• 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:
    Installation and method for storage and distribution of liquefied hydrogen comprising a source (2) of gaseous hydrogen, a liquefier (3), two storages (4, 5) of liquid hydrogen at determined respective storage pressures, the liquefier (3) comprising an inlet connected to the source (2) and an outlet connected in parallel, via a valve assembly (7, 6, 16), to a respective inlet of each storage (5, 4), the outlet of the liquefier (3) also being connected to a connection end (15) intended to be removably connected to a reservoir (10) to be filled, each storage (5, 4) comprising a respective liquid withdrawal line (9, 8) comprising one end connected to the storage (4, 5) and at least one other end intended to be connected to one at least one tank (10) to be filled, each storage (4, 5) further comprising a pipe (12, 11) respective gas withdrawal comprising an end connected to the storage (4, 5) and a e other end connected to an inlet of the liquefier (3) via a set of valves (14, 13) configured to allow the recycling of gas to the liquefier (3) for liquefaction.
    公开号:FR3088415A1
    申请号:FR1860429
    申请日:2018-11-12
    公开日:2020-05-15
    发明作者:Jean-Marc Bernhardt；Francois Lagoutte
    申请人:Air Liquide SA；LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude；
    IPC主号:
    专利说明:

    The invention relates to a method and installation for the storage and distribution of liquefied hydrogen.
    The invention relates more particularly to a storage and distribution installation of liquefied hydrogen comprising a source of gaseous hydrogen, a liquefier.
    Due to its density in particular, liquid hydrogen is preferred over gaseous hydrogen when large quantities of product have to be transported over long distances.
    Another advantage of liquid hydrogen is linked to its density and the large storage capacity in a hydrogen filling station for fuel cell vehicles. A temperature of 20K de facto removes all impurities (solid at this temperature) from the gas, which optimizes the functioning of fuel cells.
    On the other hand, due to the low density of liquid hydrogen (70g / liter) compared to water, the pressure available by hydrostatic height and the low temperature can cause fairly significant evaporation losses during liquid transfers.
    In fact, truck loading systems and tanks in hydrogen liquefaction plants can cause losses of up to 15% of production (for example 0.2% tank loss, 5% loss due "flash" in the tank filling valve and 10% loss in truck filling processes). These losses can also occur when filling containers (iso-containers in particular), boat tanks or other (other applications to which the invention can also be applied).
    These evaporation losses can of course be recovered, reheated, compressed after storage and reinjected into the liquefier. Hydrogen is produced from a source of hydrogen gas which is liquefied in a liquefier before it is transferred to storage. The vaporization gas (“boiloff”) can be sampled in a unit comprising, for example, in series, a heater, a buffer tank (for example isobaric), a compression member. The recovered and compressed gas can be admitted to the inlet of the liquefier with a view to its reliquefaction and reintroduction into storage.
    Truck tanks that come to fill usually have a high temperature and high pressure. Part of this hot gas under pressure can be evacuated to the liquid storage which is used for filling. However, part of the depressurization of the tank cannot be carried out towards the liquid storage because the pressure of the truck can become lower than that of the storage. Excessive hydrogen under pressure is therefore lost or sent to a recovery system.
    When the liquefier or the source of hydrogen supplying it is shut down, the liquid storage facilities must make it possible to continue supplying the liquid hydrogen to the users.
    In addition, the cold present in the storage does not make it possible to compensate for all the heat input brought by the tank filling operations. This can cause an increase in storage pressure and loss of hydrogen.
    These solutions therefore generate product losses (rejection to air) or require the sizing of the liquefier and the gas recovery unit in order to be able to absorb the vaporization gases produced during truck filling.
    An object of the present invention is to overcome all or part of the drawbacks of the prior art noted above.
