• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
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  • 优先权
    • 专利摘要:
    The device (100) for supplying liquefied natural gas, called "LNG", comprises: an evaporation gas buffer tank (105) comprising an inlet (110) for evaporation gas adapted to receive evaporation gas from a third device, - an evaporation gas transfer member (115) from the buffer tank to an LNG storage tank (120), - an evaporation gas transfer line (125) from the transfer member to the storage capacity, - the LNG storage capacity, - an LNG transfer line (130) from the storage capacity to a third-party device and - a heat exchanger (135) between evaporation gas passing through the evaporation gas transfer line and LNG passing through the LNG transfer line configured to liquefy or cool the evaporation gas.
    公开号:FR3074254A1
    申请号:FR1761146
    申请日:2017-11-24
    公开日:2019-05-31
    发明作者:Hicham Guedacha；Hugues Malvos；Yacine Zellouf
    申请人:Engie SA；
    IPC主号:
    专利说明:

    TECHNICAL FIELD OF THE INVENTION
    The present invention relates to a device and a method for supplying LNG. It applies, in particular, to the LNG supply area suitable for land and maritime vehicles.
    STATE OF THE ART
    The use of liquefied natural gas (hereinafter "LNG") as road or marine fuel is booming, promoted by the environmental and economic benefits that LNG provides compared to other fossil fuels.
    In general, LNG service stations are composed of an LNG reception system, of cryogenic storage making it possible to store LNG in the sub-cooled state having an operating pressure generally between 7 and 9 bar, a cryogenic pump for transferring the LNG and a distribution system to supply the vehicle.
    Today, three categories of vehicles are likely to be supplied with LNG:
    - a first category supplied with cold LNG (or "cold LNG"), that is to say having a pressure of 3 bar,
    - a second category that feeds on LNG says "saturated" (or "saturated LNG") with a pressure of 8 bar and
    - a third category that feeds on LNG says "super saturated" (or "super saturated LNG") with a pressure of 18 bar.
    Today, vehicles with a pressure of 8 bar are the majority. The vaporization of LNG created from BOG, for "Boil-off gas", is relatively high during refueling of 8 bar and 18 bar vehicles. Vehicle tanks have been sized to withstand pressure surges, but the design of this equipment is nevertheless limited by a maximum allowable pressure.
    A gas return from the vehicle to the station is then carried out in order to avoid reaching this maximum pressure leading thereafter to a significant release of gas into the atmosphere.
    This gas return within the LNG storage represents a heat source for the LNG, which favors the evaporation of LNG and therefore the increase of the pressure inside the storage. These evaporations or BOGs must be managed without being released into the atmosphere.
    In addition to the product losses generated, this adds to the operational complexity of the site.
    In addition, the LNG stored in the storage tank of the service station is generally in the sub-cooled state. The heat source for bringing the LNG to saturation (at 8 bar and 18 bar) comes from the open air, requiring the installation of substantial exchanger surface on site.
    On the other hand, two methods exist for supplying LNG fuel to vehicles 8 and 18 bar:
    - the “Bulk saturation” method which consists in storing LNG at saturation and
    - a method consisting in using "LNG saturation on the fly" packaging which aims to supply saturated LNG from sub-cooled LNG.
    It is known, with regard to compressed LNG stations, or GNLC, the storage of the return gas is in a buffer tank for CNG use. Some LNG stations accept the return of gas and do not care about its impact on the generation of BOG. These stations are generally equipped with a BOG liquefaction system.
    Current solutions use air vaporizers are used to obtain saturated LNG, requiring substantial exchange surfaces and a large footprint.
    The so-called “saturation on the fly” systems have the drawbacks of requiring very efficient and expensive exchangers and of requiring a very complex control system, which poses a problem of operational stability.
    Finally, bulk saturation systems cannot supply vehicles operating at a pressure of 3 bar and have a reduced storage capacity and storage time.
    It should be noted that in the case of stations equipped with BOG liquefaction systems, these systems are expensive and have no possible return on investment.
