CN113316696A - Device for producing gaseous gas from liquefied gas - Google Patents

Device for producing gaseous gas from liquefied gas Download PDF

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Publication number
CN113316696A
CN113316696A CN201980079322.0A CN201980079322A CN113316696A CN 113316696 A CN113316696 A CN 113316696A CN 201980079322 A CN201980079322 A CN 201980079322A CN 113316696 A CN113316696 A CN 113316696A
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China
Prior art keywords
circuit
outlet
gas
compressor
inlet
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Granted
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CN201980079322.0A
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Chinese (zh)
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CN113316696B (en
Inventor
B.奥恩
M.比萨特
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Gaztransport et Technigaz SA
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Gaztransport et Technigaz SA
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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
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F25J1/0025—Boil-off gases "BOG" from storages
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—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
    • 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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
    • F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
    • F25J1/0277—Offshore use, e.g. during shipping
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    • 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
    • F17C2201/00—Vessel construction, in particular geometry, arrangement or size
    • F17C2201/05—Size
    • F17C2201/052—Size large (>1000 m3)
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    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—Mixtures
    • F17C2221/032—Hydrocarbons
    • F17C2221/033—Methane, e.g. natural gas, CNG, LNG, GNL, GNC, PLNG
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    • 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
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
    • F17C2223/0146—Two-phase
    • F17C2223/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
    • F17C2223/033—Small pressure, e.g. for liquefied gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/04—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by other properties of handled fluid before transfer
    • F17C2223/042—Localisation of the removal point
    • F17C2223/046—Localisation of the removal point in the liquid
    • F17C2223/047—Localisation of the removal point in the liquid with a dip tube
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    • 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
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/01—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the phase
    • F17C2225/0107—Single phase
    • F17C2225/0123—Single phase gaseous, e.g. CNG, GNC
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    • 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
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    • F17C2225/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2225/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
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    • 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
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    • F17C2225/033—Small pressure, e.g. for liquefied gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/03—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the pressure level
    • F17C2225/035—High pressure, i.e. between 10 and 80 bars
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    • 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
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    • F17C2225/042—Localisation of the filling point
    • F17C2225/043—Localisation of the filling point in the gas
    • F17C2225/044—Localisation of the filling point in the gas at several points, e.g. with a device for recondensing gas
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    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
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    • F17C2265/032—Treating the boil-off by recovery
    • F17C2265/033—Treating the boil-off by recovery with cooling
    • F17C2265/034—Treating the boil-off by recovery with cooling with condensing the gas phase
    • 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
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/03—Treating the boil-off
    • F17C2265/032—Treating the boil-off by recovery
    • F17C2265/037—Treating the boil-off by recovery with pressurising
    • 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
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/05—Regasification
    • 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
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/06—Fluid distribution
    • F17C2265/066—Fluid distribution for feeding engines for propulsion
    • 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
    • F17C2270/00—Applications
    • F17C2270/01—Applications for fluid transport or storage
    • F17C2270/0102—Applications for fluid transport or storage on or in the water
    • F17C2270/0105—Ships
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/34—Details about subcooling of liquids

Abstract

Device (10) for producing a gas in gaseous form from a liquefied gas, comprising: -a first heat exchanger (24) comprising a first cooling circuit (24a) comprising an inlet for liquefied gas connected to a first line (18) intended to be connected to an outlet for liquefied gas of at least one tank (14) for liquefied gas, -means (19) for evaporation by depressurization equipped with said first line, and-at least one compressor (26,28), characterized in that the device further comprises a heater (25) comprising an inlet for gas in at least partially liquid form connected to the outlet of the first circuit (24a), and an outlet for gas in gaseous form only connected to the at least one compressor (26, 28).

Description

Device for producing gaseous gas from liquefied gas
Technical Field
The invention relates in particular to a device for producing gaseous gases from liquefied gases.
Background
The prior art includes documents FR-A1-3066257, WO-A1-2017/192136 and KR-A-20180093577.
In order to more easily transport gases such as natural gas over long distances, it is common to liquefy the gas (to liquefied natural gas-LNG) by cooling the gas to a low temperature (e.g., -160 ℃ at atmospheric pressure). The liquefied gas is then loaded onto a special vessel.
In liquefied gas transport vessels, for example of the LNG type, the energy production plant is intended to meet the energy requirements for the operation of the vessel, in particular for the propulsion of the vessel and/or the production of electricity for the plant on the vessel.