    To this end, the installation according to the invention, moreover in accordance with the generic definition given in the preamble above, is essentially characterized in that it comprises two storage of liquid hydrogen at respective storage pressures. determined, the liquefier comprising an inlet connected to the source and an outlet connected in parallel, via a valve assembly, to a respective inlet of each storage, the outlet of the liquefier also being connected to a connection end intended to be connected so removable from a tank to be filled, each storage unit comprising a respective liquid withdrawal line comprising one end connected to the storage unit and at least one other end intended to be connected to one at least one tank to be filled, each storage unit further comprising a supply line respective gas withdrawal comprising one end connected to the storage and another end connected to an inlet of the liquefac via a set of valves configured to allow gas to be recycled to the liquefier for liquefaction.
    According to possible features:
    - the two liquid hydrogen storages are maintained at respective determined storage pressures,
    - the installation comprises a second liquefier comprising an inlet connected to the source and an outlet connected in parallel, via a valve assembly to a respective inlet of each storage.
    The invention also relates to a method for filling a tank of liquid hydrogen, in particular a mobile tank of a semi-trailer, by means of an installation in accordance with any one of the characteristics above or below and comprising a preliminary step of depressurizing the reservoir to be filled at a pressure lower than the pressure of the storage having the highest pressure among the two storage.
    The invention makes it possible to differentiate the pressure of the two storages. This allows the use of the pressure difference from one storage to another as the driving force of the hydrogen in order to transfer fluid into the liquefier and bring enough cold for these tank loading operations while losing less hydrogen.
    Furthermore, embodiments of the invention may include one or more of the following characteristics:
    - the preliminary depressurization step includes a transfer of a first quantity of liquid hydrogen into the tank directly from the liquefier,
    the preliminary depressurization step comprises a transfer of pressurized gas from the reservoir to an inlet of the liquefier and / or to an inlet of at least one of the storage facilities,
    the method comprises, simultaneously with the preliminary depressurization step, a step of transferring liquid hydrogen into at least one of the storage facilities from the liquefier,
    the method comprises a first filling step comprising a transfer of liquid hydrogen into the tank by pressure differential from the storage having the highest pressure among the two storage,
    the process comprises, simultaneously with the first filling step, a step of transferring gaseous hydrogen from the reservoir to an inlet of the liquefier and its liquefaction,
    the process comprises, simultaneously with the first filling step, a step of transferring liquid hydrogen from the liquefier into the storage having the lowest pressure among the two storage,
    - The method comprises, after the first filling step, a step of depressurizing the tank at the storage pressure having the lowest pressure among the two storages, the step of depressurizing comprising pressure balancing between the tank and said storage having the lowest pressure among the two storages,
    the method comprises, simultaneously with the step of depressurizing the reservoir at the pressure of the storage having the lowest pressure among the two storage, a step of transferring liquid hydrogen from the liquefier to said storage having the lowest pressure among the two storages,
    the method comprises, after the step of depressurizing the tank at the pressure of the storage having the lowest pressure among the two storage facilities, a step of depressurizing the tank at a pressure lower than the pressure said lower among the two storage facilities the additional depressurization step comprising a transfer of gas from the reservoir to an inlet of the liquefier and / or an evacuation to the atmosphere and / or a gas collection member,
    - the process uses two separate liquefiers,
    a first storage of liquid hydrogen is maintained at a first pressure of between and 1.5 and 11 bar absolute and in particular between 2 and 3 bar absolute, preferably 2.5 bar absolute,
    a second storage of liquid hydrogen is maintained at a second pressure of between 0.8 and 2.3 bar absolute and in particular between 1 and 2 bar absolute, preferably 1.5 bar absolute,
    - before the step of transferring a first quantity of liquid hydrogen into the tank, said tank is at a pressure greater than or equal to the pressure of the storage having the highest pressure among the two storage, in particular the tank is at a pressure of 3 to 11 bar, in particular 8 bar, and, at the end of the step of transferring a first quantity of liquid hydrogen into the tank, the pressure in the tank is lowered at a pressure lower than the pressure storage having the highest pressure among the two storage, in particular a few millibars lower than this pressure,
    Other particularities and advantages will appear on reading the description below, made with reference to the figures in which:
    - Figure 1 shows a schematic and partial view illustrating the structure and operation of an installation according to a possible embodiment of the invention,
    - Figures 2 to 7 show schematic and partial views illustrating different possible operating steps of the installation of Figure 1 when filling a tank,
    - Figure 8 shows a schematic and partial view illustrating the structure and operation of an installation according to another possible embodiment of the invention.