    OBJECT OF THE INVENTION
    The present invention aims to remedy all or part of these drawbacks.
    To this end, according to a first aspect, the present invention relates to a device for supplying liquefied natural gas, called "LNG", which comprises:
    - an evaporative gas buffer tank comprising an inlet for evaporative gas adapted to receive evaporative gas from a third-party device,
    - an evaporation gas transfer device from the buffer tank to an LNG storage capacity,
    - an evaporation gas transfer line from the transfer member to the storage capacity,
    - LNG storage capacity,
    - an LNG transfer line from the storage capacity to a third-party device, and
    - a heat exchanger between evaporation gas passing through the evaporation gas transfer line and LNG passing through the LNG transfer line configured to liquefy or cool the evaporation gas.
    Thanks to these provisions, the evaporation gas transferred from the buffer tank to the storage capacity is liquefied, which makes it possible to keep the LNG stored in the capacity at a low temperature limiting the formation of BOG within this capacity.
    In embodiments, the device which is the subject of the present invention comprises, downstream of the transfer member, a compressor for the evaporating gas.
    These embodiments improve the performance of the device in terms of liquefaction of the evaporating gas.
    In embodiments, the transfer member is a valve controlled as a function of a pressure value inside the buffer tank detected, by a pressure sensor, or an overflow valve.
    In embodiments, the evaporating gas and the LNG flow counter-currently inside the heat exchanger.
    These embodiments improve the performance of the device in terms of liquefaction of the evaporating gas.
    In embodiments, the buffer tank has an operating pressure value at least two bars higher than the operating pressure value of the storage capacity.
    These embodiments allow a natural flow of the evaporation gas from the buffer tank to the storage capacity.
    In embodiments, the device which is the subject of the present invention comprises, downstream of the heat exchanger, a diversion of the transfer line for the liquefied or cooled evaporation gas in the heat exchanger, the supply of evaporation at the deflection being controlled as a function of a temperature sensed by a temperature sensor of the evaporation gas at the outlet of the heat exchanger.
    These embodiments make it possible to recycle evaporation gas which does not reach a determined temperature value.
    In embodiments, the device which is the subject of the present invention comprises, on the deflection, a first valve and, on the evaporation gas transfer pipe downstream of the deflection, a second valve, the opening of the first or the second valve being controlled as a function of the temperature of the captured evaporating gas.
    These embodiments make it possible to recycle evaporation gas which does not reach a determined temperature value.
    In embodiments, the device which is the subject of the present invention comprises a member for transferring liquefied evaporation gas from the buffer tank to the LNG transfer pipe.
    These embodiments allow saturation of the LNG transferred to the third-party device.
    In embodiments, the device which is the subject of the present invention comprises:
    - an evaporation gas extraction pipe inside the storage capacity,
    - an evaporative gas compressor passing through the extraction pipe and
    - a pipe for supplying compressed evaporation gas to the buffer tank.
    These embodiments make it possible to minimize the storage volume required by the buffer tank.
    In embodiments, the evaporative gas compressor has the inlet for evaporative gas adapted to receive evaporative gas from a third party device.
    In embodiments, the device which is the subject of the present invention comprises means for cooling the flow of evaporation gas downstream from the transfer member.
    These embodiments make it possible to cool or liquefy, in part or in whole, a flow of evaporating gas at the outlet of the heat exchanger.
    In embodiments, the device which is the subject of the present invention comprises, downstream of the heat exchanger, a gas flow regulator configured to expand the flow of evaporating gas to a determined pressure.
    In embodiments, the device which is the subject of the present invention comprises, downstream of the regulator, a gas / liquid separator, the gaseous evaporation gas being supplied to the deflection and the liquid evaporation gas being supplied to the capacity of storage.
