly comprising hydrogen.
  • the method may include providing two turbo expanders.
  • the method may include passing a first partial stream through a first turbo expander and a second partial stream through a second turbo expander.
  • the high pressure partial stream is extracted from a high pressure end of the coldest turbo expander (in other words, upstream of the coldest turbo expander).
  • the step of adjusting the composition of the gas mixture in the cycle may comprise extracting a partial stream from said gas mixture prior to the compression step.
  • the partial stream may be separated into a mainly liquid phase comprising mainly neon and a mainly vapour phase comprising mainly hydrogen.
  • the partial stream may also be cooled prior to the separation step.
  • the method may also include feeding at least part of said mainly liquid phase into the gas mixture flow or into the compressed gas mixture flow. At least part of said mainly liquid phase may be fed into the gas mixture flow or into the compressed gas mixture flow at any suitable point in the closed loop cycle.
  • the gas mixture may comprise neon and hydrogen, such that the step of separating the partial stream involves separation into a mainly liquid neon phase and a mainly vapour hydrogen phase.
  • the compression device may include two gas seals.
  • the method may include providing a first gas flow to the first gas seal and providing a second gas flow to the second gas seal.
  • the compression device may include three gas seals.
  • the method may include providing a gas flow to each gas seal.
  • the method may further comprise conveying the compressed gas mixture for use as a refrigerant in a cryogenic refrigerant cycle.
  • the compressed gas mixture may be used as a refrigerant in a cryogenic cooling cycle.
  • the compressed gas mixture may be used as a refrigerant in a cryogenic cooling cycle for liquefying hydrogen or helium.
  • the compressed gas mixture may be used as a refrigerant, particularly in a cryogenic cooling cycle
  • a method for liquefying hydrogen or helium comprising the steps of:
  • turbo compressor particularly a radial turbo compressor, having
  • the fourth chamber may be is separated from the ambient environment by a fourth separating element and in fluid connection with said ambient environment by a fourth opening in said fourth separating element.
  • Said rotating element may extend through said fourth opening.
  • the process may comprise the following steps
  • a partial stream may be separated from the compressed first process fluid, expanded and optionally cooled such that an expanded partial stream comprising a mainly liquid phase comprising mainly neon and a mainly vapour phase mainly comprising hydrogen is yielded.
  • a partial stream is separated from the first process fluid, optionally cooled and separated into said mainly liquid phase comprising mainly neon and a mainly vapour phase comprising mainly hydrogen.
  • the mainly liquid phase may be at least partly recycled (fed into) the gas mixture (refrigerant mixture).
  • the mainly liquid phase may be at least partly recycled (fed into) into the first process fluid or the compressed first process fluid.
  • a process for compressing and controlling a gas mixture comprising neon is provided.
  • the process may comprise the steps of:
  • the second process fluid is designed to serve as a seal fluid.
  • non-hermetically in the context of the present specification particularly means that a fluid may flow from one chamber in the other chamber.
  • mainly liquid stream in the context of the present specification refers to a stream wherein the majority of the molecules within the stream are present in the liquid phase.
  • vapour stream in the context of the present specification refers to a stream wherein the majority of the molecules within the stream are present in the vapour phase.
  • the term "comprising mainly neon” in the context of the present specification refers to a feature of a stream or phase, which is characterized by a neon molecular fraction above 50 %, particularly at least 60 %, 70 %, or 80%.
  • the term "comprising mainly neon" in the context of the present specification refers to a feature of a stream or phase, having a hydrogen molecular fraction above 50 %, particularly at least 60 %, 70 %, or 80%.
  • the first chamber and the second chamber are comprised within a compressor, particularly a turbo compressor, wherein the first chamber and the second chamber are separated by a first separating element, and the first chamber comprises at least one compressor rotor.
  • the turbo compressor may be a radial (centrifugal) turbo compressor.
  • the first process fluid and the second process fluid comprise hydrogen.