    The storage and distribution installation for liquefied hydrogen shown in FIG. 1 comprises a source 2 of gaseous hydrogen, a liquefier 3 and two storages 4, 5 of liquid hydrogen.
    The liquefier 3 comprises an input connected to the source 2 (for example via at least one valve 22).
    Source 2 can be a hydrogen network and / or a hydrogen production unit (for example steam reforming and / or electrolysis or any other suitable source). The hydrogen gas supplied by the source can have a pressure for example between 10 and 80 bar.
    The liquefier 3 comprises an outlet connected in parallel, via a valve assembly 7, 6, 16, to respective inlets of the two storages 5, 4 and also connected at a third end 15 of removable connection to a reservoir 10 to be filled (for a direct transfer from the liquefier 3 to the tank 10).
    The storages 4, 5 of liquid hydrogen are configured to store the liquid at respective respective pressures.
    These storages 4, 5 are, for example, isolated vacuum storages of large capacity, for example of several thousand liters. These storage units 4 conventionally contain a liquid phase with a vapor phase.
    Conventionally, the storage pressure is preferably regulated there, for example at a fixed value (for example between 1.05 and 11 bar, for example between 1.1 and 1.8 bar, in particular 1.5 bar absolute for one 5 of the storage and for example between 1.9 and 3 bar, in particular 2.5 bar for the other 4 storage.
    By “storage pressure” is meant for example the average pressure in the storage or in the lower part of the storage or in the upper part (in the gaseous sky). Indeed, due to the low density of hydrogen, the pressure in the lower part of the repository is substantially equal to the pressure in the upper part.
    The hydrogen supplied by the source 2 and liquefied by the liquefier 3 can be transferred to the storage facilities 4, 5 intermittently and / or continuously and / or in the event of a drop in the level of liquid in the tanks 4, 5 below. of a determined threshold. Preferably, the level of liquid in the storage facilities 4, 5 is automatically controlled via the supply from the liquefier 3 (flow rate of the liquefier 3 and / or valve for regulating the flow rate of liquid supplied to the storage facilities 4,
    5).
    Each storage 5, 4 comprises a respective liquid withdrawal line 9, 8 comprising one end connected to the storage 4, 5 (generally at the bottom) and at least one other end intended to be connected to at least one reservoir 10 to be filled .
    Each storage 4, 5 further comprising a respective gas withdrawal line 12, 11 comprising one end connected to the storage 4, 5 (generally in the upper part) and another end connected to an inlet of the liquefier 3 via a set of valves 14 , 13 configured to allow the recycling of vaporized gas in the storage (s) 4, 5 to the liquefier 3 for liquefaction.
    As described in more detail in the examples below, the storage 4 having the highest pressure among the storage 4, 5 can be used to transfer the liquid hydrogen to the tank 10 to be filled while the storage 5 having the pressure the lowest among the storages 4, 5 can be used to recover the gaseous hydrogen coming from the tank 10 which has been cooled and liquefied (in the liquefier 3).
    In a first configuration (cf. FIG. 1), the gaseous hydrogen supplied by the source 2 and liquefied by the liquefier 3 can be distributed in storage 4 and / or storage 5 for example via a pipe 17 comprising two connected downstream ends in parallel respectively to the two storages 4, 5 (corresponding open valves 7, 6 shown in white).
    The pressure of a first storage 4 is greater than the pressure in the second storage 5.
    The outlet valves 13, 14 allowing the evacuation of gas through the gas withdrawal lines 12, 11 are closed (closed valves shown in black).
    Likewise, the outlet valves 20, 24 allowing the evacuation of liquid via the lines 8, 9 for withdrawing liquid are closed (closed valves shown in black).