    According to a second aspect, the present invention relates to a method for supplying liquefied natural gas, called "LNG", which comprises:
    a step for storing evaporating gas from a third-party device in a evaporating gas buffer tank comprising an inlet for evaporating gas adapted to receive evaporating gas coming from a third-party device,
    - a step of transferring evaporation gas from the buffer tank to an LNG storage capacity,
    - a heat exchange step between the evaporative gas transferred and the LNG transferred to a third-party device originating from the LNG storage capacity for liquefying or cooling the evaporative gas,
    - an LNG storage step in the storage capacity,
    - a LNG transfer step from the storage capacity to a third-party device.
    The aims, advantages and particular characteristics of the method which is the subject of the present invention being similar to those of the device which is the subject of the present invention, they are not repeated here.
    BRIEF DESCRIPTION OF THE FIGURES
    Other advantages, aims and particular characteristics of the invention will emerge from the non-limiting description which follows of at least one particular embodiment of the device and of the method which are the subject of the present invention, with reference to the appended drawings, in which:
    FIG. 1 schematically represents a first particular embodiment of the device which is the subject of the present invention,
    FIG. 2 represents, diagrammatically and in the form of a flow diagram, a succession of particular steps of the method which is the subject of the present invention,
    - Figure 3 shows, schematically, a second particular embodiment of the device object of the present invention.
    DESCRIPTION OF EXAMPLES OF EMBODIMENT OF THE INVENTION
    This description is given without limitation, each characteristic of an embodiment can be combined with any other characteristic of any other embodiment in an advantageous manner.
    We note now that the figures are not to scale.
    Thereafter, we call "third party device", any device consuming LNG to produce energy. Such a third-party device is, for example, a land, sea, river or air vehicle.
    FIG. 1, which is not to scale, shows a schematic view of an embodiment of the device 100 which is the subject of the present invention. This device 100 for supplying liquefied natural gas, called “LNG”, comprises:
    - a reservoir 105 evaporative gas buffer comprising an inlet 110 for evaporative gas adapted to receive evaporative gas from a third-party device,
    - an organ 120 for transferring evaporation gas from the buffer tank to an LNG storage capacity 115,
    a pipe 125 for transferring evaporation gas from the transfer member to the storage capacity,
    - LNG storage capacity,
    an LNG transfer pipe 130 from the storage capacity to a third-party device, and
    - a heat exchanger 135 between evaporation gas passing through the evaporation gas transfer line and LNG passing through the LNG transfer line configured to liquefy or cool the evaporation gas.
    The tank 105 is, for example, an evaporation gas storage volume designed to retain a predetermined amount of evaporation gas within a determined pressure range. The inlet 110 is, for example, an orifice made in the storage volume and configured to receive a member for injecting the evaporation gas into the volume. Such an injection member is, for example, a nozzle or a one-way valve.
    This reservoir 105 is configured, for example, to operate at an operating pressure greater than 11 barg.
    This tank 105 has, for example, a capacity of one cubic meter and the capacity 115 has, for example, a capacity of eighty cubic meters.
    Input 110 is preferably connected to a connector with the third-party device configured to collect the return of evaporation gas. The type of connector depends on the standard used by the third-party device and on the purpose of the device 100 envisaged.
    The supply of evaporation gas from the third-party device to the tank 105 is carried out, for example, by pressure gradient.
    This reservoir 105 is provided, preferably in the upper part, with an outlet for evaporating gas connected to the transfer member 115. The transfer member 115 is, for example, an overflow valve or a valve controlled as a function of a pressure value sensed inside the reservoir 105. This pressure value is sensed, for example, by a pressure sensor 145 . When the sensed pressure is greater than a set value, the valve is opened.
    The choice of this set value is arbitrary and fixed by the operator. It depends on the station's design and cost objectives. A set pressure of 15 or 16 bar if the station is sized to supply vehicles operating at 18 bar can be implemented, for example.
    The gas transfer pipe 125 connects the transfer member 115 to the storage capacity 115. Preferably, the device 100 comprises, downstream of the transfer member 120, a compressor 140 or a booster.