Such plants currently comprise a heat engine consuming gas from an evaporator supplied by a liquefied gas cargo transported in one or more tanks of a ship.
Document FR- A-2837783 provides the use of A submersible pump at the bottom of the tank of the ship to supply such an evaporator and/or other systems required for propulsion.
In order to limit the evaporation of the liquefied gas, it is known practice to store it under pressure in a tank so as to move on the vaporization curve of the liquefied gas in question, thus increasing its vaporization temperature. Liquefied gases can thus be stored at higher temperatures, which results in limiting the evaporation of the gas.
However, natural evaporation of natural gas is unavoidable; this phenomenon is known as "NBOG" and is an acronym for Natural Boil-Off Gas (versus Forced Gas Boil-Off, or FBOG, Forced Boil-Off Gas). Naturally evaporated gas in the tanks of the ship is normally used for supplying the above-mentioned equipment. In case the amount of natural boil-off gas is not sufficient to meet the gas demand of the plant (first case), the pump immersed in the tank is activated to supply more fuel gas after forced evaporation. In case the amount of boil-off gas is too large compared to the demand of the plant (second case), the excess gas is usually burned in the gas combustion unit, which represents a loss of fuel gas.
In the current technology, the tank improvements result in a lower and lower natural evaporation rate (BOR) of the liquefied gas and a higher and higher mechanical efficiency of the ship. Therefore, in one of the first and second cases described above, each day, the difference between the amount of gas naturally produced by evaporation and the amount of gas required for the equipment of the ship is very large.
There is therefore an increasing interest in solutions for cooling the liquefied gas contained in the storage tank and managing the BOG produced in the tank, such as re-liquefaction or cooling units, for example those described in application WO-a 1-2016/075399. The basic idea of this document is to propose a device for cooling liquefied gases which is able to limit the natural evaporation of the liquefied gas while maintaining its thermodynamic state, allowing its continuous storage. However, the heat exchanger technology described in this document is expensive and inefficient, and has other disadvantages, which will be described in detail below.
In addition, there are several parameters that can affect the generation of NBOG, such as fluid movement and environmental conditions. The energy requirements of ships also vary greatly, depending on the operation performed or the speed of travel. Therefore, it is difficult to establish an effective BOG management solution because the amount of excess NBOG may vary greatly.
It has been proposed to force the evaporation of gases and the generation of cold by means of a vacuum evaporator. The vacuum evaporator comprises a phase separation bottle mounted between a means for evaporating liquefied gas taken from a tank and a means for depressurizing the bottle. This makes it possible to obtain a greater cooling capacity which can be used for cooling the gas contained in the main tank.
The present invention provides a simple, effective and economical improvement over the prior art.
Disclosure of Invention
The invention provides an apparatus for producing gaseous gas from liquefied gas, comprising:
a first heat exchanger comprising a first cooling circuit comprising a liquefied gas inlet connected to a first line intended to be connected to the liquefied gas outlet of at least one liquefied gas storage tank,
-means for evaporation by depressurization equipped with said first line, and
-at least one compressor for compressing the refrigerant,
characterized in that the device further comprises a heater comprising an inlet for gas at least partially in liquid form connected to the outlet of the first circuit, and an outlet for gas only in gaseous form connected to the at least one compressor.
Thus, the prior art Vacuum Evaporator (VE) separator bottle is replaced by a heater. Unlike a separation bottle intended to contain a two-phase mixture, the heater is configured to supply gas at the outlet in gaseous form only. This simplifies the construction of the device, since separate administration of liquid and gas in the bottle is no longer required.