    The hydrogen leaving the liquefier 3 is sub-cooled in order to maintain the pressure of the storage facilities and to combat their thermal inputs. That is to say that the liquefier 3 can be configured to produce a sub-cooled liquid, that is to say at a temperature below the bubble temperature of hydrogen at the pressure of the storage concerned.
    Alternatively or in combination, an ejector 25 could be provided in or at the outlet of the liquefier 3, the pressurized gas taken from the second storage 5 would be used in the ejector 25 and mixed with the liquid transferred to the first storage 4 (cf. representation schematic with dotted lines in figure 1). This makes it possible to maintain the pressure of the second storage 5 and to reduce the level of subcooling for the first storage 4.
    When a truck arrives at installation 1 to fill its liquid tank 10, the latter is generally partially empty and at a relatively high temperature and pressure (for example pressure from 2 to 10 bar and temperature from 100 to 25K for example) .
    After connection of the reservoir 10 to the installation 1 (to the liquid supply lines 8, 15 and to a gas return line 18 of the installation), the pressure in the reservoir 10 must be reduced below the pressure of the pressure of the first storage 4 to allow filling of the reservoir 10 by pressure balancing from this first storage 4.
    The hydrogen present in the tank 10 to be filled is generally predominantly gaseous (from 1 to 10% of liquid phase for example) and at a temperature between 100K and 25K.
    This pressure drop can be achieved by transferring liquid hydrogen under cooled into the tank 10 directly from the liquefier 3 via the end 15 of the transfer line, the valve 16 of which is then open.
    This arrival of liquid hydrogen (preferably sub-cooled) in the tank 10 will reduce the pressure there by cooling and condensation of the hydrogen present, this even if the evacuation of gas from the tank closed (valve 19 closed on the gas return line 18 18 see Figure 1).
    It is possible to transfer "push" liquid hydrogen into the tank 10 because the supply pressure of the source 2 is preferably higher than the pressure prevailing in the tank 10 to be filled.
    This depressurization of the reservoir 10 will be all the more rapid as the hydrogen leaving the liquefier 3 will be sub-cooled (for example at a temperature of 21K to 15K). The flow of liquefaction which is not transferred into the tank 10 (that is to say the portion of the liquid supplied by the liquefier 3 in surplus) can be used to fill the second storage 5 (cf. corresponding valve 7 open like before).
    Alternatively or cumulatively, the preliminary step of depressurization of the reservoir 10 can comprise a transfer of pressurized gas from the reservoir 10 to an inlet of the liquefier 3 (cf. FIG. 3 via the opening of the valve 19 on the gas return line 18 18). Simultaneously, the liquefier 3 can supply liquid to the first storage 4 and / or the second storage 5 (cf. FIG. 3, valves 6, 7 open).
    Alternatively or cumulatively, the preliminary step of depressurization of the reservoir 10 comprises a transfer of pressurized gas from the reservoir 10 to an inlet of the first storage 4 (cf. FIG. 4, via the opening of the valve 20 on the pipe 8 of liquid feed). Simultaneously, the valve 6 located between the outlet of the liquefier 3 and the inlet of the first storage 4 is closed while the valve 14 located between a gas outlet of the first storage 4 and an inlet of the liquefier 3 is open. In addition, the liquid supplied by the liquefier 3 can be used to fill the second storage 5 (cf. corresponding valve 7 opened as above).
    When the tank 10 has reached a pressure lower than the pressure of the first storage 4, the liquid level in the tank 10 is generally between 10% and 50% of its maximum capacity (variable according to the initial conditions of the tank 10).
    In a possible sequence, there may firstly be filling (sub-cooled) of the reservoir 10 from the liquefier 3 (to begin to drop the pressure and cool the vapors in the reservoir 10) then depressurization of the reservoir 10 to a inlet of the liquefier 3 with return of liquid from the liquefier 3 to the storage 4 and / or the storage 5 until a first pressure P1 greater than the pressure in the storage 4 having the highest pressure is reached in the tank 10.
    Depressurization of the tank 10 can then be carried out towards the liquefier 3 with return of the liquid from the liquefier 3 to the storage 5 at the lowest pressure until reaching in the tank 10 a pressure P2 comprised between the pressures of the two storages 4 and 5.
