EP3701129A1 - Installation de liquéfaction de gaz, plus particulièrement du gaz de réseau - Google Patents

Installation de liquéfaction de gaz, plus particulièrement du gaz de réseau

Info

Publication number
EP3701129A1
EP3701129A1 EP18800770.2A EP18800770A EP3701129A1 EP 3701129 A1 EP3701129 A1 EP 3701129A1 EP 18800770 A EP18800770 A EP 18800770A EP 3701129 A1 EP3701129 A1 EP 3701129A1
Authority
EP
European Patent Office
Prior art keywords
gas
plant
fluid
axial direction
fact
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.)
Granted
Application number
EP18800770.2A
Other languages
German (de)
English (en)
Other versions
EP3701129B1 (fr
Inventor
Mario MORMILE
Marco PALELLA
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.)
Graf Industries SpA
Original Assignee
Graf SpA
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 Graf SpA filed Critical Graf SpA
Priority to HRP20220249TT priority Critical patent/HRP20220249T1/hr
Publication of EP3701129A1 publication Critical patent/EP3701129A1/fr
Application granted granted Critical
Publication of EP3701129B1 publication Critical patent/EP3701129B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01L—CYCLICALLY OPERATING VALVES FOR MACHINES OR ENGINES
    • F01L15/00—Valve-gear or valve arrangements, e.g. with reciprocatory slide valves, other than provided for in groups F01L17/00 - F01L29/00
    • F01L15/14—Arrangements with several co-operating main valves, e.g. reciprocatory and rotary
    • F01L15/16—Arrangements with several co-operating main valves, e.g. reciprocatory and rotary with reciprocatory slide valves only
    • 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
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—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
    • F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • 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
    • F25J2210/42—Nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream

Definitions

  • the present invention relates to a plant for the liquefaction of gas, particularly network gas.
  • network gas a gaseous mixture of highly volatile hydrocarbons, composed largely of methane, which is present in a percentage between 90% and 99%, while the remaining part consists of ethane, propane and butane, with possible traces of carbon dioxide, nitrogen, noble gases and hydrogen sulfide.
  • This network gas is extracted from oil or natural gas fields or, alternatively, is produced by anaerobic fermentation processes, and is intended for both domestic and automotive transportation use.
  • the distribution of gas is carried out, where possible, through a distribution network consisting of pipelines, which transport the gas at high pressure.
  • the gas can be stored and transported by suitably prepared tankers and then treated, at the user's premises, in regasification stations where it is returned to its aeriform state, and fed into the local gas pipeline network.
  • the plants for the liquefaction of gas comprise a compressor, generally of the type of a turbocharger, which increases the gas pressure to significantly high values.
  • the compressed gas is conveyed to a heat exchanger, which significantly reduces its temperature.
  • the gas is subjected to expansion, so as to bring it to a pressure and a temperature such as to cause the change of its state from gas to liquid.
  • it is not possible to liquefy the entire flow rate of treated gas, but a gas-liquid mixture is obtained.
  • the two phases are separated by a gas-liquid separator, which allows obtaining a liquefied gas flow rate, while the fraction in the gaseous phase is mixed with the flow rate of gas to be liquefied entering the liquefaction plant.
  • the expansion can be carried out by means of a turbo-expander, which permits making a considerable pressure jump, but also producing electricity, which is used to supply the liquefaction plant itself.
  • the liquefied gas is stored on the LNG carriers, which transport it from the place of extraction to the place of consumption.
  • This particular type of plant is particularly advantageous inasmuch as it allows the recovery of energy through the turbo-expander, but its use is only useful in the case of sufficiently large flow rates.
  • the liquefaction plant provides for the expansion thereof by means of rolling valves, which, however, does not allow the recovery of energy.
  • the liquefied gas is stored in cryogenic cylinders and transported, so as to be available for uses of various kinds, including automotive transportation.
  • the plants for the liquefaction of network gas to be used for automotive transportation involve high operating costs related to the compression of the gas and its subsequent expansion.
  • the main aim of the present invention is to provide a plant for the liquefaction of gas which permits limiting the operating costs of the process as a whole.
  • one object of the present invention is to allow the recovery of useful work within the plant.
  • Another object of the present invention is to provide a plant for the liquefaction of gas which permits maximizing the fraction of liquefied gas obtained, thus minimizing the need for recovery of the fraction in the gas phase.
  • a further object of the present invention is to provide a plant for the liquefaction of gas which allows overcoming the aforementioned drawbacks of the prior art within the scope of a simple, rational, easy, efficient to use and cost-effective solution.
  • Figure 1 is a schematic view of the plant according to the invention.
  • Figure 2 is a schematic sectional view of a detail of the plant of Figure 1 with the fluid- operated distributor in the intake configuration;
  • Figure 3 is a schematic sectional view of the detail of Figure 2 with the fluid- operated distributor in an expansion configuration
  • Figure 4 is a schematic sectional view of the detail of Figure 2 with the fluid- operated distributor in the exhaust configuration.
  • reference numeral 1 globally indicates a plant for the liquefaction of gas.
  • the plant 1 for the liquefaction of gas, particularly network gas comprises: at least one compressor 2 adapted to increase the pressure of at least one gas in order to obtain compressed gas;
  • At least one cooling device 3 connected in a fluid- operated manner to the compressor 2 and adapted to cool the compressed gas
  • At least one expansion assembly 6, 10, 20 which is connected in a fluid- operated manner to the cooling device 3 and adapted to reduce the pressure of the compressed gas in order to obtain liquefied gas;
  • At least one filling station 4 which is connected in a fluid- operated manner to the expansion assembly 6, 10, 20 and adapted to fill at least one cryogenic reservoir 5 with the liquefied gas.
  • the plant 1 is intended to be used for the liquefaction of cryogenic gases, i.e. gases with very low boiling temperatures at atmospheric pressure (generally below -100°C).
  • cryogenic gases i.e. gases with very low boiling temperatures at atmospheric pressure (generally below -100°C).
  • the plant 1 can be used for the liquefaction of any cryogenic gas by varying the pressure and temperature operating conditions depending on the treated gas.
  • the network gas as well as other cryogenic gases, is in supercritical fluid condition, i.e., a gas that cannot be liquefied by simple compression.
  • the plant 1 therefore exploits the combined effect of compression, cooling and subsequent expansion of the gas in order to liquefy it.
  • the gas taken from the network is sent to the compressor 2, which increases the pressure, bringing it to rather high pressure values.
  • the compressed gas which is obtained out of such compressor 2 is then cooled by means of the cooling device 3, the purpose of which is to cool the gas down to temperatures well below 0°C.
  • a cryogenic heat exchanger in which the coolant liquid, usually liquid nitrogen, is used to cool the compressed gas, bringing it down to a very low temperature, which in the particular case of network gas is about -60°C.
  • the cooling device 3 is a cryogenic heat exchanger of the "plate" type, although the possibility of providing a different type of cooling device 3 cannot be ruled out.
  • the cooling device 3 is made of special materials, e.g., special steels with the addition of chrome and nickel, which have a very low tendency to brittle fracture.
  • the compressed and adequately cooled gas is sent to the expansion assembly 6, 10, 20, in which the actual liquefaction of the gas takes place.
  • the pressure reduction of the gas made by the expansion assembly 6, 10, 20 involves a further reduction in temperature, so that the gas is in conditions of temperature and pressure such as to obtain the change of state from gas to liquid, obtaining the liquefied gas.
  • the conditions of the liquefied gas out of the expansion assembly 6, 10, 20 are about 3 bar and -145°C.
  • a liquefied gas is not obtained out of the plant 1 consisting of a flow rate entirely in the liquid phase, but a mist is obtained, i.e., a gas-liquid mixture in the form of aerosol, wherein therefore the liquid fraction is dispersed inside the gaseous fraction in the form of small drops.
  • the plant 1 is made to maximize the obtainable fraction of liquefied gas, so as to increase as much as possible the output of the plant itself and reduce overall production costs.
  • the expansion assembly 6, 10, 20 comprises at least one piston expander 6 comprising at least one expansion chamber 7 which extends along a first axial direction A and is provided with at least one intake and exhaust mouth 8 and at least one piston 9 housed in the expansion chamber 7 and moveable sliding inside the expansion chamber itself along the first axial direction A.
  • the expansion assembly 6, 10, 20 is able to operate with very high inlet gas pressures, even higher than 150 bar.
  • the compressed gas is introduced into the expansion chamber 7 and the expansion is performed by varying the volume of the expansion chamber itself by means of the sliding of the piston 9.
  • the piston 9 is mobile sliding along the first axial direction A between a first position wherein the piston 9 is placed in the proximity of the mouth 8 and the volume of the expansion chamber 7 is the least possible and a second position wherein the piston itself is separated from the mouth 8 and the volume of the expansion chamber 7 is the largest possible.
  • the compressed gas is introduced into the piston expander 6 when the piston 9 is in the first position.
  • the mouth 8 is closed and the piston 9 is moved as far as the second position, thus increasing the volume of the expansion chamber 7 and, consequently, reducing the pressure of the compressed gas and obtaining liquefied gas.
  • the piston expander 6 is of the type of a cryogenic piston expander, meaning that it is in contact with a fluid at a temperature even lower than -100°C, so that in this case as well, it is necessary to use steels which are particularly resistant to brittle fracture.
  • the piston expander 6 comprises at least one fluid- operated distributor 10 associated with the mouth 8 and adapted to control the flow direction of the gas.
  • the fluid- operated distributor 10 allows managing the opening and closing of the mouth 8 of the piston expander 6 according to precise timescales, so as to ensure the exhaust of the liquefied gas only once complete expansion has occurred, thus optimizing the operation of the plant 1.
  • the fluid- operated distributor 10 comprises:
  • At least one valve body 11 comprising at least one sliding chamber 12a, 12b having a substantially elongated shape which extends along at least a second axial direction B and provided with at least one inlet opening 13 for the inlet of the compressed gas, at least one exhaust opening 14 for the exhaust of the liquefied gas and at least one mouth opening 15 associated with the mouth 8 for the connection of the fluid- operated distributor 10 to the expansion chamber 7 of the piston expander 6; and
  • At least one slider 16a, 16b having a substantially elongated shape, housed in the sliding chamber 12a, 12b, moveable sliding along the second axial direction B and comprising at least one internal duct 17a, 17b for the passage of the compressed gas and expanded gas and partly liquefied and locatable in fluidic connection with at least two of the inlet opening 13, the mouth opening 15 and the exhaust opening 14.
  • the fact of providing the internal duct 17a, 17b with an elongated shape, or rather with a width significantly reduced compared to the length, allows obtaining a greater resistance of the fluid- operated distributor 10 to the high pressure of the fluid which passes through it, in particular of the compressed gas entering towards the piston expander 6.
  • first axial direction A and the second axial direction B are substantially parallel to one another, so that the piston expander 6 and the fluid- operated distributor 10 are arranged in a manner substantially aligned with one another, obtaining a configuration which allows minimizing the overall dimensions of the expansion assembly 6, 10, 20.
  • the possibility cannot however be ruled out of providing the first axial direction A and the second axial direction B arranged, the one to the other, in a different manner with respect to that shown in the illustrations.
  • the fluid- operated distributor 10 comprises a plurality of sliding chambers 12a, 12b and a plurality of sliders 16a, 16b, each housed in a respective sliding chamber 12a, 12b and moveable sliding in a substantially staggered manner to one another along the second axial direction B.
  • the fluid- operated distributor 10 comprises:
  • At least a first sliding chamber 12a in which is housed at least a first slider 16a provided with at least a first internal duct 17a;
  • At least a second sliding chamber 12b in which is housed at least a second slider 16b provided with at least a second internal duct 17b.
  • first slider 16a and the second slider 16b are moveable sliding in a substantially alternated manner to one another along the second axial direction B among:
  • the movement of the first slider 16a and of the second slider 16b is performed in a manner substantially synchronized with the movement of the piston 9 of the piston expander 6.
  • the fluid- operated distributor 10 is in the intake configuration.
  • the fluid- operated distributor 10 is placed in the expansion configuration, so as to occlude the mouth 8, while the piston 9 is moved towards the second position.
  • the fluid- operated distributor 10 is provided with a plurality of seals 21 which are adapted to ensure its fluid- operated seal.
  • the fluid- operated distributor 10 comprises at least one motorized linear actuator 18 adapted to move at least one of the first slider 16a and the second slider 16b along the second axial direction B.
  • the fluid- operated distributor 10 comprises at least two motorized linear actuators 18, adapted to move the first slider 16a and the second slider 16b, respectively, along the second axial direction B.
  • the plant 1 comprises at least one electric current generator 19 associated with the piston expander 6 and adapted to produce electricity, shown schematically in the illustrations.
  • the electric current generator 19 also acts as a motor, regulating the speed, start and stop of the piston expander 6.
  • the expansion assembly 6, 10, 20 can also comprise at least one rolling valve 20 interposed between the piston expander 6 and the filling station 4 and is adapted to reduce the pressure of the gas out of the piston expander 6.
  • the rolling valve 20 makes possible a further reduction in the pressure of the liquefied gas out of the piston expander 6, so as to maximize the effect of temperature drop and, consequently, maximize the fraction in liquid phase obtained out of the plant 1.
  • the liquefied gas obtained out of the expansion assembly 6, 10, 20 is conveyed to the filling station 4, by means of which it is stored in a cryogenic reservoir 5 to be transported to the end user.
  • cryogenic reservoir 5 is adapted to maintain the liquefied gas under the temperature and pressure conditions obtained out of the expansion assembly 6, 10, 20, so it must be made in such a way as to ensure adequate thermal insulation with respect to the environment.
  • cryogenic reservoir 5 is provided with an inner wall and an outer wall, between which is defined a cavity containing highly insulating materials, so as to thermally insulate the liquefied gas.
  • the cryogenic reservoir 5 can also comprise a cooling system which exploits the flow of a coolant fluid inside pipes housed inside the cryogenic reservoir itself, so as to keep the liquefied gas under the set temperature conditions, avoiding the heating and subsequent evaporation thereof.
  • the cryogenic reservoir 5 must be resistant to overpressure and to cryogenic temperatures, so it is made using steels resistant to brittle fracture and the wall thicknesses are assessed in accordance with the working pressure.
  • the fluid- operated connection inside the plant 1 is made by means of a system of pipes made of materials resistant to both high pressures and to cryogenic temperatures.
  • the piston expander is associated with an electric current generator makes it possible to recover the useful work done by the expander itself and produce electric current, which is used to supply the plant itself, in order to reduce the amount of electricity supplied by the network.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Chemical & Material Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Supply Devices, Intensifiers, Converters, And Telemotors (AREA)
  • Treating Waste Gases (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Abstract