  • leaking of the second process fluid into the first process fluid results only in a shift of the neon to hydrogen ratio without polluting the first process fluid, wherein particularly hydrogen may be separated from the first process fluid, thereby adjusting the composition to the predefined value.
  • the first process fluid (refrigerant) comprises or essentially consists of hydrogen and neon and is has a molecular mass in the range of 3.88 g*mol -1 to 13 g*mol -1 . In certain embodiments, the first process fluid comprises or essentially consists hydrogen and neon and has a molecular mass in the range of 6.5 g*mol -1 to 11.2 g*mol -1 .
  • the process further comprises removing from the first process fluid (refrigerant) at least one component of the second process fluid (first seal gas), (preferably hydrogen) that leaked from the second process fluid into the first process fluid in the compression step.
  • first process fluid refrigerant
  • first seal gas preferably hydrogen
  • the second process fluid essentially consists of hydrogen.
  • the hydrogen that has leaked from the second process fluid into the first process fluid during compression of the first process fluid may be removed from the first process fluid.
  • the second process fluid (first seal gas) that has leaked into the first process fluid (refrigerant) during compression of the refrigerant, may be removed from the first process fluid.
  • the method may further comprise the step of providing a third process fluid, preferable comprising or essentially consisting of hydrogen or nitrogen, in a third chamber with a third pressure.
  • the third pressure may be between the ambient pressure and the second pressure, or above the second pressure.
  • the third pressure may be between ambient pressure and the second pressure.
  • the second process fluid may leak into the first process fluid or into the third process fluid.
  • the third pressure is above the second pressure.
  • the third process fluid acts or is designed to serve as an additional seal fluid. Accordingly, the first process fluid is sealed by two pressure gradients.
  • the third chamber is comprised within the above mentioned turbo compressor, wherein the third chamber is separated from the second chamber by a second separating element.
  • the method may further comprise the step of providing a fourth process fluid, preferably comprising or essentially consisting of nitrogen, in a fourth chamber with a fourth pressure, wherein particularly the fourth pressure lies between the third pressure and the ambient pressure.
  • a fourth process fluid preferably comprising or essentially consisting of nitrogen
  • the fourth chamber is comprised within the above mentioned turbo compressor, wherein the fourth chamber is separated from the third chamber by a third separating element.
  • the method may further comprise the steps of
  • the process parameter(s) which is/are adjusted may be one or more of the following:
  • the compression performance may be adjusted via the rotational speed of the compressor.
  • the step of adjusting the process parameter may be performed automatically.
  • the compressed first process fluid may be used as a refrigerant, particularly in a cryogenic cooling cycle.
  • cryogenic cooling cycles is comprised within a process for liquefying hydrogen or helium.
  • a process for liquefying hydrogen or helium comprises the steps of:
  • the feed gas stream may be provided with a pressure of at least 15 bar (a).
  • the feed gas stream may be provided with an initial temperature and precooled to intermediate temperature, particularly in the range of 70 K to 150°K, before being cooled by the first refrigerant stream.
  • the feed gas stream may be cooled by the first refrigerant stream to a first temperature, particularly from the intermediate temperature.
  • the feed gas stream may be further cooled by a second refrigerant stream from the first temperature to a temperature below the critical temperature of hydrogen or helium, particularly below 24 K, and optionally expanded the cooled feed gas stream, yielding a liquid product stream comprising hydrogen or helium.
  • a second refrigerant stream may be provided which comprises or consists of hydrogen and is expanded, thereby producing cold
  • the feed gas stream may have hydrogen concentration of at least 99.99 Vol.%.
  • ortho hydrogen comprised within the feed gas stream (about 75%) is converted to higher para hydrogen fractions preferably before liquefaction of the feed gas stream to avoid that the exothermic ortho to para reaction takes place in the liquid product possibly resulting in an undesired partial vaporization of the liquid hydrogen product during storage and transport.
  • the first temperature may lie in the range of 24.6 K to 44.5 K, particularly in the range of 26 K to 33 K.