    At the outlet of the compressor 140 or of the booster, the gas has sufficient pressure to overcome the pressure drops in the circuit and allow the recycle to be carried out. The choice of discharge pressure is set according to the station's design objectives and the operating mode desired by the operator.
    The evaporation gas, compressed or not by the compressor 140 depending on the presence of this compressor 140 in the device 100, passes through the heat exchanger 135.
    The heat exchanger 135 is, for example, a fin or plate exchanger between the evaporation gas passing through the transfer line 125 and the LNG passing through the transfer line 130. The evaporating gas acts as a hot fluid and the LNG as a cold fluid so that the outlet temperature of the evaporating gas is cooler than the inlet temperature of the evaporating gas in the exchanger 135 thermal. Preferably, the heat exchanger 135 is designed so that the evaporating gas is liquefied or cooled at the outlet of the heat exchanger 135 for determined flows of LNG and evaporating gas.
    The heat exchanger 135 is also provided for, preferably, heating the LNG to a determined temperature. As a function of said temperature, the gas flow rate passing through the transfer line 125 is adjusted. If the LNG temperature needs to be increased, the gas transfer rate in line 125 is increased.
    Preferably, the LNG and the evaporating gas flow in counter-current so as to optimize the heat exchange between the two fluids.
    The storage capacity 115 is, for example, an evaporation gas storage volume designed to retain a predetermined quantity of LNG within a determined pressure range. The capacity 115 preferably includes an inlet for liquefied evaporation gas. This inlet is, for example, an orifice made in the storage capacity and configured to receive a member for injecting the liquefied evaporation gas into the volume. Such an injection member is, for example, a nozzle or a one-way valve.
    The capacity 115 is configured to operate, for example, at an operating pressure between 7 and 9 bar.
    Preferably, the operating pressure inside the storage capacity 115 is at least two bar lower than the operating pressure inside the buffer tank 105.
    The capacity 115 is provided with an LNG outlet, preferably in the lower part, connected to the transfer pipe 130.
    The transfer line 130 is connected to a connector, the nature of which depends on the type of third-party device connected to the device 100.
    In variants, the device 100 includes a pump 116 configured to facilitate the transfer of the LNG from the capacity 115 to the third-party device.
    In preferred embodiments, such as that shown in FIG. 1, the device 100 comprises, downstream of the heat exchanger 135, a deflection 150 of the pipe 125 for transferring the liquefied or cooled evaporation gas in the exchanger thermal, the supply of evaporation gas to the deflection being controlled as a function of a temperature sensed by a sensor 155 for the temperature of the evaporation gas at the outlet of the heat exchanger.
    In preferred embodiments, such as that shown in FIG. 1, the device 100 comprises, on the deflection 150, a first valve 160 and, on the pipe 125 for transferring evaporation gas downstream of the deflection, a second valve 165, the opening of the first or second valve being controlled as a function of the temperature of the captured evaporating gas.
    When the evaporating gas has a temperature below a predetermined threshold value, the first valve 160 is open and the second valve 165 closed. Conversely, when the evaporating gas has a temperature above the predetermined threshold value, the first valve 160 is closed and the second valve 165 open.
    In preferred embodiments, such as that shown in FIG. 1, the device 100 comprises a member 170 for transferring liquefied evaporation gas from the buffer tank 105 to the line 130 for transferring LNG.
    The member 170 is, for example, a valve controlled as a function of the pressure sensed inside the storage tank 105 by a pressure sensor 171.
    FIG. 3, which is not to scale, shows a schematic view of an embodiment of the device 200 which is the subject of the present invention. This device 200 for supplying liquefied natural gas, called “LNG”, comprises:
    - a reservoir 105 evaporative gas buffer comprising an inlet 110 for evaporative gas adapted to receive evaporative gas from a third-party device,
    - a device 115 for transferring evaporation gas from the buffer tank to a capacity 120 for storing LNG,
    a pipe 125 for transferring evaporation gas from the transfer member to the storage capacity,
    - LNG storage capacity,
    an LNG transfer pipe 130 from the storage capacity to a third-party device, and
    - a heat exchanger 135 between evaporation gas passing through the evaporation gas transfer line and LNG passing through the LNG transfer line configured to liquefy or cool the evaporation gas.