    At the end of this depressurization the level of liquid in the reservoir 10 is also between 10 and 50% of its maximum capacity.
    The main phase of filling the reservoir 10 can then take place.
    As illustrated in FIG. 5, liquid hydrogen can then be transferred from the first storage 4 to the reservoir 10 by the line 8 for drawing off the liquid connecting them (corresponding valve 20 open) by means of the pressure differential (the other valves 14 6 for access to the first storage 4 are closed).
    Any vapors leaving the tank 10 (for example at a temperature between 100K and 23K) can possibly be recovered by the gas return line 18 (valve 19 open in particular) connecting the tank 10 to the inlet of the liquefier 3.
    This hot gas is thus liquefied and the liquid obtained can be transferred to the second storage 5 via the pipe and the corresponding valve 7 open.
    It is also possible to continue liquefying hydrogen supplied by the source 2. In this case, the liquid will preferably be produced / expanded in the liquefier 3 at a pressure intermediate between the pressure of the reservoir 10 and the pressure of the second storage 4, to allow its transfer to the second storage 5 by the pressure differential (via the transfer line 17 and the opening of the corresponding valve 7.
    As before (cf. FIG. 1), it is alternatively possible to provide an ejector at the outlet of the liquefier 3 which is this time supplied by the pressurized gas coming from the reservoir 10 in order to reduce the pressure of the reservoir 10 more quickly and to accelerate its filling with liquid.
    When the desired quantity of liquid has been transferred to the tank (tank 10 having reached its determined filling threshold), the tank 10 can then be depressurized at the pressure of the second storage 5 (or below).
    After the above filling, the pressure in the tank 10 is generally close to the pressure in the first storage 4. The filling level of the tank 10 is for example between 50% and 95%. However, its pressure must be reduced in order to be able to hit the road and not lose hydrogen during the journey.
    This road pressure is variable according to local regulations.
    The connection of the reservoir 10 (its vapor outlet) to the second storage 5 via the gas return lines 18 and the gas withdrawal line 11 (valves 19 and 13 corresponding open) allows steam to be discharged from the tank 10 to the second storage 5. This makes it possible to balance the pressures of the reservoir 10 and of the second storage 5 at a pressure close to the pressure of the second storage 5 (at a pressure that is close and not equal because sub-cooled liquid arrives in the second storage 5 of the liquefier 3 and due to the difference in size between the tank 10 and the storage 5).
    As a variant or in combination, it is also possible to return the vapors from the tank 10 trucks to the liquefier 3 via an ejector at the source 2 and sucking the gas during the expansion of the gas in the liquefier 3.
    After this depressurization, the reservoir 10 has a pressure close to the pressure in the second storage 5.
    If this pressure is compatible with the required road pressure, the truck can disconnect from installation 1 and set off again to transport the liquid hydrogen to its destination. The system returns to the first initial configuration.
    If, on the other hand, the pressure in the tank 10 is still too high to take the road (compared to regulatory requirements), additional depressurization is possible, for example towards a vent (cf. reference 21 figure 7) and / or towards a system hydrogen recovery.
    Otherwise, the end of the filling can also be carried out via the second storage 5 by means of the corresponding pipe 9. The pressure in the tank 10 is then reduced via the recovery of the vapors to the liquefier (via the gas return line 18 and its valve 19 open (and / or via an ejector taking the vapors from the storage to the source 2).
    In the case where the source 2 is not available (for example a valve 22 located between the source 2 and the liquefier 3 is closed).
    In this case, when there is no reservoir 10 to be filled (according to the configuration in FIG. 1) but the pressures of the two storage units 4, 5 must be maintained in the event of the arrival of a reservoir 10 to be filled .
    In this case, the liquefier 3 can use its refrigerating liquefaction capacity to condense and / or sub-cool vapors from the storage facilities 4, 5.
