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EP4575301A1 - Dispositif et procédé de compression de gaz d'évaporation - Google Patents

Dispositif et procédé de compression de gaz d'évaporation Download PDF

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Publication number
EP4575301A1
EP4575301A1 EP23219436.5A EP23219436A EP4575301A1 EP 4575301 A1 EP4575301 A1 EP 4575301A1 EP 23219436 A EP23219436 A EP 23219436A EP 4575301 A1 EP4575301 A1 EP 4575301A1
Authority
EP
European Patent Office
Prior art keywords
gas
compressor stage
heat exchanger
exhaust
compressed
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP23219436.5A
Other languages
German (de)
English (en)
Inventor
Torsten Kirchhoff
Fabrizio Botta
Thorsten Harder
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.)
Burckhardt Compression AG
Original Assignee
Burckhardt Compression AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Burckhardt Compression AG filed Critical Burckhardt Compression AG
Priority to EP23219436.5A priority Critical patent/EP4575301A1/fr
Priority to PCT/EP2024/086449 priority patent/WO2025132147A1/fr
Publication of EP4575301A1 publication Critical patent/EP4575301A1/fr
Pending legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F17C9/04—Recovery of thermal energy
    • 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
    • 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
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • 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
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F25J1/0015—Nitrogen
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    • 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
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    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F25J1/0017—Oxygen
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    • 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
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    • F25J1/002—Argon
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    • 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
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    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F25J1/0025—Boil-off gases "BOG" from storages
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    • 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
    • F25J1/02—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
    • F25J1/0201—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 only internal refrigeration means, i.e. without external refrigeration
    • F25J1/0202—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 only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal 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
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    • 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
    • F25J1/0247—Different modes, i.e. 'runs', of operation; Process control start-up of the process
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    • 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.
    • F25J1/0296—Removal of the heat of compression, e.g. within an inter- or afterstage-cooler against an ambient heat sink
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    • F17C2223/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
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    • F17C2265/032—Treating the boil-off by recovery
    • F17C2265/038—Treating the boil-off by recovery with expanding
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/90—Boil-off gas from storage

Definitions

  • the present invention relates to a device and a method for compressing evaporation gas of a cryogenically stored gas.
  • Facilities that process or consume large quantities of gas are typically supplied with liquefied gas stored at cryogenic temperatures, as this is easier to transport and deliver than large quantities of compressed gas.
  • liquid gas maintained at low temperatures presents the problem that, even when properly stored in a suitable storage vessel, the gas warms up and vaporizes due to heat from the environment, leading to a continuous increase in the pressure in the storage vessel.
  • the vaporized gas also known as boil-off gas (BOG)
  • BOG boil-off gas
  • the pressure of the boil-off gas accumulating in the storage vessels is increased in suitable devices before the boil-off gas is supplied to a consumer.
  • the state-of-the-art devices for compressing exhaust gas which are used, for example, in natural gas and hydrogen compressor stations, typically operate with gas inlet temperatures. which are in the range of ambient temperature or down to approximately -40 °C or even -160 °C, and thus significantly warmer than -196 °C.
  • the gas inlet temperature into the compressor is adjusted using preheating systems.
  • the energy required to raise the temperature of the exhaust gas in the preheating systems is obtained, for example, by extracting heat from the environment or using an electrical preheating device.
  • such devices have the disadvantage of being energy-intensive and wasting the cold contained in the exhaust gas.
  • the present invention is based on the object of mitigating or even eliminating these and other disadvantages of the prior art and providing a device of the type mentioned above, which is characterized by higher compression and energy efficiency, enables lower complexity and thus greater operational readiness, and in which the use of cost-intensive materials, which are particularly stable at low temperatures, in particular at temperatures below approximately -196 °C, can be dispensed with. It is a further object of the present invention to provide a method for compressing evaporation gas from a cryogenically stored gas, which has higher compression and energy efficiency than the methods known from the prior art and does not require the use of expensive low-temperature-resistant materials.
  • a device for compressing evaporation gas of a cryogenically stored gas comprises a container for cryogenic stored gas, which has an outlet for discharging an exhaust evaporation gas of the cryogenically stored gas that can be provided in the container.
  • the device further comprises a compressor with at least one compressor stage, preferably at least two compressor stages, and a heat exchanger for carrying out a heat exchange between the exhaust evaporation gas and an exhaust evaporation gas compressed in the first compressor stage.
  • the heat exchanger has a first inlet for receiving the exhaust evaporation gas, a first outlet for discharging a heated exhaust evaporation gas to the first compressor stage, a second inlet for receiving the exhaust evaporation gas compressed in the first compressor stage, and a second outlet for discharging a cooled and compressed exhaust evaporation gas to a downstream process, in particular to a consumer.