  • the feed gas stream may be precooled to an intermediate temperature in the range of 80 K to 120 K, particularly 100 K, yielding the precooled feed gas stream, and the precooled feed gas stream is brought into contact with a catalyst being able to catalyse the ortho to para conversion of hydrogen, particularly before the first cooling step.
  • the catalyst may be or may comprise hydrous ferric oxide.
  • the catalyst is arranged within a heat exchanger, in which the feed gas stream is precooled.
  • the first cooling cycle may comprise the steps of:
  • the first refrigerant stream equates to the first process fluid of the method compressing and controlling a gas mixtures comprising neon.
  • directly heat transfer in the context of the present invention refers to the heat transfer between at least two fluid streams that are spatially separated such that the at least two fluid streams do not merge or mix but are in thermal contact, e.g. two fluid streams are guided through two cavities, for example of a plate heat exchanger, wherein the cavities are separated from each other by a wall or plate, and both streams do not mix, but heat can be transferred via the wall or the plate.
  • the first expansion device and/or the second expansion device may comprise at least one turbo-expander.
  • a partial stream may be separated from the first refrigerant stream, particularly additionally to the aforementioned first and second partial stream.
  • a partial stream may be expanded, optionally cooled, and separated into a neon rich partial stream and a hydrogen rich partial stream.
  • the neon rich partial stream may be recycled into the first refrigerant stream or the expanded refrigerant stream.
  • the neon rich partial stream may be stored.
  • a refrigerant turbo compressor comprises
  • a turbo compressor provided with third and fourth chambers, which in use are supplied with gas seal flow, provides significant operational advantages over known turbo compressors.
  • the provisional of additional seal gas filled chamber provides an additional seal for the inner chambers, which achieves the overall result that the gas mixture to be compressed is more effectively sealed and leakage of this gas mixture, in particular the expensive neon component is reduced. This means that the inventory loss can be minimised.
  • the rotating element is a shaft, particularly the drive shaft of the turbo compressor.
  • the turbo compressor is a radial (centrifugal) turbo compressor.
  • the above described turbo compressor is designed or configured to perform the process of the invention for compressing and controlling a gas mixtures comprising neon, or the process of the invention for liquefying hydrogen or helium according to the above aspects or embodiments of the invention.
  • the fourth chamber is separated from the ambient environment by a fourth separating element and in fluidic connection by a fourth opening in the fourth separating element with the ambient environment, wherein the rotating element extends through the fourth opening.
  • the embodiments described below relate to a process to compress and control a refrigerant gas mixture composition comprising neon in a cryogenic refrigerant cycle.
  • the embodiments relate a process to produce liquid hydrogen or helium.
  • FIG. 1 An embodiment of the process of the invention can be understood from figure 1 .
  • Figure 1 shows an embodiment of process for compressing and controlling a refrigerant gas mixture, where the compressed gas mixture is used in a cryogenic refrigeration cycle.
  • Figure 1 shows a refrigeration circuit for compressing a refrigerant 21, 22.
  • the refrigerant circuit comprises a compression device 11, a water cooling device 12, turbo expanders 13, 14, a precooling heat exchanger 17, and a cooling (main) heat exchanger 18.
  • the precooling heat exchanger 17 is supplied with a precooling refrigerant 51, 52.
  • the main heat exchanger 18 is also supplied with a second refrigerant stream 31, 32.
  • the second refrigerant stream may comprise hydrogen, or any other suitable refrigerant.
  • the compression device 11 is a centrifugal refrigerant compressor.
  • a particularly advantageous embodiment of a compressor is described below with reference to Figure 2 .
  • the feed stream to be liquefied 41 is passed firstly through the precooling heat exchanger 17, through adsorber vessels 19, 20 to form a precooled feed stream 42.
  • the precooled feed stream 42 is then conveyed through the main cooling heat exchanger 18 to produce cooled, liquefied feed stream.
  • the feed stream is taken to be hydrogen. It will be understood the arrangement of Figure 1 can be used to liquefy/cool other other feed streams, for example helium.