The device according to the invention may comprise one or more of the following features taken separately from each other or in combination with each other:
-the first circuit is configured to heat the fluid circulating therein from a temperature of less than or equal to-165 ℃ to a temperature of greater than or equal to-165 ℃,
-the heater is a heat exchanger comprising a third circuit comprising an inlet for gas at least partly in liquid form connected to the outlet of the first circuit, and an outlet for gas only in gaseous form connected to the at least one compressor,
-the third circuit is configured to heat the fluid circulating therein from a temperature of less than or equal to-165 ℃ to a temperature of greater than or equal to-50 ℃,
the exchanger forming the heater comprises a fourth circuit in which the heating fluid circulates,
-the fourth circuit is configured to cool the fluid circulating therein from a temperature greater than or equal to 50 ℃ to a temperature less than or equal to 0 ℃,
-the heated fluid is compressed gas taken from the outlet of the at least one compressor,
-the outlet of said at least one compressor, preferably a single outlet, is connected to the inlet of said fourth circuit forming an exchanger of the heater,
the device comprises at least two compressors mounted in series, the outlet of the upstream compressor being connected to the inlet of said fourth circuit forming the exchanger of the heater, one outlet of said fourth circuit being connected to the inlet of the downstream compressor,
the device comprises at least two compressors mounted in series, the outlet of the upstream compressor being connected to the inlet of the downstream compressor, the outlet of the downstream compressor being connected to the inlet of said fourth circuit forming an exchanger of the heater,
-said fourth circuit has an outlet connected to at least one compressor,
-the inlet of the third circuit is also connected to an outlet (45) for gaseous gas from the tank,
the first heat exchanger comprises a second circuit comprising a liquefied gas inlet connected to a third line intended to be connected to the liquefied gas outlet of the tank; depending on the mode of operation of the device, this second circuit may be a cooling circuit and a heating circuit in sequence,
said first heat exchanger comprises a fifth heating circuit comprising a gaseous gas inlet connected to a fourth line intended to be connected to the outlet of said compressor or, in the case of two compressors in series, to the outlet of a downstream compressor,
-the second circuit is configured to cool the fluid circulating therein from a temperature of less than or equal to-160 ℃ to a temperature of less than or equal to-165 ℃ and/or the fifth circuit is configured to cool the fluid circulating therein from a temperature of less than or equal to-100 ℃ to a temperature of less than or equal to-130 ℃,
the outlet of the fourth circuit is also connected to the inlet of the fifth circuit,
the device comprises a fifth line equipped with expansion means comprising an inlet connected to the outlet of the fifth circuit and an outlet intended to be connected to the liquefied gas inlet of the tank,
the device comprises a sixth line, the inlet of which is connected to the outlet of the second circuit and the outlet of which is connected to the liquefied gas inlet of the tank,
the gas inlet of the fifth circuit is connected to the outlet of the compressor via a sixth circuit of second heat exchangers or, in the case of two compressors in series, to the outlet of a downstream compressor,
-the sixth circuit is configured to cool the fluid circulating therein from a temperature greater than or equal to 0 ℃ to a temperature less than or equal to-100 ℃,
the second heat exchanger comprises a seventh circuit, the inlet of which is connected to the outlet for the gaseous gas from the tank, the outlet of which is connected to the compressor, or to a downstream compressor in the case of two compressors in series,
-said seventh circuit is configured to heat the fluid circulating therein from a temperature lower than or equal to-100 ℃ to a temperature higher than or equal to-50 ℃
The invention also relates to a ship, in particular for transporting liquefied gas, comprising at least one device as described above.
The invention also relates to a method for producing a gas in gaseous form from a liquefied gas by means of a device according to one of the preceding claims, characterized in that it comprises the step of extracting the liquefied gas and completely evaporating the gas before supplying said at least one compressor.
The evaporation may be obtained by heating the liquefied gas with a heating fluid, which may be a compressed gas taken from an outlet of the at least one compressor. The compressed gas is preferably taken between two compressors installed in series or at the outlet of two compressors installed in series.
Drawings
The invention will be better understood and other details, characteristics and advantages thereof will become more apparent from a reading of the following description, given by way of non-limiting example, with reference to the accompanying drawings. In the drawings:
fig. 1 is a schematic view of a first embodiment of the device according to the invention, which device is here equipped with a ship,
fig. 2 is a schematic view of a second embodiment of the device according to the invention, here equipped with a vessel,
FIG. 3 is a schematic view of a third embodiment of the apparatus according to the invention, here equipped with a vessel;
fig. 4 is a schematic view of a fourth embodiment of the device according to the invention, which is here equipped with a vessel,
FIG. 5 is a schematic view of a fifth embodiment of the device according to the invention, where the device is equipped with a vessel, and
fig. 6 is a schematic diagram illustrating the mode of operation of the device of fig. 5.
Fig. 7 is a schematic diagram illustrating another mode of operation of the device of fig. 5.
Detailed Description
Fig. 1 shows a first embodiment of a device 10 according to the invention, which device 10 makes it possible in particular to produce gas in gaseous form from liquefied gas.
The apparatus 10 is particularly, but not exclusively, suitable for supplying fuel gas to a vessel, such as a liquefied gas carrier vessel (fig. 1 to 3).