    The tank 105 is, for example, an evaporation gas storage volume designed to retain a predetermined amount of evaporation gas within a determined pressure range. The inlet 110 is, for example, an orifice made in the storage volume and configured to receive a member for injecting the evaporation gas into the volume. Such an injection member is, for example, a nozzle or a one-way valve.
    The reservoir 105 is, for example, configured to operate at an operating pressure greater than 30 bar.
    This tank 105 has, for example, a capacity of one cubic meter and the capacity 115 has, for example, a capacity of eighty cubic meters.
    Input 110 is preferably connected to a connector with the third-party device configured to collect the return of evaporation gas. The type of connector depends on the standard used by the third-party device and on the intended purpose of the device 200.
    The supply of evaporation gas from the third-party device to the tank 105 is carried out, for example, by pressure gradient or by the use of a booster.
    This reservoir 105 is provided, preferably in the upper part, with an outlet for evaporating gas connected to the transfer member 115. The transfer member 115 is, for example, an overflow valve or a valve controlled as a function of a pressure value sensed inside the reservoir 105. This pressure value is sensed, for example, by a pressure sensor 145 . When the sensed pressure is greater than a set value, the valve is opened.
    The set value is chosen, for example, to correspond to the maximum operating pressure of capacity 105. Note that the operator can also allow gas transfer remotely without this maximum pressure being reached if necessary, by one second all or nothing valve, for example.
    The gas transfer pipe 125 connects the transfer member 115 to the storage capacity 115. Preferably, the device 200 comprises, downstream of the transfer member 120, a compressor 140.
    At the outlet of the compressor 140, the gas has, for example, a pressure greater than or equal to 50 bar.
    The evaporation gas, compressed or not by the compressor 140 depending on the presence of this compressor 140 in the device 200, passes through the heat exchanger 135.
    In embodiments, such as that shown in FIG. 3, the device 200 comprises a means 126 for cooling the flow of evaporation gas downstream from the transfer member 120. This cooling means 126 is, for example, a heat exchanger using liquid nitrogen as cold fluid. At the outlet of the heat exchanger 135, the flow of evaporating gas is preferably two-phase, that is to say partially liquid and partially gaseous, or more generally cooled. This flow can be injected into the storage capacity 115.
    In embodiments, such as that shown in FIG. 3, the device 200 comprises, downstream of the heat exchanger 135, a gas flow regulator 136 configured to relax the flow of evaporating gas to a determined pressure.
    In embodiments, such as that shown in FIG. 3, the device 200 comprises, downstream of the regulator 136, a gas / liquid separator 137, the gaseous evaporation gas being supplied to the deflection 150 and the evaporation gas liquid being supplied to the storage capacity 115.
    The separator 137 is, for example, a separation flask.
    The heat exchanger 135 is, for example, a fin or plate exchanger between the evaporation gas passing through the transfer line 125 and the LNG passing through the transfer line 130. The evaporating gas acts as a hot fluid and the LNG as a cold fluid so that the outlet temperature of the evaporating gas is cooler than the inlet temperature of the evaporating gas in the exchanger 135 thermal. Preferably, the heat exchanger 135 is designed so that the evaporating gas is liquefied or cooled at the outlet of the heat exchanger 135 for determined flows of LNG and evaporating gas.
    The heat exchanger 135 is also provided for, preferably, heating the LNG to a determined temperature. As a function of said temperature, the gas flow rate passing through the transfer line 125 is adjusted. If the LNG temperature needs to be increased, the gas transfer rate in line 125 is increased.
    Preferably, the LNG and the evaporating gas flow in counter-current so as to optimize the heat exchange between the two fluids.