  • the composition of the first process fluid 21 or the compressed process fluid 22 (i.e. the composition of the refrigerant), is monitored after compression or at any suitable point of the above mentioned refrigerant cycle. If a deviation of the refrigerant composition from a predefined value or range is present, a process parameter is adjusted.
  • the process parameter may be the pressure or the temperature of the first process fluid 21 or the compressed first process fluid 22, or a parameter of the compressor used for the compressing.
  • the composition of the refrigerant 21, 22 may be adjusted in case of a deviation from a predefined value. For example, this can be advantageously achieved by separating hydrogen that has leaked into the refrigerant (first process fluid 21 or the compressed first process fluid 22) from the first seal gas (second process fluid) 33 during compression of the refrigerant21.
  • gas a mixture comprising mainly hydrogen and neon is used as the refrigerant (first process fluid) 21, with a molar mass between 3.83 g per mol and 13 g per mol, particularly for a hydrogen neon mixture with a molar mass between 6.5 g per mol and 11.2 g per mol.
  • mixture compositions represent an optimised solution between:
  • An arrangement or device for monitoring and adjusting the refrigerant gas mixture is provided.
  • the gas composition or volumetric fraction of at least one constituent of the refrigerant gas mixture (first process fluid 21 or compressed first process fluid 22) is determined in at least one location within the refrigeration process cycle.
  • key process parameters are modified correspondingly.
  • the refrigeration cycle process temperature at the cold end can be varied depending on the measured neon mixture fraction of the first process fluid 21 (can be measured, for example, at the suction of the centrifugal refrigerant compressor 11 or at the inlet or outlet of turbo expander 14) to avoid two-phase turbine discharge by e.g. manipulating the high/low gas pressure levels of the refrigeration cycle.
  • rotational speed(s) of the centrifugal refrigerant compressor 11 can be monitored and adjusted, if required, in function of the determined volumetric fraction e.g. if the hydrogen fraction is increased.
  • the pressure ratios at the inlet and outlet of the centrifugal refrigeration compressor 11 and turbo expanders 13, 14 can thus be shifted in order to adapt the operating point to the changing process gas mixture (first process fluid 21 or compressed first process fluid 22) composition.
  • the pressure ratio of the refrigeration cycle (HP to LP) can be adapted in function of the process gas mixture (first process fluid 21 or compressed first process fluid 22), if the composition of the mixture varies significantly due to the leakage of compressor seal gas 33 (hydrogen) into the process gas mixture (first process fluid 21 or compressed first process fluid 22).
  • these adjustments are performed automatically.
  • the device for monitoring and adjusting the process of the invention or the centrifugal refrigerant compressor 11 serves to compensate fluctuations in the hydrogen content within the process gas mixture (first process fluid 21 or compressed first process fluid 22).
  • a required high-pressure refrigerant stream 25, preferably comprising neon and hydrogen, is drawn continuously or intermittently from the refrigeration cycle at cryogenic temperature (e.g. in the range of 50 K to 26 K), for example, by opening / closing of a regulating valve or other suitable flow control device.
  • the flow of the high-pressure refrigerant stream 25 can be controlled by measuring the neon or hydrogen refrigerant fraction (gas mixture composition) and then adjusting the flow rate through stream 25.
  • the high-pressure refrigerant stream 25 (neon recovery stream) is taken from a high-pressure line 22 upstream of the coldest turbo expander 14.
  • the high-pressure refrigerant stream (neon recovery stream 25) is further cooled down in the heat exchanger 18 to a temperature below the critical point of pure neon (44.5 K), particularly below 35 K. In alternative embodiments (not shown), the high pressure refrigerant stream 25 is not cooled in the heat exchanger 18.
  • the high-pressure refrigerant stream 25 is expanded and cooled in a Joule-Thomson throttle valve 15 to produce an expanded stream 26.
  • the expanded stream's 26 temperature is constrained by the gas mixture freezing point, which when neon is present, is close to the triple point of neon (24.6 K) or slightly below, depending on the hydrogen fraction.