The vessel comprises one or more tanks 14 for storing liquefied gas. The gas is for example methane or a gas mixture comprising methane. The or each tank 14 may contain the gas in liquefied form at a predetermined pressure and temperature, for example at atmospheric pressure and a temperature of-160 ℃. One or more tanks 14 on the vessel may be connected to the apparatus 12 for generating energy on the vessel. Therefore, the number of cans is not limited. For example between 1 and 6. Each tank 14 may have a capacity of 1000 to 50000 cubic meters.
In the following, the term "tank" should be interpreted as "the or each tank".
The tank 14 contains a liquefied gas 14a and a gas 14b generated by evaporation, in particular natural evaporation, of the liquefied gas 14a in the tank 14. Naturally, the liquefied gas 14a is stored in the bottom of the tank 14, while the boil-off gas 14b is located above the liquefied gas in the tank, schematically indicated by the letter N.
Hereinafter, "LNG" means liquefied gas, that is, gas in liquid form, "BOG" means boil-off gas, "NBOG" means natural boil-off gas, "FBOG" means forced boil-off gas, these acronyms being known to those skilled in the art, as they correspond to the initials of the relevant english expression.
In the embodiment shown in fig. 1, the pumps 16a, 16b are submerged in the LNG in the tank 14 and are preferably located at the bottom of the tank to ensure that they are supplied with LNG only.
Here, there are two pumps 16a, 16 b. The pump 16a is connected to one end, here the lower end, of a line 18. The pump 16b is connected to one end, here the lower end, of the line 20. In a variant, there may be more of each type of pump, for example to provide redundancy of 16a and 16b, or to use an existing pump, such as an ejector pump already present on board the vessel (in which case the function of 16b may be provided by four ejector pumps, each present in four separate tanks). In a variant, it is also possible to use fuel gas pumps already present on board the vessel (in which case the function of 16a may be provided by the fuel gas pump(s), each fuel gas pump being present in one or more separate tanks).
The pipeline 20 comprises an upper end connected to a boom 22 for spraying LNG droplets above the level N in the upper part of the tank 14. Boom 22 is thus configured to inject LNG droplets into the NBOG. This makes it possible to force the NBOG to re-condense in the tank 14. Pump 16b is configured to force circulation of LNG in line 20 from the bottom of tank 14 to boom 22 and ensure that the LNG is sprayed in the form of droplets. In practice, there may be a gas overhead in the main tank, while NBOG may circulate in the pipeline.
The pump 16a is configured to force the LNG in the line 18 to pass from the bottom of the storage tank 14 to the heat exchanger 24. Line 18 includes a pressure reduction device 19 to reduce the pressure of the LNG circulating in line 18 before reaching exchanger 24. The pressure reducing means 19 comprises, for example, a joule-thomson valve.
Thus, the passage of LNG in line 18 and through pressure reduction device 19 causes the LNG to partially vaporize prior to being supplied to exchanger 24.
In the example shown, the heat exchanger 24 comprises three heat exchange circuits, of which a first circuit 24a has an inlet connected to the line 18 for supplying the first circuit 24a with the two-phase gas leaving the pressure reducing means 19.
The outlet of the first circuit 24a is connected to the inlet of a heater 25, the outlet of the heater 25 being connected to a single inlet of a first compressor 26. The compressor 26, referred to as the upstream compressor, here has a single outlet connected to a first inlet of a compressor 28, referred to as the downstream compressor. The compressor 28 here has a single outlet which is connected to the plant 12 by one of the paths of the three-way valve 46.
The heat exchanger 24 includes a second circuit 24b, the second circuit 24b including an inlet connected by a line 30 to one of the paths of a three-way valve 38a, the other two paths of the three-way valve 38a being connected to the line 20 and the boom 22, respectively.
The outlet of second circuit 24b is connected to line 32, line 32 also being connected to one of the paths of three-way valve 38b, the other path of three-way valve 38b being connected to boom 22.
The heat exchanger 24 comprises a third circuit 24c, the third circuit 24c comprising an outlet connected by a line 34 to the last path of a three-way valve 38b and to a plunger system 35 for refilling the tank 14 with LNG, preferably at the bottom of the vessel. Line 34 is equipped with an expansion device 36, the expansion device 36 being configured to reduce the pressure of the gas and recondense it before it is re-injected into the tank 24.
The expansion device 36 comprises, for example, a joule-thomson effect valve, with the aim of reducing the gas temperature by adiabatic expansion.