  • the downstream process can in particular be the second compressor stage of the compressor.
  • the second compressor stage is designed to further compress the exhaust gas compressed in the first compressor stage and cooled in the heat exchanger, in order to provide a further compressed exhaust gas.
  • such a device In contrast to the prior art devices for compressing exhaust gas, such a device is characterized by the fact that it operates a purely compressor-internal cooling management system. In other words, the cold of the exhaust gas and the heat generated during compression in the first compressor stage are not transferred to other processes but are used exclusively for gas cooling in the compressor system. Because the cold of the exhaust gas is not transferred to preheaters but to gas pre-compressed in the first compressor stage, the available process cooling is not wasted and the energy efficiency of the compressor system is optimized. On the other hand, the efficiency of the The efficiency of this device is also increased because the procurement and operation of a preheater with an external heat source is no longer necessary, and the energy for preheating the exhaust steam gas does not have to be used separately, as it is provided by the first compressor stage.
  • a further advantage of such a device is that the compressor, and in particular the first compressor stage of the compressor, is not exposed to the low temperatures of the exhaust steam gas. This is particularly relevant for gases whose boiling point is lower than the boiling point of nitrogen, as the materials commonly used in compressors cannot withstand temperatures below approximately -196 °C or are very expensive. This means that these very expensive materials, which also function at very cold exhaust steam gas temperatures, can be dispensed with in the design of compressors.
  • the container for cryogenically stored gas, the heat exchanger, and the at least one compressor stage, preferably the at least two compressor stages, of the compressor are fluidically connected to one another, so that exhaust gas from the container can be fed via the heat exchanger to the first compressor stage.
  • the first compressor stage and the heat exchanger are fluidically connected to one another such that the exhaust gas compressed in the first compressor stage can be fed directly to the second inlet of the heat exchanger.
  • the exhaust gas compressed in the first compressor stage can then be fed via the heat exchanger to the downstream process, in particular to the second compressor stage.
  • One or more further compressor stages can be connected to the second compressor stage. the same compressor or another compressor.
  • a "further compressor stage” is understood to mean a compressor stage designed to increase the pressure of the gas supplied to it.
  • the container is suitable for the cryogenic storage of gas selected from the group consisting of hydrogen, nitrogen, helium, neon, krypton, argon, liquefied natural gas, oxygen, and mixtures thereof.
  • the cryogenically stored gas is selected from the group consisting of hydrogen, helium, neon, and mixtures thereof. Due to the very low boiling points of hydrogen (-252 °C), helium (-269 °C), and neon (-246 °C) at atmospheric pressure, the advantages of the device according to the invention are particularly evident when used with these gases, since the use of the usually required, low-temperature-resistant and expensive materials, particularly for the compressor, can be dispensed with.
  • the cryogenically stored gas is particularly preferably hydrogen.
  • the heat exchanger is a countercurrent heat exchanger. Due to the flow in opposite directions, there is always a temperature gradient between the material flows, i.e., between the exhaust steam gas and the exhaust steam gas compressed in the first compressor stage, so that almost the entire amount of heat can be transferred from one material flow, i.e., the exhaust steam gas compressed in the first compressor stage, to the other, i.e., the exhaust steam gas. Countercurrent exchange is thus significantly more effective and cost-effective. and due to the associated energy savings, it is also more environmentally friendly than direct current.
  • the heat exchanger is preferably a diffusion-welded counterflow heat exchanger.
  • Diffusion-welded heat exchangers printed circuit heat exchangers; PCHEs
  • PCHEs printed circuit heat exchangers
  • diffusion-welded heat exchangers can be cooled down within a relatively short time, which is particularly advantageous during start-up of the process described in more detail below.
  • diffusion-welded heat exchangers are characterized by a very wide performance window compared to conventional shell-and-tube heat exchangers and significantly greater resistance to temperature fluctuations and the effects of thermal fatigue. The latter leads to a reduction in the overall costs associated with repair and maintenance.
  • the temperature of the gas exiting the heat exchanger should not be lower than the temperature at which nitrogen and/or oxygen condense. Rapid cooling of the heat exchanger is therefore advantageous, as it shortens the time until the process can begin.
  • a first valve is arranged downstream of the first outlet of the heat exchanger and upstream of the first compressor stage. This first valve is designed to feed the heated exhaust gas to the second compressor stage. Due to the parallel connection of the The first and second compressor stages, for example, make it possible for the first compressor stage to be serviced without the need to temporarily store or dispose of the exhaust gas that still accumulates in the vessel.
  • the first valve can be arranged in the line fluidically connecting the second outlet of the heat exchanger and the second compressor stage.