    The storage capacity 115 is, for example, an evaporation gas storage volume designed to retain a predetermined quantity of LNG within a determined pressure range. The capacity 115 preferably includes an inlet for liquefied evaporation gas. This inlet is, for example, an orifice made in the storage capacity and configured to receive a member for injecting the liquefied evaporation gas into the volume. Such an injection member is, for example, a nozzle or a one-way valve.
    The capacity 115 has, for example, an operating pressure value of between 7 and 9 bar.
    Preferably, the operating pressure inside the storage capacity 115 is at least two bar lower than the operating pressure inside the buffer tank 105.
    The capacity 115 is provided with an LNG outlet, preferably in the lower part, connected to the transfer pipe 130.
    The transfer line 130 is connected to a connector, the nature of which depends on the type of third-party device connected to the device 200.
    In variants, the device 200 comprises a pump 116 configured to facilitate the transfer of the LNG from the capacity 115 to the third-party device.
    In preferred embodiments, such as that shown in FIG. 3, the device 200 comprises, downstream of the heat exchanger 135, a deflection 150 of the pipe 125 for transferring the liquefied or cooled evaporation gas in the exchanger thermal, the supply of evaporation gas to the deflection being controlled as a function of a temperature sensed by a sensor 155 for the temperature of the evaporation gas at the outlet of the heat exchanger.
    In preferred embodiments, such as that shown in FIG. 3, the device 200 comprises, on the deflection 150, a first valve 160 and, on the pipe 125 for transferring evaporation gas downstream of the deflection, a second valve 165, the opening of the first or second valve being controlled as a function of the temperature of the captured evaporating gas.
    When the evaporating gas has a temperature below a predetermined threshold value, the first valve 160 is open and the second valve 165 closed. Conversely, when the evaporating gas has a temperature above the predetermined threshold value, the first valve 160 is closed and the second valve 165 open.
    In preferred embodiments, such as that shown in FIG. 3, the device 200 includes a member 170 for transferring liquefied evaporation gas from the buffer tank 105 to the LNG transfer pipe 130.
    The member 170 is, for example, a valve controlled as a function of the pressure sensed inside the storage tank 105 by a pressure sensor 171.
    In preferred embodiments, such as that shown in FIG. 3, the device 200 comprises:
    - a line 205 for extracting evaporative gases inside the storage capacity 115,
    - a compressor 210 for the evaporation gas passing through the extraction pipe and
    - a pipe 215 for supplying the compressed evaporation gas to the buffer tank 105.
    Line 205 is preferably connected in the upper part of storage capacity 115.
    The compressor 210 is configured to, for example, bring the gas pressure to a value greater than 30 bar.
    In preferred embodiments, such as that shown in FIG. 3, the evaporative gas compressor 210 has the inlet 110 for evaporative gas adapted to receive evaporative gas from a third-party device.
    FIG. 2 schematically shows a particular embodiment of the method 300 which is the subject of the present invention. This method 300 for supplying liquefied natural gas, called "LNG", characterized in that it comprises:
    a step 305 of storing evaporating gas from a third-party device in a evaporating gas buffer tank comprising an inlet for evaporating gas adapted to receive evaporating gas coming from a third-party device,
    a step 310 of transferring evaporation gas from the buffer tank to an LNG storage capacity,
    a step 315 of heat exchange between the evaporation gas transferred and the LNG transferred to a third-party device originating from the LNG storage capacity for liquefying or cooling the evaporation gas,
    a step 320 of LNG storage in the storage capacity,
    a step 325 of transferring LNG from the storage capacity to a third party device.
    The operation of this method 200 is achieved, for example, by the implementation of the devices, 100 and 300, as described with reference to Figures 1 and 3, all the variants and embodiments of the devices 100 and 300 being able to be transposed in the form of process steps 200.