Joule-thomson relaxation or decompression is a steady and slow laminar relaxation achieved by passing gas through a buffer (usually cotton wool or silk grey cloth) in an insulated horizontal conduit, the pressure on the left and right sides of the buffer being different. For real gases, joule-thomson expansion is usually accompanied by a temperature change: this is the joule-thomson effect.
Line 32 is also connected to the boom 22 and the LNG refilling system 35 from the other tanks 14 of the vessel by means of other three-way valves 38a ', 38 b'.
The inlet of the third circuit 24c is connected to the outlet of the circuit 42b of the other heat exchanger 42, and the inlet of the other heat exchanger 42 is connected to the remaining path of the three-way valve 46. The exchanger 42 comprises a further circuit 42a, one outlet of which is connected to a second inlet of the compressor 28.
The inlet of loop 42a is connected to the BOG outlet 45 of the or each tank 14.
Circuit 24a is a cold circuit in which a fluid circulates, in this case depressurized LNG, intended to be heated by its circulation in order to partially vaporize it. It is intended to be heated and thus to transmit cold. The circuit 24a is therefore considered to be a cooling circuit.
The circuit 24b is in the first case a hot circuit, and therefore a heating circuit, and in the second case a cold circuit, and therefore a cooling circuit, in which the fluid circulates and in which case the LNG coming from the storage tank 14 is intended to be cooled by circulating in this circuit. It will be appreciated that the depressurization upstream of loop 24a allows the vaporization temperature to be reduced, which allows FBOG to be generated by heat exchange with LNG withdrawn from the vessel and circulated in loop 24 b. Vaporization of the FBOG requires heat to be supplied by the lng circulating in loop 24 b; it is therefore the refrigeration source used to cool the LNG circulating in loop 24 b.
The circuit 24c is a thermal circuit, and therefore a heating circuit, in which the fluid circulates, in which case the compressed gas leaving the compressors 26,28 is intended to be cooled by circulating in this circuit. Expansion downstream of loop 24c allows the gas to be recondensed and reliquefied before being re-injected into tank 14.
In the first case, the LNG coming from the storage tank 14 is therefore sent by the pump 16a to the pressure reduction means 19 and then circulates in the cold circuit 24a of the exchanger 24. At the same time, LNG from the storage tank 14 is delivered by pump 16b to the hot loop 24b of the exchanger 24. Thus, the heat exchange between these circuits results in:
heating the depressurized and partially vaporized LNG in order to continue its vaporization, which is done in heater 25, and
chilled LNG, which is re-injected into the tank 14 via the system 35 or the boom 22.
In the second case, the compressed gas from the compressor 28 is further circulated in the circuit 24c before being expanded and reliquefied. At the same time, LNG from the storage tank 14 is delivered by the pump 16b to the cold loop 24b of the exchanger 24. Thus, the heat exchange between these circuits results in:
heated LNG, which is re-injected into the tank 14 via the system 35,
cooling the compressed gas, which is then expanded and reliquefied before being injected into the tank 14 via the system 35.
The compressors 26,28 may be two separate compressors or two compression stages of the same compressor. The compressors 26,28 may thus be shared.
The outlet of the compressor 28 is connected to the plant 12 for its supply of fuel gas. The compressor 28 is configured to compress the gas to an operating pressure suitable for its use in the plant 12.
In the embodiment of fig. 1, the purpose of the heater 25 is to completely heat and evaporate the gas at the outlet of the circuit 24a and to this end comprises a heating circuit 25a, which may be an electric circuit or a heat transfer fluid circuit, for example for water vapour.
Preferably, at the inlet of the heater 25, the pressure of the two-phase gas is between 120 and 800mbara, preferably between 300 and 800mbara, and the temperature is between-182 ℃ and-151 ℃, and at the outlet of the heater, the pressure of the gas in gaseous form is equal to the inlet, except for the pressure drop of the heater, and the temperature is between-120 ℃ and-15 ℃.
Fig. 2 shows an alternative embodiment of the device 10, which differs from the embodiment of fig. 1 in that the heater 25' comprises a fluid circuit 25a, the inlet of which fluid circuit 25a is connected to the outlet (preferably a single outlet) of the compressor 26, and the outlet of which fluid circuit 25a is connected to the inlet of the compressor 28.