  • the first valve is fluidically connected to the first outlet of the heat exchanger via a first line branching off from the line connecting the first outlet of the heat exchanger to the first compressor stage.
  • the first outlet of the heat exchanger is or can be fluidly connected to the vessel via a bypass line arranged downstream of the first compressor stage and/or downstream of the second compressor stage.
  • a bypass line makes it possible to return compressed exhaust evaporation gas to the vessel without using compressed exhaust evaporation gas in the first and/or second compressor stage to heat fresh exhaust evaporation gas from the vessel in the heat exchanger. This is particularly advantageous when starting up the process described in more detail below.
  • the first outlet of the heat exchanger is fluidically connected or connectable to the container via a bypass line arranged downstream of the first compressor stage and/or downstream of the second compressor stage, wherein a second valve is arranged downstream of the first compressor stage and upstream of the second inlet of the heat exchanger.
  • This second valve is configured to instead of feeding it to the second inlet of the heat exchanger of the bypass line.
  • a bypass line makes it possible to return compressed exhaust evaporation gas to the vessel without exhaust evaporation gas compressed in the first and/or second compressor stage being used to heat fresh exhaust evaporation gas from the vessel in the heat exchanger. This is particularly advantageous when starting up the process described in more detail below.
  • the exhaust evaporation gas compressed in the first compressor stage is preferably fed into the bypass line downstream of the second compressor stage via a line which opens downstream of the second compressor stage.
  • the bypass line can have a reliquefaction device for previously compressed evaporation gas.
  • the reliquefaction device allows evaporation gas to be returned to the container in cryogenic form if it is not taken up by a consumer after compression.
  • the reliquefaction device can, in particular, be a throttle valve.
  • the container for cryogenically stored gas is a mobile cryogenic tank, a storage tank of a liquefaction plant, or a storage tank of a transshipment terminal.
  • the compressor further comprises at least one further compressor stage, which is or can be fluidically connected to the first compressor stage and/or the second compressor stage.
  • the further compressor stage is configured to compress the exhaust gas compressed in the first compressor stage and cooled in the heat exchanger. This allows the second compressor stage to be shut down, for example, for maintenance purposes.
  • the additional compressor stage is configured to further compress the exhaust gas further compressed in the second compressor stage to provide an even more compressed exhaust gas. The presence of an additional compressor stage increases the operational flexibility of the device, since it can be used to provide an even more compressed exhaust gas, for example, depending on the pressure requirements of different consumers.
  • the exhaust gas is heated before its compression in step a) in the heat exchanger by heat exchange with the exhaust gas compressed in the first compressor stage in order to obtain a heated exhaust gas.
  • step b) the exhaust evaporation gas compressed in the first compressor stage is cooled in the heat exchanger by heat exchange with the exhaust evaporation gas which is generated in the vessel and is to be compressed in the first compressor stage.
  • the method according to the invention can be carried out in particular with a device as described herein, whereby the advantages described for the corresponding device are additionally achieved.
  • the cryogenically stored gas is selected from the group consisting of hydrogen, nitrogen, helium, neon, krypton, argon, liquefied natural gas, oxygen, and mixtures thereof.
  • the cryogenically stored gas is selected from the group consisting of hydrogen, helium, neon, and mixtures thereof.
  • the cryogenically stored gas is hydrogen.
  • the heat exchange between the exhaust steam gas and the exhaust steam gas compressed in the first compressor stage takes place according to the countercurrent principle.
  • the heat exchange between the exhaust steam gas and the exhaust steam gas compressed in the first compressor stage takes place using a diffusion-welded heat exchanger. This allows the advantages described in connection with the corresponding embodiments of the device disclosed herein to be achieved.
  • the exhaust gas should be heated to temperatures higher than the temperatures at which nitrogen and/or oxygen condense. Since heat is generated during gas compression, and higher temperatures can also have a detrimental effect on compressor efficiency and the materials used in the compressor, compression of the coolest gas possible should be attempted.
  • the exhaust gas accumulating in the vessel has a temperature between -272 °C and -160 °C.
  • the exhaust gas heated by heat exchange has a temperature between -196 °C and -120 °C before its compression in step a), i.e. before its compression in the first compression stage of the multi-stage compressor.
  • the use of particularly low-temperature-stable and therefore expensive materials in the compressor can be dispensed with.
  • the nevertheless low temperature range is also advantageous for the compression of an exhaust gas, as it improves the efficiency of the compression process and helps to manage the heat generated during compression. This is crucial for achieving higher compression ratios and reducing thermal stress on the compressor components, which can extend their service life.
  • the exhaust gas heated by heat exchange has a temperature between -180 °C and -140 °C before its compression in the first compressor stage of the single- or multi-stage compressor.