    权利要求:
    Claims (14)
    [1" id="c-fr-0001]
    1. Device (100, 200) for supplying liquefied natural gas, called "LNG", characterized in that it comprises:
    - a reservoir (105) of evaporative gas buffer comprising an inlet (110) for evaporative gas adapted to receive evaporative gas from a third-party device,
    - an organ (120) for transferring evaporation gas from the buffer tank to an LNG storage capacity (115),
    - a pipe (125) for transferring evaporation gas from the transfer member to the storage capacity,
    - LNG storage capacity,
    - an LNG transfer pipe (130) from the storage capacity to a third-party device, and
    - a heat exchanger (135) between evaporation gas passing through the evaporation gas transfer line and LNG passing through the LNG transfer line configured to liquefy or cool the evaporation gas.
    [2" id="c-fr-0002]
    2. Device (100, 200) according to claim 1, which comprises, downstream of the transfer member (120), a compressor (140) of the evaporation gas.
    [3" id="c-fr-0003]
    3. Device (100, 200) according to one of claims 1 or 2, wherein the transfer member (120) is a valve controlled as a function of a pressure value inside the buffer tank (105) detected by a pressure sensor (145) or an overflow valve.
    [4" id="c-fr-0004]
    4. Device (100, 200) according to one of claims 1 to 3, in which the evaporation gas and the LNG circulate against the current inside the heat exchanger (135).
    [5" id="c-fr-0005]
    5. Device (100, 200) according to one of claims 1 to 4, in which the buffer tank (105) has an operating pressure value greater by at least two bar than the operating pressure value of the capacity (115 ) storage.
    [6" id="c-fr-0006]
    6. Device (100, 200) according to one of claims 1 to 5, which comprises, downstream of the heat exchanger (135), a deflection (150) of the pipe (125) for transferring the evaporation gas liquefied or cooled in the heat exchanger, the supply of evaporation gas to the deflection being controlled as a function of a temperature sensed by a sensor (155) of temperature of the evaporation gas at the outlet of the heat exchanger.
    [7" id="c-fr-0007]
    7. Device (100, 200) according to claim 6, which comprises, on the deflection (150), a first valve (160) and, on the pipe (125) for transferring evaporation gas downstream of the deflection, a second valve (165), the opening of the first or of the second valve being controlled as a function of the temperature of the captured evaporating gas.
    [8" id="c-fr-0008]
    8. Device (100, 200) according to one of claims 1 to 7, which comprises a member (170) for transferring liquefied evaporation gas from the buffer tank (105) to the LNG transfer pipe (130) .
    [9" id="c-fr-0009]
    9. Device (200) according to one of claims 1 to 8, which comprises:
    - an evaporation gas extraction pipe (205) inside the storage capacity (115),
    - a compressor (210) for the evaporation gas passing through the extraction pipe and
    - a pipe (215) for supplying the compressed evaporation gas to the buffer tank (105).
    [10" id="c-fr-0010]
    10. Device (200) according to claim 9, wherein the evaporator gas compressor (210) has the inlet (110) for evaporator gas adapted to receive evaporator gas from a third party device.
    [11" id="c-fr-0011]
    11. Device (200) according to one of claims 1 to 10, which comprises means (126) for cooling the flow of evaporation gas downstream of the transfer member (120).
    [12" id="c-fr-0012]
    12. Device (200) according to claim 11, which comprises, downstream of the heat exchanger (135), a gas flow regulator (136) configured to expand the flow of evaporating gas to a determined pressure.
    [13" id="c-fr-0013]
    13. Device (200) according to claim 12 and claim 6, which comprises, downstream of the regulator (136), a gas / liquid separator (137), the gaseous evaporation gas being supplied to the deflection (150) and the liquid evaporation gas being supplied to the storage capacity (115).
    [14" id="c-fr-0014]
    14. Method (300) for supplying liquefied natural gas, called "LNG", characterized in that it comprises:
    a step (305) of storing evaporation gas from a third-party device in a buffer tank for evaporation gas comprising an inlet for evaporation gas adapted to receive evaporation gas from a third-party device ,
    - a step (310) of transferring evaporation gas from the buffer tank to an LNG storage capacity,
    a step (315) of heat exchange between the evaporation gas transferred and the LNG transferred to a third-party device originating from the LNG storage capacity for liquefying or cooling the evaporation gas,
    - a step (320) of LNG storage in the storage capacity,
    - A step (325) of transferring LNG from the storage capacity to a third-party device.