L'installation (1) pour la liquéfaction de gaz, en particulier de gaz de réseau, de la présente invention comprend: - un compresseur (2) adapté pour augmenter la pression d'un gaz afin d'obtenir du gaz comprimé; - un dispositif de refroidissement (3) relié de manière fluidique au compresseur (2), conçu pour refroidir le gaz comprimé; un ensemble d'expansion (6, 10, 20) qui est relié de manière fluidique au dispositif de refroidissement (3), conçu pour réduire la pression du gaz comprimé afin d'obtenir un gaz liquéfié; et une station de remplissage (4) relié de manière fluidique à l'ensemble d'expansion (6, 10, 20) et conçu pour remplir un réservoir cryogénique (5) avec le gaz liquéfié. L'ensemble d'expansion (6, 10, 20) comprend un dispositif d'expansion de piston (6) comprenant une chambre d'expansion (7) qui s'étend le long d'une première direction axiale (A) et comportant une bouche d'admission et d'échappement (8) et un piston (9) logé dans la chambre d'expansion (7) et mobile en coulissant à l'intérieur de la chambre d'expansion (7) suivant le long de la première direction axiale (A).
EP18800770.2A 2017-10-27 2018-10-24 Installation de liquéfaction de gaz, plus particulièrement du gaz de réseau Active EP3701129B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
HRP20220249TT HRP20220249T1 (hr) 2017-10-27 2018-10-24 Postrojenje za ukapljivanje plina, posebno mrežnog plina