  • the high-pressure refrigerant stream (recovery stream) 25 flow rate as well as the low pressure downstream of the throttle valve 15 can be adjusted depending on monitored process conditions; depending on the designed refrigerant mixture composition (hydrogen-neon), and the volume of gas (hydrogen) that has to be removed/recovered (in function of seal gas leakage into process).
  • a hydrogen flow 28 of 3 Nm 3 /h can be extracted from the cycle at cryogenic temperature to keep the refrigerant mixture composition 21, 22 within a defined range.
  • this is achieve by passing the high-pressure refrigerant stream (recovery stream) 25 through at least one cryogenic vapor-liquid separation stage in a hydrogen-neon mixture phase separator 16.
  • the expanded stream 26 downstream of the throttle valve 15 enters the phase separator 16 in a two-phase flow condition.
  • a neon-rich liquid 27 can be drawn out at the bottom of the phase separator; a hydrogen-rich vapor 28 is extracted at the top of the phase separator.
  • 3 Nm 3 /h hydrogen are extracted from the top of the phase separator 16.
  • the required mass flow of approximately of a 50 mol.%-50 mol.% hydrogen-neon refrigerant mixture 25 is separated from the process cycle in the high pressure line at e.g. 25 bar(a).
  • the separated stream 25 is cooled to a temperature (e.g. 32 K) and is then expanded in an isenthalpic throttle valve 15 to a suitable pressure, for example below 5 bar(a) or a temperature close to or below 26 K.
  • the hydrogen-rich vapor 28 at the top of the separator vessel 16 is composed of approximately or above 80 mol. % hydrogen and approximately or below 20 mol. % neon.
  • the neon-rich liquid 27 at the bottom of the separator vessel 16 is composed of above 80 mol.% neon and below 20 mol.% hydrogen.
  • the hydrogen-rich vapor stream 28, corresponding to a pure hydrogen flow of approximately 3 Nm 3 /h, can be removed from the process to balance out the refrigerant mixture composition 21, 22 in the cycle.
  • the hydrogen-rich vapor stream 28 can be vented or stored in a buffer tank for hydrogen recovery or used, for instance, as a source for the seal gas 33, 34.
  • the hydrogen-rich vapor 28 can be further cooled, expanded and guided to a second liquid-vapor phase separator stage to further reduce the quantity of neon loss.
  • the neon-rich liquid 27 can be used to recover the expensive neon and can be, for instance, routed back directly into the low pressure line 21 of the hydrogen-neon mixture cycle or can be stored in a buffer tank for neon recovery/make up. In this manner, a substantial reduction in continuous neon inventory losses can be achieved, below a total of 1 Nm 3 /h, particularly below 0.5 Nm 3 /h, compared to the significantly higher leakage losses with conventional double seal gas systems (approximately up to 10 Nm 3 /h per compressor stage).
  • a nitrogen separation can be performed using a vapour-liquid phase separator with subsequent nitrogen absorber(s) in the refrigeration cycle above the melting point of nitrogen at 63 K particularly in order to avoid freeze out of nitrogen.
  • the compressor 11 that can be used for this purpose is preferably a centrifugal (radial) turbo compressor, more particularly an integrally-geared centrifugal turbo compressor.
  • the compressor 11 is designed with up to 10 compressor stages, more particularly with up to 8 compressor stages with interstage cooling after at least every second compressor stage.
  • the compressor 11 is preferably a high-speed compressor that can run at high compressor blade tip speeds, particularly up to 650 m/s.
  • the feasible compressor stage pressure ratio is dependent on the mentioned fluid or fluid mixture composition and rotational speed: preferably stage pressure ratios of at least 1.15, and particularly between 1.2 and 1.4.
  • the compressor is used for comparatively large gas volumes and a total compressor power above 1 000 kW at coupling, particularly for larger compressors above 5'000 kW coupling power.
  • the compressor 11 comprises a first chamber 68 and, in this first chamber 68 there is a compressor rotor 61.