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    FR3079006A1|2019-09-20|PRESSURE GAS TANK | FILLING STATION AND METHOD FOR INCREASING ITS AUTONOMY
    同族专利:
    公开号 | 公开日
    KR20200093571A|2020-08-05|
    WO2019102155A1|2019-05-31|
    SG11202005304VA|2020-07-29|
    FR3074254B1|2021-06-04|
    CN111630312A|2020-09-04|
    US20200370709A1|2020-11-26|
    EP3714201A1|2020-09-30|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    FR2131238A5|1970-10-23|1972-11-10|Cryogenic Engineering Cy|
    EP1776541A1|2004-08-07|2007-04-25|Messer France S.A.|Method and device for filling a container with liquid gas from a storage tank|
    DE102007023821A1|2007-05-21|2008-11-27|Bayerische Motoren Werke Aktiengesellschaft|Method for filling cryogenic hydrogen tank on vehicle has residual gas tapped off to be conditioned at lower temperature before returning to cool the tank prior to filling with fresh gas|
    US20130263609A1|2012-04-04|2013-10-10|Gp Strategies Corporation|Pumpless fluid dispenser|
    US20140202583A1|2013-01-22|2014-07-24|Ron C. Lee|Methods for liquefied natural gas fueling|
    FR3017184A1|2014-02-03|2015-08-07|Cryostar Sas|CRYOGENIC LIQUID DELIVERY AND TREATMENT FACILITY|
    CN1332327A|2001-07-18|2002-01-23|青岛化工设计院|Liquefied natural gas gasifying supplier|
    CN100451436C|2005-08-10|2009-01-14|中国石油天然气股份有限公司|Storage conveying method and device for liquiefied natural gas|
    CN204573577U|2015-04-15|2015-08-19|陈东升|A kind of safe LNG stores conveying integrated device|FR3106391A1|2020-01-17|2021-07-23|L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude|Installation and method for storing and distributing cryogenic fluid|
    KR102243009B1|2020-06-23|2021-04-22|발맥스기술|Control method and refrigerant charging system of LNG filling station|
    CN112432053A|2020-11-19|2021-03-02|深圳市凯丰实业发展有限公司|Zero discharge system device of liquid nitrogen storage tank|
    法律状态:
    2019-05-31| PLSC| Publication of the preliminary search report|Effective date: 20190531 |
    2019-10-22| PLFP| Fee payment|Year of fee payment: 3 |
    2020-10-21| PLFP| Fee payment|Year of fee payment: 4 |
    2021-10-20| PLFP| Fee payment|Year of fee payment: 5 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1761146|2017-11-24|
    FR1761146A|FR3074254B1|2017-11-24|2017-11-24|DEVICE AND METHOD FOR SUPPLYING LIQUEFIED NATURAL GAS|FR1761146A| FR3074254B1|2017-11-24|2017-11-24|DEVICE AND METHOD FOR SUPPLYING LIQUEFIED NATURAL GAS|
    PCT/FR2018/052957| WO2019102155A1|2017-11-24|2018-11-22|Device and method for providing liquefied natural gas|
    KR1020207017063A| KR20200093571A|2017-11-24|2018-11-22|Apparatus and method for supplying liquefied natural gas|
    EP18819541.6A| EP3714201A1|2017-11-24|2018-11-22|Device and method for providing liquefied natural gas|
    SG11202005304VA| SG11202005304VA|2017-11-24|2018-11-22|Device and method for providing liquefied natural gas|
    CN201880087062.7A| CN111630312A|2017-11-24|2018-11-22|Plant and method for providing liquefied natural gas|
    US16/766,714| US20200370709A1|2017-11-24|2018-11-22|Device and method for providing liquefied natural gas|
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