  • This temperature range is particularly preferred, in particular in the case that the cryogenically stored gas is hydrogen, since on the one hand the use of expensive materials can be avoided and, on the other hand, the efficiency of the first compressor stage remains high.
  • the exhaust gas compressed in the first compressor stage and cooled in the heat exchanger in step b) is provided to the second compressor stage at a temperature between -170 °C and -60 °C. Efficient compression can be achieved by the second compressor stage in this temperature range.
  • the further compressed exhaust gas i.e., the exhaust gas obtained from the second compressor stage, is further compressed in at least one additional compressor stage.
  • this increases the flexibility of the process and provides exhaust gas with the final pressure required by the respective customer.
  • Typical final pressures required by typical customers for compressed steam gas are: between 30 bar and 100 bar, in particular around 60 bar, for pipeline injection; between 350 bar and 800 bar for trailer filling; between 16 bar and 25 bar for refineries; between 20 bar and 200 bar for ammonia synthesis; between 6 bar and 65 bar for fuel gas supply, in particular for liquid hydrogen gensets or fuel cell gas turbines.
  • the exhaust steam gas is used for a predetermined time to cool the heat exchanger before the exhaust steam gas is used in step b) to cool the exhaust steam gas compressed in the first compressor stage.
  • the exhaust steam gas flows through the heat exchanger and is subsequently compressed in the first compressor unit, without the exhaust steam gas compressed in the first compressor unit being fed to the heat exchanger for heat exchange with the exhaust steam gas for a predetermined time. This allows the heat exchanger to be cooled particularly quickly to the desired low temperature.
  • the predetermined time may be the time until a predetermined temperature is reached at a first inlet of the heat exchanger for receiving the exhaust evaporation gas.
  • the predetermined time may be the time until a predetermined temperature, in particular a temperature between -196°C and -120°C, is reached at a first outlet of the heat exchanger for discharging the heated exhaust evaporation gas to the first compressor stage. This ensures that the temperature of the exhaust evaporation gas supplied to the first compressor stage is compatible with the materials used in the first compressor stage of the compressor.
  • the exhaust gas is liquefied in a reliquefaction device and returned to the vessel after being compressed in at least one of the two compression stages of the compressor. Recycling the exhaust gas is particularly advantageous when no consumer is available for the compressed exhaust gas.
  • Figure 1a is a schematic representation of an embodiment of an apparatus for compressing evaporation gas of a cryogenically stored gas.
  • the device 100 comprises a container 10 for cryogenically stored gas LG.
  • evaporation gas 1 of the cryogen provided in the container is produced, which can leave the container 10 via outlet 11 of the container 10.
  • the device 100 further comprises a compressor 20 with a compressor stage 21 as well as a heat exchanger 30, wherein the heat exchanger 30 is designed to carry out a Heat exchange between the exhaust steam gas 1 and the exhaust steam gas 3 compressed in the first compressor stage 21.
  • the container 10 is fluidly connected to a first inlet 31 of the heat exchanger via the outlet 11.
  • the first inlet 31 of the heat exchanger 30 is correspondingly designed to receive the exhaust steam gas 1 and is in turn fluidly connected to a first outlet 32 of the heat exchanger 30.
  • the first outlet 32 of the heat exchanger 30 is fluidly connected to the first compressor stage 21 and is designed to discharge the exhaust steam gas 2, which has flowed through the heat exchanger 30, to the first compressor stage 21.
  • the first compressor stage 21 is in turn fluidly connected to a second inlet 33 of the heat exchanger 30, which is designed to receive the exhaust steam gas 3 compressed in the first compressor stage 21.
  • the second inlet 33 of the heat exchanger 30 is designed to receive the exhaust evaporation gas 3 compressed in the first compressor unit 21 and is in turn fluidly connected to a second outlet 34 of the heat exchanger 30.
  • the second outlet 34 of the heat exchanger 30 is in turn fluidly connected to a consumer 80 arranged downstream of the heat exchanger 30, i.e., a downstream process.
  • a further heat exchanger 60 can optionally be arranged between the second outlet 34 of the heat exchanger 30 and the consumer 80 in order to further temper, i.e., cool or heat, the exhaust evaporation gas 4 compressed in the first compressor stage 21 and cooled in the heat exchanger 30 before it is discharged to a consumer 80.
  • the gas cryogenically stored in the container 10 can, in particular, be hydrogen.
  • the pressure of the evaporation gas 1 in the head space of the container 10 can be between 1.01 and 20 bara, in particular about 8 bara.
  • Figure 1b is a schematic representation of another example of a device for compressing exhaust gas of a cryogenically stored gas.
  • the device 100 comprises a container 10 for cryogenically stored gas LG.
  • exhaust evaporation gas 1 of the cryogen provided in the container is produced, which can leave the container 10 via outlet 11 of the container 10.