Fig. 3 shows another variant embodiment of the device 10, which differs from fig. 1 in that the heater 25 "comprises a fluid circuit 25a, the inlet of the fluid circuit 25a being connected to the outlet (preferably a single outlet) of the compressor 28, and the outlet of the fluid circuit 25a being connected to one of the paths of a three-way valve 46, the three-way valve 46 also being connected to the apparatus 12 and to the exchanger 42. These three variants of figures 1 to 3, in addition to completely vaporizing the LNG, can also heat it to a non-cryogenic temperature, i.e. above-40 ℃
The device 10 of fig. 1 and its variants of fig. 2 and 3 may operate as follows.
1. As in the case of an insufficient amount of BOG, for example, when the vessel is sailing at a speed that requires more BOG to supplement the NBOG produced in the tank(s) 14. The device 10 will provide additional BOG or FBOG.
To control the pressure in the tank 14, the NBOG is removed from the tank through outlet 45 and then supplied to compressor 28, which compressor 28 will produce fuel gas at a pressure allowed by the plant 12, for example, approximately 6-7 bar, 15-17 bar or 300-. To replenish the gas volume and meet the consumption requirements of the plant 12, LNG from the tank 14 is delivered by a pump 16a and line 18 to a pressure reduction means 19 where the LNG undergoes pressure reduction. Then, by exchanging with the LNG circulating in the circuit 24b of the first exchanger 24, it is reheated by the circuit 24a of the first exchanger 24, while the LNG is transported by the pump 16b, the line 20 and the line 30. The so cooled LNG is then transported to the bottom of tank 14 via line 32 and plunger 35. The two-phase gas mixture reaches the heater 25 where the two-phase gas will completely change to the gas phase. The resulting FBOG is then compressed by compressor 26. The FBOG is then recompressed by compressor 28 to achieve the desired pressure for plant 12.
2. In case of excessive NBOG generation, for example when the ship is sailing at low speed or is moored, the excessive NBOG must be managed in a safe and environmentally friendly manner.
The amount of NBOG produced in the tank 14 is sufficient or superior to the reconstitution phase to meet the needs of the device 12. To control the pressure in tank 14, BOG is removed from the tank and fed to compressor 28 to achieve the desired pressure for plant 12. The excess BOG, which cannot be consumed by the plant, is sent from the outlet of the compressor 28 to the exchanger 42, where it is cooled by heat exchange with the cold NBOG taken directly from the tank 14 through the outlet 45. The excess BOG is then sent to a loop 24c where it is cooled again by heat exchange with LNG taken from the tank in the loop 24 c. The excess BOG is then recondensed by valve 36 and reinjected into the tank.
3. In the case where the vessel's main tanks 14 are cooled, for example after the return trip before loading (during which managing BOG is generally unnecessary since one or more tanks 14 are almost empty).
Typically, the reliquefaction terminal of a ship's cargo load requires cryogenic temperatures in the tank 14 prior to loading to limit the amount of LNG that will be immediately vaporized (flashed). This is typically accomplished by spraying the LNG already contained in the tank 14 using the boom 22 and associated pump 16b in order to cool the BOG of the tank. Thanks to the device 10, this operation can be performed by supplying the boom 22 with LNG from the second circuit 24b of the exchanger, which is therefore colder than the LNG contained in the tank 14.
Fig. 4 shows a variant embodiment of the device according to the invention, in which elements already described above are denoted by the same reference numerals.
The heater 25 is here shown in the form of an exchanger, wherein one circuit 25b connects the outlet of the circuit 24a of the exchanger 24 to the inlet of the compressor 26 and the other circuit 25a thereof connects the outlet of this compressor 26 to the inlet of the compressor 28, and more particularly here to two compressors 28 in parallel, since this type of compressor on board the ship requires redundancy.
Fig. 4 shows an example of the temperature of the fluid circulating in the device. It can be seen that the liquefied gas taken from the container 14 is cooled in the circuit 24b and reheated in the circuit 24a, the exchanger circuit also making it possible to cool and reliquefy the gas previously cooled in the circuit 42 b. Loop 42a allows for reheating of the sampled BOG. The circuit 25b ensures heating of the two-phase mixture and complete evaporation of the remaining liquid, and the circuit 25a ensures cooling. The temperature at the outlet of the circuit 25b is higher than-50 ℃ (for example higher than or equal to-35 ℃), which makes it possible to use a compressor 26 which is cheaper than a cryogenic compressor (which can operate at temperatures well below-50 ℃). Furthermore, this temperature level ensures that all the liquefied gas is completely evaporated at the outlet of the circuit 25b and therefore in gaseous form, and therefore in gaseous form at the inlet of the compressor 26.