    Thus, for example, when the pressure rises in the first storage 4 (because of the thermal inlets which evaporate the liquid), the gas produced can be transferred into the liquefier 3 via the line 12 for withdrawing gas (valve (s) 14 correspondents open). The liquefied and sub-cooled gas can then be transferred to the second storage 5 at a lower pressure (via line 17 and the corresponding valve 7).
    The sub-cooling of the hydrogen (for example up to 15K) makes it possible to avoid a rise in pressure in this second storage 5 despite the thermal inputs.
    When the source 2 is not available (valve 22) closed for example and a tank 10 is connected to the installation and must be depressurized, the pressure in the tank 10 can be reduced below the pressure in the first storage 4 to allow filling from this storage 4.
    The hydrogen present in the tank 10 to be filled is mainly gaseous (from 1 to 10% of liquid phase for example) and at a temperature for example between 100K and 25K. By connecting the gas outlet of the tank 10 to the liquefier 3 (gas return line 18 via the open valve 19), this makes it possible to liquefy the gaseous hydrogen coming from the tank 10. This liquefied hydrogen can be transferred to the first storage 4 and / or at the second storage 5 as a function of the pressure in the tank 10. At the end of this step, the tank 10 is at a pressure lower than the pressure of the first storage 4 allowing it to be filled by this storage 4 as previously described).
    In a possible alternative embodiment, the installation comprises more than two storage units which may have respective determined storage pressures.
    In an alternative embodiment represented in FIG. 8, the installation 1 can comprise two liquefiers 3, 26. FIG. 8 has been simplified compared to the preceding figures (same architecture but all the preceding valves are not represented in FIG. 8) .
    This variant is advantageous in particular during large variations in the demand for hydrogen when the flexibility of a single liquefier can become penalizing.
    In particular, the second liquefier 26 (or additional liquefier compared to the above solution) is also supplied by the source 2. In addition, this additional liquefier 26 may also have a liquid outlet connected to each of the two storages 4, 5 (for example via a pipe comprising two downstream ends connected in parallel respectively to two inputs to the storage facilities 4, 5).
    Preferably the two liquefiers 3, 26 are of different sizes. In addition, as illustrated in FIG. 8, preferably only one (the first) liquefier 3 is configured to recover the vapors from the installation. The other additional liquefier produces liquid only from the gas supplied by source 2.
    This additional liquefier 26 will make it possible to resume management of the vapors of the storages 4, 5 and of the reservoir 10. The cooling / filling stages can be similar to those described above with the difference that the additional liquefier 26 can supply hydrogen. liquid also in the storage (s) 4, 5 if necessary.
    Optionally, low pressure hydrogen from the first liquefier 3 could be returned to the second liquefier 26 in order to recover the frigories available to liquefy the gas supplied by the source (or higher pressure vapors). Similarly, it may be possible to envisage the possibility that the second liquefier 26 may recover heated vapors with a view to liquefying them.
    Thus all or part of the above processes carried out by a single liquefier 3 can be carried out by one of the two or both liquefiers 3, 26.
    In addition, the system can be configured to fill several tanks 10.
    In this case, as many ends and valves 20, 24, 16, 19 can be provided as there are tanks to be filled (in particular simultaneously).
    权利要求:
    Claims (14)
    [1" id="c-fr-0001]
    1. Installation and storage of liquefied hydrogen comprising a source (2) of gaseous hydrogen, a liquefier (3), two storage (4, 5) of liquid hydrogen at determined respective storage pressures, the liquefier (3) comprising an inlet connected to the source (2) and an outlet connected in parallel, via a valve assembly (7, 6, 16), to a respective inlet of each storage (5, 4), the outlet of the liquefier (3) also being connected to a connection end (15) intended to be removably connected to a tank (10) to be filled, each storage (5, 4) comprising a respective liquid withdrawal line (9, 8) comprising one end connected to the storage (4, 5) and at least one other end intended to be connected to one at least one tank (10) to be filled, each storage (4, 5) further comprising a pipe (12, 11) respective gas withdrawal system comprising one end connected to the storage (4, 5) and another end connected to an inlet of the liquefier (3) via a set of valves (14, 13) configured to allow the recycling of gas to the liquefier (3) for liquefaction.