  • the device 100 further comprises a compressor 20 with at least two compressor stages 21, 22 and a heat exchanger 30.
  • the container 10 is fluidly connected to a first inlet 31 of the heat exchanger via the outlet 11.
  • the first inlet 31 of the heat exchanger 30 is designed to receive the exhaust evaporation gas 1 and is in turn fluidly connected to a first outlet 32 of the heat exchanger 30.
  • the first outlet 32 of the heat exchanger 30 is fluidly connected to the first compressor stage 21 and is designed to discharge the exhaust evaporation gas 2, which has flowed through the heat exchanger 30, to the first compressor stage 21.
  • the first compressor stage 21 is in turn fluidly connected to a second inlet 33 of the heat exchanger 30, which is designed to receive the exhaust evaporation gas 3 compressed in the first compressor stage 21.
  • the second inlet 33 of the heat exchanger 30 is correspondingly designed to receive the exhaust evaporation gas 3 compressed in the first compressor unit 21 and is in turn fluidly connected to a second outlet 34 of the heat exchanger 30.
  • the second outlet 34 of the heat exchanger 30 is in turn fluidly connected to the second compressor stage 22 and is designed to discharge the exhaust evaporation gas 4, which has flowed through the heat exchanger 30, to the second compressor stage 22.
  • the heat exchanger 30 is thus designed to perform a heat exchange between the exhaust steam gas 1 and the exhaust steam gas 3 compressed in the first compressor stage 21.
  • the second compressor stage 22 is designed to further compress the exhaust steam gas 4 compressed in the first compressor stage 21 and cooled in the heat exchanger 30 to provide a further compressed exhaust steam gas 5.
  • Downstream A further heat exchanger 60 can optionally be arranged in the second compressor stage 22 to temper the exhaust evaporation gas 5 further compressed in the second compressor stage 22 before it is discharged to a consumer 80.
  • the gas cryogenically stored in the container 10 can be, in particular, hydrogen.
  • the pressure of the exhaust evaporation gas 1 in the headspace of the container 10 can be between 1.01 and 20 bara, in particular approximately 8 bara.
  • Figure 2 is a schematic representation of an example of another apparatus for compressing evaporation gas of a cryogenically stored gas.
  • the device 100 comprises, in addition to the elements already described in connection with the Figure 1 illustrated embodiment and their description also applies analogously to the embodiments shown in Figure 2 illustrated embodiment applies, further comprises a further compressor stage 23, which adjoins the second compressor stage 22 and is configured to further compress the exhaust evaporation gas 5 further compressed in the second compressor stage 22, in order to provide an even further compressed exhaust evaporation gas 6.
  • the further compressor stage 23 can - as indicated in Figure 2 by the dashed group with the reference number 20 - be part of the compressor, which also comprises the first and second compressor stages 21 and 22, respectively.
  • the illustrated embodiment of the device 100 further comprises a reliquefaction device 50, which is arranged in a bypass line 40 and is designed to liquefy previously compressed exhaust gas.
  • the bypass line 40 is fluidically connected to the container 10 in order to be able to return gaseous exhaust gas 7 or that has been reliquefied in the reliquefaction device 50 to the container 10.
  • bypass line 40 branches off after the heat exchanger 70 arranged downstream of the further compressor stage 23.
  • the bypass line branches off the exhaust steam gas flow at another point of the device 100, in particular after the heat exchanger 60 arranged downstream of the second compressor stage 22 and upstream of the optionally present further compressor stage 23.
  • Figure 3a is a schematic representation of the material flows during the start-up phase of a process for compressing exhaust gas according to an embodiment of the present invention.
  • a device 100 is used which, in addition to the devices already described in connection with the Figure 1b elements described in the embodiment shown, the description of which also applies analogously to the Figure 3a illustrated embodiment applies, further comprises a first valve 41, a second valve 42, a first line 43 branching off upstream of the first compressor stage 21 and a line 44 opening downstream of the second compressor stage 22.
  • the first valve 41 is arranged downstream of the first outlet 32 of the heat exchanger 30 and upstream of the first compressor stage 21 and is designed to supply heated exhaust gas from the heat exchanger 30 to the first compressor stage 21 and/or the second compressor stage 22.
  • the first valve 41 is arranged in the line which fluidically connects the second outlet 34 of the heat exchanger and the second compressor stage 22, and via a first line 43 which connects the first outlet 32 of the heat exchanger 30 with the first compressor stage 21 connecting line, fluidically connected to the first outlet 32 of the heat exchanger 30.
  • the second valve 42 is arranged downstream of the first compressor stage 21, more precisely in the line fluidically connecting the first compressor stage 21 with the second inlet 33 of the heat exchanger.