Fig. 5 shows another variant embodiment, and fig. 6 and 7 show the mode of operation of this variant.
In this variant, the pumps 16a and 16b are replaced by a single pump 16c, which pump 16c is immersed in the liquefied gas contained in the container 14 and whose outlet is connected on the one hand to the three-way valve 38a and on the other hand to the divaricating member 50, so that it is possible to supply one or even both of the two circuits 24a, 24b of the exchanger 24.
By comparing the variants of fig. 4 and 5, it can be seen that the exchangers forming the heater 25 on the one hand, and the exchanger 42 on the other hand, are combined to form a single exchanger 52.
The exchanger 52 comprises two circuits, a first circuit 52a connecting the outlet of the circuit 24a of the exchanger 24 to the inlet of the compressor 26, and a second circuit 52b connecting the outlet of the compressor 26 to the compressor 28 or to the compressor(s) 28.
The function of the circuit 42b of the exchanger 42 is here integrated into the circuit 52b, the inlet of the circuit 52b also being connected to the outlet of the compressor 28, and the outlet of the circuit 52b also being connected to the circuit 24c of the exchanger 24.
Moreover, the BOG outlet 45 is connected, on the one hand, to the inlet of the circuit 52a, which integrates the function of the circuit 42a, and, on the other hand, to the inlet of the compressor 28. The outlet of circuit 52a is further connected to the inlet of compressor 28.
Fig. 6 shows a first mode of operation of this variant, in which BOG is taken from the vessel 14 through the outlet 45 and fed to the compressor 28. In parallel, the liquefied gas is drawn by the pump 16c and supplied to the circuits 24a, 24b of the exchanger 24. The liquefied gas cooled in circuit 24b is re-injected at the bottom of the container and the liquefied gas expanded by valve 19 enters circuit 24a and is completely in gaseous form at the outlet of circuit 52 a. The gas is compressed by compressor 26 before being cooled in loop 52b and supplied to compressor 28.
Fig. 7 shows a second mode of operation of this variant, in which BOG is withdrawn from the vessel 14 through the outlet 45 and enters the circuit 52a, where it is reheated before being fed to the compressor 28. A portion of the compressed gas exiting compressor 28 flows in loop 52b and then in loop 24c, and is then reliquefied and re-injected into vessel 14.

Claims (25)

1. Device (10) for producing a gas in gaseous form from a liquefied gas, comprising:
a first heat exchanger (24) comprising:
a first cooling circuit (24a) comprising a liquefied gas inlet connected to a first line (18) for connection to a liquefied gas outlet of at least one liquefied gas storage tank (14),
a second cooling circuit (24b) comprising a liquefied gas inlet connected to a third line (30) for connection to a liquefied gas outlet of the tank (14),
means (19) for evaporation by depressurization, equipped with the first line (18), and
at least one compressor (26,28),
a heater (25,52) comprising an inlet for a gas at least partially in liquid form connected to the outlet of the first circuit (24a) and an outlet for a gas only in gaseous form connected to the at least one compressor (26,28), and
characterized in that said first heat exchanger (24) also comprises a further heating circuit (24c) comprising an inlet for gas in gaseous form connected to the outlet of said compressor (28) and a gas outlet connected to means (35, 34, 22) for injecting liquefied gas into the tank (14).
2. The apparatus (10) of claim 12, wherein the first circuit (24a) is configured to heat fluid circulating therein from a temperature less than or equal to-165 ℃ to a temperature greater than or equal to-165 ℃.
3. The device (10) according to claim 1 or 2, wherein the heater (25) is a heat exchanger comprising a third circuit (25b) comprising an inlet for gas at least partially in liquid form connected to the outlet of the first circuit (24a) and an outlet for gas only in gaseous form connected to the at least one compressor (26, 28).
4. The device according to claim 3, wherein the inlet of the third circuit is also connected to an outlet (45) for gaseous gas from the tank (14).
5. The device (10) according to claim 3 or 4, wherein said third circuit is configured to heat the fluid circulating therein from a temperature less than or equal to-165 ℃ to a temperature greater than or equal to-50 ℃.
6. Device (10) according to any one of claims 3 to 5, wherein the exchanger forming the heater (25) comprises a fourth circuit (25a) in which a heating fluid circulates.
7. The device (10) according to claim 6, wherein said fourth circuit (25a) is configured to cool the fluid circulating therein from a temperature greater than or equal to 50 ℃ to a temperature less than or equal to 0 ℃.