  • the refrigerant compressor 11 includes a second chamber 69, which is separated from the first chamber 68 by a first separating element 64a having a first opening 64b.
  • the first chamber 68 is supplied with and substantially filled with the refrigerant gas or refrigerant gas mixture 21.
  • the refrigerant 21 may comprise: hydrogen, neon, helium or a mixture of these, preferably a gas mixture of hydrogen and neon.
  • the refrigerant gas 21 for example a mixture of hydrogen and neon
  • the second chamber 69 is supplied and filled with a first seal gas 33.
  • the first seal gas 33 is preferably hydrogen 33 for a hydrogen-neon compressor 11.
  • the first seal gas may comprise hydrogen, helium, neon, nitrogen or a gas mixture of these fluids depending on the refrigerant gas 21 to be compressed.
  • the pressure p2 in the second chamber 69 is higher than the gas pressure p1 in the first chamber 68, as a result of which a seal gas sealing is realized. In this way, it is ensured that the refrigerant gas (or refrigerant gas mixture) 21 in the first chamber 68 cannot flow through the opening 64b of the first separating element 64a. Given that only the first seal gas 33, e.g.
  • This arrangement means that the refrigerant compressor 11 can be operated with high rotational speeds and at comparatively high efficiencies.
  • the refrigerant compressor 11 includes a third chamber 70, which is separated from the second chamber 69 by a second separating element 65a with a second opening 65b.
  • a second seal gas (a third process fluid) 34 In the third chamber 70, there is a second seal gas (a third process fluid) 34.
  • the second seal gas 34 preferably substantially consists of nitrogen.
  • the second seal gas 34 pressure p3 is higher than atmospheric pressure and lower than the first seal gas 33 pressure.
  • the compressor 11 also includes a fourth chamber 71, separated from the third chamber 70 by a third separating element 66a having a third opening 66b.
  • the fourth chamber 70 is supplied with a third seal gas 35.
  • the fourth chamber 71 is substantially filled with nitrogen as a third seal gas. It is thereby achieved that between the second chamber 69 and the environment there is still at least one further chamber 70, 71, in which the gas can be used to realize an additional seal of the second chamber 69 and thus also of the first space or chamber 68 from the environment. Furthermore, the fourth chamber 71 is separated from the environment by a fourth separating element 67a with a fourth opening 67b.
  • the compressor 11 of Figure 2 further comprises a rotating element 62, particularly a drive shaft of the compressor, wherein the rotating element 62 is connected to the compressor rotor 61.
  • the rotating element 62 extends through the first opening 64b of the first separating element 65a and further to a second opening 65b of the second separating element 65a; through the third opening 66b of the third separating element 66a and the fourth opening 67b of the fourth separating opening 67a.
  • turbo compressor 11 of Figure 2 The operation of the turbo compressor 11 of Figure 2 will now be described with reference to exemplary process fluids.
  • the first process fluid (refrigerant) 21 comprises or essentially consists of neon and hydrogen is compressed in the first chamber 68 to a compressed first process fluid (compressed refrigerant) 22 with a first pressure.
  • the first chamber 68 is non-hermitically separated from the second chamber 69 which filled with a second process fluid (first seal gas) 33 comprising or essentially consisting of hydrogen.
  • the second process fluid (first seal gas) 33 is provided with a second pressure being larger than the first pressure.
  • the second process fluid 33 acts as a seal gas, which means that the first process fluid 21 cannot leak out of the first chamber 68 during compression, and whereby only hydrogen of the second process fluid 33 may leak into the first chamber 68 and the first process fluid 21 or the compressed first process fluid 22, respectively.
  • the compressed first process fluid 22 can be used as a refrigerant in a refrigerant cycle (as shown in Figure 1 ).
  • the second process fluid 33 is preferably sealed from the environment by the third process fluid (second seal gas) 34 comprised within a third chamber 70 that is non-hermetically separated from the second chamber 69 and in fluidic connection with the second chamber 69.