  • the second valve 42 is further fluidically connected to the device 100 via a second line 44 opening downstream of the second compressor stage 22.
  • the Figure 3a The device 100 used in the process shown further comprises an optional bypass line 90 with a valve 91 arranged therein, with which the likewise optional heat exchanger 60 can be bridged. This allows flash gas in the tank to be minimized if the outlet temperature of the exhaust evaporation gas compressed in the first and second compressor stages 21, 22 is lower than the temperature of the heat exchanger cooling medium in heat exchanger 60.
  • the material flows present when starting up the process, ie the path of the exhaust evaporation gas 1 through the device 100, are shown in Figure 3a shown in bold.
  • the start-up of the process represents a state which exists before the start of the actual process for compressing exhaust evaporation gas.
  • exhaust evaporation gas 1 accumulating in the vessel 10 is passed through the first inlet 31 through the heat exchanger 30 and is heated only due to the temperature difference between the cold exhaust evaporation gas and the heat exchanger which is at a warmer temperature, i.e. without heat exchange against exhaust evaporation gas compressed in the first compressor stage 21, as is the case after start-up of the process in the normal operation of the device and the process.
  • a cooling of the heat exchanger 30 takes place.
  • the valve position of the first valve 41 is such that the exhaust evaporation gas is subsequently compressed in the first compressor stage 21 and in the second compressor stage 22. In principle, however, it is also conceivable that the valve position of the first valve 41 is such that the exhaust evaporation gas is only fed to the first compressor stage.
  • the person skilled in the art will understand that, by suitable adjustments to the positioning of the first valve in the device 100, it is also possible in principle to feed the exhaust evaporation gas only to the second compressor stage 22.
  • the valve position of the second valve 42 is such that exhaust evaporation gas compressed in the first compressor stage is not led to the second inlet 33 of the heat exchanger 30, but via the second line 44 to a point after the second compressor stage 22, where the exhaust evaporation gas compressed in the first compressor stage flows into the line connecting the second compressor stage 22 to the heat exchanger 60 included in this embodiment.
  • the exhaust steam gas compressed in the two compressor stages 21, 22 is fed via the bypass line 90, valve 91 and the bypass line 40 to the reliquefaction device 50. This results in recycling of the exhaust steam gas 1 from the container 10 back into the container 10 and/or into a Figure 3a additional containers not shown for cryogenic storage of liquefied petroleum gas or gas.
  • Figure 3b is a schematic representation of the material flows of the process from Figure 3a after the start-up phase, ie as it is the case after the process has started up in the normal operation of the device and the process.
  • the valve position of the first valve 41 is determined in the manner described in Figure 3b described method is changed in such a way that the line connecting the first outlet 32 of the heat exchanger 30 and the first compressor stage 21 is no longer is fluidly connected to the second compressor stage 22.
  • the valve position of the second valve 42 is changed such that the exhaust evaporation gas compressed in the first compressor stage 21 is fed to the heat exchanger 30 via its second inlet 33.
  • the exhaust evaporation gas 1 accumulating in the container 10 is now fed to the heat exchanger 30 via its first inlet 31 and heated by heat exchange with the exhaust evaporation gas compressed in the first compressor stage 21 in order to obtain a heated exhaust evaporation gas.
  • the cooling of the exhaust evaporation gas compressed in the first compressor stage 21 takes place in the heat exchanger 30 by heat exchange with the exhaust evaporation gas 1, which accrues in the container 10 and is to be compressed in the first compressor stage 21.
  • the exhaust gas compressed in the first compressor stage 21 and cooled against exhaust gas 1 from the vessel 10 leaves the heat exchanger via its second outlet 34 and is fed to the second compressor stage 22 to obtain a further compressed exhaust gas.
  • the further compressed exhaust gas Downstream of the second compressor stage 22, the further compressed exhaust gas is optionally cooled in heat exchanger 60 before it is made available to a consumer 80 of a downstream process.
  • the even further compressed exhaust gas can be fed via the bypass line 40 to the reliquefaction device 50, which can in particular be a throttle valve.
  • the cryogen recycled in this way is returned to the vessel 10 from which it originates.
  • the liquefied exhaust gas is fed into a Figure 3b another container, not shown, for cryogenic storage of gas.
  • Figure 4a is a schematic representation of the material flows during the start-up phase of a process for compressing exhaust gas according to an embodiment of the present invention.
  • a device 100 is used which, in addition to the devices already described in connection with Figure 2 elements described in the embodiment shown, the description of which also applies analogously to the Figure 4a illustrated embodiment applies, further comprises a first valve 41, a second valve 42, a first line 43 branching off upstream of the first compressor stage 21 and a line 44 opening downstream of the second compressor stage 22.