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IT102017000122573A IT201700122573A1 (it) 2017-10-27 2017-10-27 Impianto per la liquefazione di gas, particolarmente gas di rete
PCT/IB2018/058296 WO2019082096A1 (fr) 2017-10-27 2018-10-24 Installation de liquéfaction de gaz, plus particulièrement du gaz de réseau

Publications (2)

Publication Number Publication Date
EP3701129A1 true EP3701129A1 (fr) 2020-09-02
EP3701129B1 EP3701129B1 (fr) 2021-12-08

Family

ID=61526973

Family Applications (1)

Application Number Title Priority Date Filing Date
EP18800770.2A Active EP3701129B1 (fr) 2017-10-27 2018-10-24 Installation de liquéfaction de gaz, plus particulièrement du gaz de réseau

Country Status (6)

Country Link
EP (1) EP3701129B1 (fr)
DK (1) DK3701129T3 (fr)
ES (1) ES2907034T3 (fr)
HR (1) HRP20220249T1 (fr)
IT (1) IT201700122573A1 (fr)
WO (1) WO2019082096A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
IT201800009221A1 (it) * 2018-10-05 2020-04-05 Graf Spa Stazione di servizio per mezzi di trasporto

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR562911A (fr) * 1922-05-08 1923-11-22 Air Liquide Perfectionnements aux procédés pour la séparation d'un mélange gazeux en ses éléments, par liquéfaction et rectification, et dispositifs pour la mise en oeuvre
US3246478A (en) * 1963-04-08 1966-04-19 Union Carbide Corp Process and apparatus for separating low-boiling gas mixtures
RU2234646C2 (ru) * 2001-10-25 2004-08-20 Общество с ограниченной ответственностью "Оренбурггазпром" Свободнопоршневой детандер
US7673476B2 (en) * 2005-03-28 2010-03-09 Cambridge Cryogenics Technologies Compact, modular method and apparatus for liquefying natural gas
US20160047243A1 (en) * 2012-06-26 2016-02-18 Cogen Microsystems Pty Ltd Expander for a heat engine

Also Published As

Publication number Publication date
RU2020114196A (ru) 2021-11-30
HRP20220249T1 (hr) 2022-04-29
ES2907034T3 (es) 2022-04-21
RU2020114196A3 (fr) 2022-03-17
WO2019082096A1 (fr) 2019-05-02
DK3701129T3 (da) 2022-02-07
EP3701129B1 (fr) 2021-12-08
IT201700122573A1 (it) 2019-04-27

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