    [2" id="c-fr-0002]
    2. Installation according to claim 1, characterized in that the two storage (4, 5) of liquid hydrogen are maintained at respective determined respective storage pressures.
    [3" id="c-fr-0003]
    3. Installation according to claim 1 or 2, characterized in that it comprises a second liquefier (26) comprising an inlet connected to the source (2) and an outlet connected in parallel, via a valve assembly (27) to a respective entry of each storage (5, 6).
    [4" id="c-fr-0004]
    4. Method for filling a tank (10) of liquid hydrogen, in particular a mobile tank of a semi-trailer, by means of an installation (1) according to any one of claims 1 to 3, characterized in what it comprises a preliminary stage of depressurization of the reservoir (10) to be filled at a pressure lower than the pressure of the storage (4) having the highest pressure among the two storage (4, 5).
    [5" id="c-fr-0005]
    5. Method according to claim 4, characterized in that the preliminary depressurization step comprises a transfer of a first quantity of liquid hydrogen in the tank (10) directly from the liquefier (3).
    [6" id="c-fr-0006]
    6. Method according to any one of claims 4 or 5, characterized in that the preliminary step of depressurization comprises a transfer of gas under pressure from the reservoir (10) to an inlet of the liquefier (3) and / or to an inlet from at least one of the storages (4, 5).
    [7" id="c-fr-0007]
    7. Method according to any one of claims 4 to 6, characterized in that it comprises, simultaneously with the preliminary step of depressurization, a step of transfer of liquid hydrogen in at least one of the storage (4, 5) from the liquefier (3).
    [8" id="c-fr-0008]
    8. Method according to any one of claims 4 to 7, characterized in that it comprises a first filling step comprising a transfer of liquid hydrogen into the tank (10) by pressure differential from the storage (4) having the highest pressure among the two storages (4, 5).
    [9" id="c-fr-0009]
    9. Method according to claim 8, characterized in that it comprises, simultaneously with the first filling step, a step of transfer of gaseous hydrogen from the reservoir (10) to an inlet of the liquefier (3) and its liquefaction.
    [10" id="c-fr-0010]
    10. Method according to claim 8 or 9, characterized in that it comprises, simultaneously with the first filling step, a step of transferring liquid hydrogen from the liquefier (3) in the storage (5) having the pressure the lower of the two storages (4, 5).
    [11" id="c-fr-0011]
    11. Method according to claim 8 to 10, characterized in that it comprises, after the first filling step, a step of depressurizing the reservoir (10) at the storage pressure (5) having the lowest pressure among the two storages (4, 5), the depressurization step comprising a pressure balancing between the reservoir (10) and said storage (5) having the lowest pressure among the two storages (4, 5).
    [12" id="c-fr-0012]
    12. Method according to claim 11, characterized in that it comprises, simultaneously with the depressurization step of the reservoir (10) at the storage pressure (5) having the lowest pressure among the two storage (4,
    5), a step of transferring liquid hydrogen from the liquefier (3) to said storage (5) having the lowest pressure among the two storage (4, 5).
    [13" id="c-fr-0013]
    13. Method according to claim 12, characterized in that it comprises,
    5 after the depressurization step of the reservoir (10) at the storage pressure (5) having the lowest pressure among the two storages (4, 5), an additional depressurization step of the reservoir (10) at a lower pressure at said lower pressure among the two storage (4, 5), the additional depressurization step comprising a transfer of gas from the reservoir (10) to an inlet of the liquefier (3) and / or an evacuation to the atmosphere and / or a gas collection device.