8. The device (10) according to claim 6 or 7, wherein the heating fluid is a compressed gas taken from the outlet of the at least one compressor (26, 28).
9. Device (10) according to claim 8, wherein the outlet, preferably a single outlet, of said at least one compressor (26) is connected to the inlet of said fourth circuit (25a) forming an exchanger of the heater (25).
10. Device (10) according to claim 9, wherein it comprises at least two compressors (26,28) mounted in series, the outlet of the upstream compressor (26) being connected to the inlet of the fourth circuit (25a) forming an exchanger of the heater (25), one outlet of the fourth circuit being connected to the inlet of the downstream compressor (28).
11. Device (10) according to claim 9, wherein it comprises at least two compressors (26,28) mounted in series, the outlet of the upstream compressor (26) being connected to the inlet of the downstream compressor (28), the outlet of the downstream compressor being connected to the inlet of the fourth circuit (25a) forming the exchanger of the heater (25).
12. The device according to any one of claims 6 to 11, wherein the fourth circuit (25a) has an outlet connected to at least one compressor (28).
13. The device (10) according to any one of the preceding claims, wherein the second circuit (24b) is, in turn, a cooling circuit and a heating circuit, depending on the operating mode of the device.
14. The device (10) according to any one of the preceding claims, wherein the second circuit (24b) is configured to cool the fluid circulating therein from a temperature of less than or equal to-160 ℃ to a temperature of less than or equal to-165 ℃ and/or the further circuit (24c) is configured to cool the fluid circulating therein from a temperature of less than or equal to-100 ℃ to a temperature of less than or equal to-130 ℃.
15. The device according to any one of claims 6 to 13, wherein the outlet of the fourth circuit (25a) is also connected to the inlet of the further circuit (24 c).
16. Apparatus (10) according to claim 15, wherein the apparatus comprises a fifth line (34) equipped with expansion means (36) and comprising an inlet connected to the outlet of the further circuit (24c) and an outlet for liquefied gas connected to the tank (14).
17. Device (10) according to claim 16, wherein the device comprises a sixth line (32) having an inlet connected to the outlet of the second circuit (24b), the outlet of the sixth line being connected to the liquefied gas inlet of the tank.
18. The device (10) according to any one of the preceding claims, wherein the gas inlet of the further circuit (24c) is connected to the outlet of the compressor (28) through a sixth circuit (42b) of second heat exchangers (42).
19. The device (10) according to claim 18, wherein the sixth circuit (42b) is configured to cool the fluid circulating therein from a temperature greater than or equal to 0 ℃ to a temperature less than or equal to-100 ℃.
20. The device (10) according to claim 19, wherein the second heat exchanger (42) comprises a seventh circuit (42a) whose inlet is connected to an outlet (45) for the gaseous gas from the tank (14) and whose outlet is connected to the compressor (28).
21. The device (10) according to claim 20, wherein said seventh circuit is (42a) configured to heat the fluid circulating therein from a temperature less than or equal to-100 ℃ to a temperature greater than or equal to-50 ℃.
22. Vessel, in particular for transporting liquefied gases, comprising at least one device according to any of the preceding claims.
23. A method of producing gas in gaseous form from liquefied gas by means of a device according to any one of claims 1 to 21, characterised in that the method comprises: a step of extracting the liquefied gas and completely evaporating the gas before supplying the at least one compressor (26, 28).
24. Method according to claim 23, wherein evaporation is obtained by heating the liquefied gas with a heating fluid, the heating fluid being a compressed gas taken from an outlet of the at least one compressor (26, 28).
25. A method according to claim 24, wherein the compressed gas is extracted between or at the outlet of two compressors (26,28) mounted in series.
CN201980079322.0A 2018-11-30 2019-11-29 Device for producing gaseous gases from liquefied gases Active CN113316696B (en)

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FR1872123A FR3089274B1 (en) 2018-11-30 2018-11-30 Device for generating gas in gaseous form from liquefied gas
PCT/EP2019/083187 WO2020109607A1 (en) 2018-11-30 2019-11-29 Device for generating gas in gaseous form from liquefied gas

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FR3121504B1 (en) * 2021-04-01 2023-04-14 Gaztransport Et Technigaz Method for cooling a heat exchanger of a gas supply system of a gas-consuming device of a ship

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CN113316696B (en) 2023-09-26
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WO2020109607A1 (en) 2020-06-04
FR3089274B1 (en) 2022-03-04

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