  • the first valve 41 is arranged downstream of the first outlet 32 of the heat exchanger 30 and upstream of the first compressor stage 21 and is designed to supply heated exhaust gas from the heat exchanger 30 to the first compressor stage 21 and/or the second compressor stage 22.
  • the first valve 41 is arranged in the line which fluidically connects the second outlet 34 of the heat exchanger and the second compressor stage 22, and is fluidically connected to the first outlet 32 of the heat exchanger 30 via a first line 43 which branches off from the line connecting the first outlet 32 of the heat exchanger 30 to the first compressor stage 21.
  • the second valve 42 is arranged downstream of the first compressor stage 21, more precisely in the line fluidically connecting the first compressor stage 21 to the second inlet 33 of the heat exchanger.
  • the second valve 42 is further fluidly connected to the bypass line 40 via a second line 44 which opens into the device 100 downstream of the second compressor stage 22.
  • the material flows present during the start-up of the process ie the path of the evaporation gas 1 through the device 100, are shown in bold in Figure 4a for improved clarity.
  • the start-up of the process represents a state which exists before the start of the actual process for compressing evaporation gas.
  • evaporation gas 1 accumulating in the container 10 is passed through the first inlet 31 through the heat exchanger 30 and is only heated due to the Temperature difference between the cold exhaust evaporation gas and the heat exchanger which is at a warmer temperature, i.e.
  • valve position of the first valve 41 is such that the exhaust evaporation gas is subsequently compressed in the first compressor stage 21 and in the second compressor stage 22. In principle, however, it is also conceivable for the valve position of the first valve 41 to be such that the exhaust evaporation gas is only fed to the first compressor stage.
  • the person skilled in the art understands that by suitable adjustments to the positioning of the first valve in the device 100 it is also possible in principle to feed the exhaust evaporation gas only to the second compressor stage 22.
  • the valve position of the second valve 42 is such that exhaust evaporation gas compressed in the first compressor stage is not directed to the second inlet 33 of the heat exchanger 30, but via the second line 44 to a point after the second compressor stage 22, where the exhaust evaporation gas compressed in the first compressor stage flows into the line connecting the second compressor stage 22 to the heat exchanger 60.
  • the line required to carry out the Figure 4a The device 100 used in the method illustrated further comprises an optional bypass line 90 with a valve 91 arranged therein for bypassing the likewise optional heat exchanger 60 of the device 100. Downstream of the second compressor stage 22 or the heat exchanger 60, further compression optionally takes place in the further compressor stage 23 and subsequently cooling in the heat exchanger 70.
  • the device 100 can have a further bypass line 92 with a valve 93 arranged therein for bypassing the optional heat exchanger 70.
  • flash gas in the tank can be minimized if the outlet temperature of the exhaust evaporation gas compressed in the first and second compressor stages 21, 22 or in the third compressor stage 23 is lower than the temperature of the heat exchanger cooling medium in heat exchanger 60 or in heat exchanger 70.
  • the exhaust evaporation gas is then fed via the bypass line 40 to the reliquefaction device 50. This results in recycling of the exhaust evaporation gas 1 from the container 10 back into the container 10 and/or into a Figure 4a additional containers not shown for cryogenic storage of liquefied petroleum gas or gas.
  • Figure 4b is a schematic representation of the material flows of the process from Figure 4a after the start-up phase, ie as it is the case after the process has started up in the normal operation of the device and the process.
  • the valve position of the first valve 41 is determined in the manner described in Figure 3b
  • the method described above is modified such that the line connecting the first outlet 32 of the heat exchanger 30 and the first compressor stage 21 is no longer fluidically connected to the second compressor stage 22.
  • the valve position of the second valve 42 is changed such that the exhaust evaporation gas compressed in the first compressor stage 21 is fed to the heat exchanger 30 via its second inlet 33.
  • the exhaust evaporation gas 1 accumulating in the container 10 is now fed to the heat exchanger 30 via its first inlet 31 and heated by heat exchange with the exhaust evaporation gas compressed in the first compressor stage 21 to obtain a heated exhaust evaporation gas.
  • the cooling of the exhaust evaporation gas compressed in the first compressor stage 21 in the heat exchanger 30 takes place by heat exchange with the exhaust evaporation gas 1 accumulating in the container 10. and is to be compressed in the first compressor stage 21.
  • the exhaust steam gas compressed in the first compressor stage 21 and cooled against exhaust steam gas 1 from the vessel 10 leaves the heat exchanger via its second outlet 34 and is fed to the second compressor stage 22 to obtain a further compressed exhaust steam gas.