    [14" id="c-fr-0014]
    14. Method according to any one of claims 4 to 13, characterized in that it uses two separate liquefiers (3, 26).
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    WO2021233666A1|2021-11-25|Liquefied gas storage tank
    WO2020109607A1|2020-06-04|Device for generating gas in gaseous form from liquefied gas
    EP3488139A1|2019-05-29|Module and system for depressurising a cryogenic tank
    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
    EP3650741A1|2020-05-13|
    FR3088415B1|2020-10-23|
    AU2019261745A1|2020-05-28|
    KR20200054884A|2020-05-20|
    US20200149684A1|2020-05-14|
    CN111174086A|2020-05-19|
    CA3058444A1|2020-05-12|
    US11073245B2|2021-07-27|
    EP3650741B1|2021-04-14|
    JP2020079641A|2020-05-28|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US20080178612A1|2005-03-28|2008-07-31|Osamu Utata|Method for Supplying Hydrogen Gas and Liquefied Hydrogen Delivery Vehicle|
    DE102010047300A1|2010-10-01|2012-04-05|Linde Aktiengesellschaft|Method for filling portable storage tank with cryogenic medium, particularly with hydrogen or helium, involves recondensing gaseous medium contained in portable storage container to start refueling procedure|
    FR3061533A1|2017-01-02|2018-07-06|L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude|STATION AND METHOD FOR SUPPLYING GAS UNDER PRESSURE|
    US20030021743A1|2001-06-15|2003-01-30|Wikstrom Jon P.|Fuel cell refueling station and system|
    CA2401926C|2002-09-06|2004-11-23|Westport Research Inc.|Combined liquefied gas and compressed gas re-fueling station and method of operating a combined liquefied gas and compressed gas re-fueling station|
    GB0406615D0|2004-03-24|2004-04-28|Air Prod & Chem|Process and apparatus for liquefying hydrogen|
    DE102005039202A1|2005-08-18|2007-02-22|Linde Ag|Mobile, self-sufficient and immission-free hydrogen filling station|
    FR2908859B1|2006-11-22|2009-02-20|Air Liquide|METHOD AND STATION FOR REFUELING IN HYDROGEN|
    US9291309B2|2009-07-22|2016-03-22|Shell Oil Company|Hydrogen dispensing system and method thereof|
    JP6021430B2|2012-05-22|2016-11-09|川崎重工業株式会社|Reliquefaction method of boil-off gas generated from liquid hydrogen storage tank|FR3112198A1|2020-07-03|2022-01-07|L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude|Hydrogen refrigeration installation and process|
    EP3951240A1|2020-08-07|2022-02-09|Linde Kryotechnik AG|Method and device for providing a cryogenic gas|
    CN112032555A|2020-08-28|2020-12-04|夏鹏|Low-temperature ultra-large liquefied natural gas storage tank|
    法律状态:
    2019-11-20| PLFP| Fee payment|Year of fee payment: 2 |
    2020-05-15| PLSC| Publication of the preliminary search report|Effective date: 20200515 |
    2020-11-20| PLFP| Fee payment|Year of fee payment: 3 |
    2021-11-22| PLFP| Fee payment|Year of fee payment: 4 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1860429A|FR3088415B1|2018-11-12|2018-11-12|PROCESS AND INSTALLATION FOR STORAGE AND DISTRIBUTION OF LIQUEFIED HYDROGEN|FR1860429A| FR3088415B1|2018-11-12|2018-11-12|PROCESS AND INSTALLATION FOR STORAGE AND DISTRIBUTION OF LIQUEFIED HYDROGEN|
    EP19202157.4A| EP3650741B1|2018-11-12|2019-10-09|Method and device for storage and supply of liquefied hydrogen|
    CA3058444A| CA3058444A1|2018-11-12|2019-10-09|Method and installation for storing and dispensing liquefied hydrogen|
    KR1020190141803A| KR20200054884A|2018-11-12|2019-11-07|Method and installation for storing and dispensing liquefied hydrogen|
    AU2019261745A| AU2019261745A1|2018-11-12|2019-11-07|Method and installation for storing and dispensing liquefied hydrogen|
    JP2019203761A| JP2020079641A|2018-11-12|2019-11-11|Method and installation for storing and dispensing liquefied hydrogen|
    CN201911094694.9A| CN111174086A|2018-11-12|2019-11-11|Method and apparatus for storing and dispensing liquefied hydrogen|
    US16/681,167| US11073245B2|2018-11-12|2019-11-12|Method and installation for storing and dispensing liquefied hydrogen|
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