  • the third process fluid 34 preferably comprises or consists of nitrogen with a third pressure lying between the second pressure and the ambient pressure. Accordingly, the second process fluid 33 may leak into the first process fluid 21 or the third process fluid 34 during compression of the first process fluid 21.
  • the third process fluid 34 comprises or essentially consists of hydrogen and is provided with a third pressure being larger than the second pressure.
  • first process fluid 21 is effectively sealed by the second process fluid 33 and third process fluid 34 during compression, whereby the possibility of leakage of the first process fluid 21 can be further decreased.
  • the third process fluid 34 is sealed from the environment by the fourth process fluid (third seal gas) 35 comprising or essentially consisting of nitrogen, wherein the fourth process fluid 35 is comprised within a fourth chamber 71 being non-hermetically separated from the third chamber 70 and being in fluidic connection with the third chamber 70.
  • the second process fluid 33 may comprise a mixture of neon and hydrogen instead of hydrogen only in order to reduce the potential dilution of the refrigerant 21 by hydrogen.
  • a process for compressing a refrigerant gas and controlling the designed refrigerant gas composition during operation can be advantageously performed, in particular for a cryogenic refrigerant cycle for hydrogen and helium liquefiers/refrigerators, particularly for a refrigerant gas involving a gas mixture comprising neon, and particularly for a hydrogen-neon mixture.
  • a refrigerant gas (preferably a mixture of hydrogen and neon) is compressed in a compression device having at least one gas seal (for example the turbo compressor 11) at high-speed, and the compressed refrigerant is maintained at a consistent, desired composition.
  • the high quality compressed refrigerant can be used as a cryogenic refrigerant, while keeping the continuous losses of expensive gas (i.e. neon) inventory to a minimum and thus allowing the economically viable use of this refrigeration process for cryogenic applications, for example, in the production of liquid hydrogen or refrigeration of helium.
  • the method of the invention can also be applied to the compression of refrigerant gas in other compression devices in which seal gas(es) are provided and where therefore leakage of the seal gas(es) into the refrigerant gas flow may occur.
  • the compression device may be a turbocompressor having two chambers, with a single seal gas supplied to the second chamber.
  • the compression device may be a turbocompressor having three chambers, with two seal gases (which may be the same or different) being supplied to the second and third chambers.

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EP16206671.6A 2016-12-23 2016-12-23 Procédé de compression d'un mélange de gaz comprenant néon Withdrawn EP3339605A1 (fr)

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EP16206671.6A EP3339605A1 (fr) 2016-12-23 2016-12-23 Procédé de compression d'un mélange de gaz comprenant néon
PCT/EP2017/084417 WO2018115456A1 (fr) 2016-12-23 2017-12-22 Procédé de compression et de commande d'une composition de mélange gazeux destinée à être utilisée dans un cycle de réfrigération cryogénique

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FR3119883A1 (fr) 2021-02-18 2022-08-19 L'air, Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de liquéfaction d’hydrogène

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JP7450798B2 (ja) * 2020-07-13 2024-03-15 ゼロ・エミッション・インダストリーズ，インク． 気体燃料供給システム
US11391511B1 (en) 2021-01-10 2022-07-19 JTurbo Engineering & Technology, LLC Methods and systems for hydrogen liquefaction

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EP2211124A1 (fr) * 2007-11-19 2010-07-28 IHI Corporation Réfrigérateur cryogénique et son procédé de commande
US20090151391A1 (en) * 2007-12-12 2009-06-18 Conocophillips Company Lng facility employing a heavies enriching stream
US20100254811A1 (en) * 2009-04-06 2010-10-07 Dresser-Rand Co. Dry gas blow down seal
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WO2018219964A1 (fr) * 2017-05-30 2018-12-06 Linde Ag Système de circuit de réfrigération et procédé d'entretien d'un joint étanche au gaz d'un système de compresseur
FR3119883A1 (fr) 2021-02-18 2022-08-19 L'air, Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de liquéfaction d’hydrogène
WO2022175204A1 (fr) 2021-02-18 2022-08-25 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de liquéfaction d'hydrogène

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