  • the further compressed exhaust steam gas Downstream of the second compressor stage 22, the further compressed exhaust steam gas is optionally cooled in heat exchanger 60 and optionally further compressed in the further compressor stage 23 to obtain an even further compressed exhaust steam gas.
  • the even further compressed exhaust steam gas can optionally be cooled in a heat exchanger 70 arranged downstream of the further compressor stage 23 before being made available to a consumer 80.
  • the further compressed evaporation gas can be fed via the bypass line 40 to the reliquefaction device 50, which can in particular be a throttle valve.
  • the cryogen thus recycled is returned to the container 10 from which it originates.
  • the liquefied evaporation gas is fed into a Figure 4b another container, not shown, for cryogenic storage of gas.
  • FIG. 5 is a flow diagram showing possible material flows that are conceivable in processes according to embodiments of the present invention.
  • Evaporation gas which is produced by the evaporation of cryogenically stored gases LG due to the supply of ambient heat in the container 10, is referred to as "evaporation gas 1" up to the first outlet of the heat exchanger 30.
  • Evaporation gas leaving the heat exchanger 30 via its first outlet is referred to herein as "heated evaporation gas 2".
  • compressed exhaust steam gas 3 The exhaust steam gas obtained by compressing the heated exhaust steam gas 2 in the first compressor stage 21 is referred to as "compressed exhaust steam gas 3". If the heated exhaust steam gas 2 is fed to the second compressor stage 22 instead of the first compressor stage 21, the exhaust steam gas compressed in the second compressor stage 22 is referred to as "compressed exhaust steam gas 3" for easier differentiation from the exhaust steam gas 3 compressed in the first compressor stage.
  • the compressed exhaust steam gas 3 thus obtained is compressed in a further compressor stage 23, different from the second compressor stage 22, to "further compressed exhaust steam gas 5" or is cooled in a reliquefaction device 50 to obtain "liquefied exhaust steam gas 7".
  • Exhaust steam gas compressed in the first compressor stage 21, which leaves the heat exchanger 30 via its second outlet is referred to herein as "cooled and compressed exhaust steam gas 4".
  • the cooled and compressed exhaust steam gas 4 is fed to the second compressor stage 22 and after its compression by the second compressor stage 22, is referred to as "further compressed exhaust gas 5.”
  • the cooled and compressed exhaust gas 4 is fed to a further compressor stage 23 instead of the second compressor stage, for example, during maintenance work on the second compressor stage 22.
  • the exhaust gas compressed in the further compressor stage is referred to as "further compressed exhaust gas 5" for easier differentiation from the exhaust gas 5 further compressed in the second compressor stage 22.
  • the further compressed evaporation gas 5, 5' can be made available to a consumer 80 or cooled in a reliquefaction device 50 to obtain "liquefied evaporation gas 7" for return to the vessel 10.
  • the further compressed evaporation gas 5, 5' can be previously fed to a further compressor stage 23. In this case, after its compression by the further compressor stage 23, it is referred to as "further compressed evaporation gas 6".
  • the return of the evaporation gas, in the gaseous state, to the vessel 10 can take place from the outlet of each of the described compressor stages 21, 22, 23, which for improved clarity in Figure 5 is not shown separately.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
EP23219436.5A 2023-12-21 2023-12-21 Dispositif et procédé de compression de gaz d'évaporation Pending EP4575301A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP23219436.5A EP4575301A1 (fr) 2023-12-21 2023-12-21 Dispositif et procédé de compression de gaz d'évaporation
PCT/EP2024/086449 WO2025132147A1 (fr) 2023-12-21 2024-12-16 Dispositif et procédé de compression de gaz d'évaporation

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP23219436.5A EP4575301A1 (fr) 2023-12-21 2023-12-21 Dispositif et procédé de compression de gaz d'évaporation

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EP4575301A1 true EP4575301A1 (fr) 2025-06-25

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EP (1) EP4575301A1 (fr)
WO (1) WO2025132147A1 (fr)

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4305413A1 (de) * 1993-02-22 1994-08-25 Linde Ag Verfahren zur Rekondensation eines Kaltgases
US20160216029A1 (en) * 2013-09-12 2016-07-28 Cryostar Sas Device for recovering vapours from a cryogenic tank
KR20190071179A (ko) * 2017-12-14 2019-06-24 대우조선해양 주식회사 선박용 증발가스 재액화 시스템 및 방법

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4305413A1 (de) * 1993-02-22 1994-08-25 Linde Ag Verfahren zur Rekondensation eines Kaltgases
US20160216029A1 (en) * 2013-09-12 2016-07-28 Cryostar Sas Device for recovering vapours from a cryogenic tank
KR20190071179A (ko) * 2017-12-14 2019-06-24 대우조선해양 주식회사 선박용 증발가스 재액화 시스템 및 방법

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