Equipment and method for distributing liquefied hydrogen

Abstract

A facility for distributing liquefied hydrogen, comprising a source of gaseous hydrogen (2), a liquefier (3) and at least one means (4) for storing liquid hydrogen, the liquefier (3) comprising an outlet connected to an inlet of the storage means (4) via a liquid circuit (5), the facility (1) comprising a liquid filling circuit (12) provided with a first end connected to the storage means (4) and a second end intended to be removably connected to a first end of a mobile liquid tank (6) to be filled, the facility (1) comprising a gaseous hydrogen supply circuit (12) provided with a first end intended to be removably connected to the second end of the tank (6) and a second end connected to a receiving member of the facility (1). The installation (1) further comprises a gas recovery circuit (7) including a pressure and / or flow regulating member (8) (e.g. a valve) for reducing the pressure in the transfer liquid tank (6) to a predetermined filling pressure (Pr), the installation (1) includes an electronic control unit (10) including a microprocessor configured to receive at least one filling request signal (13) from the transfer liquid tank (6), the pressure and / or flow regulating member (8) being adjustable, and the electronic control unit (10) is configured to operate the pressure and / or flow regulating member (8) to regulate the pressure level in the transfer liquid tank (6) to the predetermined filling pressure (Pr) based on the received filling request signal (13).

Description

[Technical field]

[0001] The present invention relates to an installation and method for dispensing liquefied hydrogen.

[0002] The invention more particularly relates to an installation for dispensing liquefied hydrogen, comprising a source of gaseous hydrogen, a liquefier and at least one liquid hydrogen storage vessel, the liquefier having an inlet connected to the source and an outlet connected via a liquid circuit to the inlet of the storage vessel in order to store the liquefied hydrogen produced by the liquefier in the storage vessel, the installation comprising a liquid filling circuit provided with a first end connected to the storage vessel and a second end intended to be removably connected to a first end of a mobile liquid tank (e.g. a semi-trailer) to be filled, the installation further comprising a gas recovery circuit provided with a first end intended to be removably connected to the second end of said tank and a second end connected to a receiving member of the installation (in particular the inlet of the liquefier), the gas recovery circuit comprising pressure and / or flow regulating members (e.g. valves) capable of reducing the pressure in the mobile liquid tank to a predetermined filling pressure, the installation comprising an electronic control unit comprising a microprocessor configured to control all or part of the installation, the electronic control unit being configured to receive at least one signal requesting the filling of the mobile liquid tank. [Background technology]

[0003] Hydrogen liquefiers are typically configured to operate at rated load and produce liquid hydrogen at a given temperature, which is stored in one or more storage vessels that fill mobile tanks (semi-trailers).

[0004] Furthermore, the liquefier storage vessel and the associated loading procedures for filling the trailer from the storage vessel are designed to operate under fixed operating conditions. Indeed, all these parameters are typically optimized during the design phase. Then, during the operational phase, these parameters remain the same regardless of the trailer to be filled and the customer acceptance dispatch.

[0005] However, typically several customers (reception points) will be accepting liquid hydrogen deliveries from this facility with different logistics and different expectations (various degrees of dense or cold hydrogen).

[0006] For this purpose, the nominal liquefied hydrogen production point is set to the level required to satisfy the most demanding customers, so that the facility wastes part of its energy producing "excessively high quality" hydrogen for certain users. Summary of the Invention [Problem to be solved by the invention]

[0007] SUMMARY OF THE PRESENT EMBODIMENT An object of the present invention is to overcome all or part of the above-mentioned disadvantages of the prior art. [Means for solving the problem]

[0008] For this purpose, the installation according to the invention, further complying with the general definition given in the preamble above, is essentially characterised in that the pressure and / or flow regulating member is adjustable and that the electronic control unit is configured to control the pressure and / or flow regulating member and to regulate the pressure level in the mobile liquid tank to a predetermined filling pressure in response to a received filling request signal.

[0009] The present invention allows the tank to be filled at an optimum pressure to meet the customer's delivery expectations without producing excessive evaporative gases during filling.

[0010] On the other hand, according to known solutions, too low a pressure is imposed on the mobile tank for a certain delivery. This represents unused and costly energy consumption for the installation. In fact, this generates more flash gas than in the case of a higher pressure. This flash gas, which is generated when filling the tank at a relatively low pressure, is not transported. This gas is released to the liquefier or reliquefied. But if the tank leaves with too low a pressure, additional liquid is evaporated and pressurized at the station (increasing the boil-off gas).

[0011] Furthermore, embodiments of the invention may include one or more of the following features.

[0012] The gas recovery circuit includes a compression member disposed between the pressure and / or flow regulating member and a second end connected to the liquefier, the compression member configured to compress the flow of gas from the first end to a predetermined pressure for the purpose of reinjecting the gas into the liquefier circuit. The predetermined filling pressure is selected between a predetermined minimum pressure and a predetermined maximum pressure. - The predetermined minimum pressure (Pmini) is equal to 1.05 bar. the compression member is configured to operate at a minimum suction pressure at the inlet of the compression member, the predetermined minimum pressure (Pmini) being equal to the minimum suction pressure of the compression member increased by a predetermined value that corresponds at least to the pressure loss in the gas recovery circuit between the first end and the inlet of the compression member. - the predetermined maximum pressure is equal to the value of the pressure in the storage container reduced if necessary by the value of the pressure loss between the storage container and the second end of the liquid filling circuit, and the electronic control unit is configured to receive at least one signal requesting filling of the mobile liquid tank, the signal including at least one of the filling parameters (maximum pressure level permitted in the tank, required fluid pressure level at the receiving point from which the tank needs to deliver liquefied hydrogen after filling, the amount of liquefied hydrogen to be filled into the tank, the distance the tank needs to travel after filling and then deliver liquefied hydrogen to the receiving point, the number of receiving points from which the tank needs to deliver liquefied hydrogen after filling, the temperature of the storage container, the volume of the tank), and the electronic control unit is configured to calculate the predetermined filling pressure level depending on these parameters. the liquefier is of a type having a controlled variable cooling power, i.e. a type capable of varying the temperature of the produced liquid hydrogen, in particular of producing liquid hydrogen that is subcooled relative to a saturated state, and the electronic control unit is configured to control the temperature level of the liquid hydrogen produced in the storage vessel in response to the received demand signal. The liquid charge circuit includes two withdrawal pipes connected to two different heights of the storage vessel to draw hydrogen out of the storage vessel under different thermodynamic conditions. The installation comprises two separate storage vessels which are filled with different liquid hydrogen temperatures, a first end of a liquid filling circuit is connected to the storage vessels, the liquid filling circuit comprises a set of valves configured to fill the tank with a mixture of liquids coming from the storage vessels and to obtain a predetermined liquid temperature.

[0013] Furthermore, the present invention relates to a method for dispensing liquefied hydrogen using an installation according to any of the above or below characteristics, comprising the steps of generating a signal requesting filling of a mobile liquid tank, calculating a predetermined filling pressure level in response to this signal, and filling the tank with liquid hydrogen at the predetermined filling pressure level.

[0014] According to other possible features, the invention is as follows. - The predetermined filling pressure level is adjusted during the filling step by controlling the opening of the pressure and / or flow regulating members. - carrying out control of the opening of the pressure and / or flow regulating members during and / or before and / or after the transfer of liquid hydrogen to the tank, during the degassing operation of the tank; - The step of generating a fill request signal is performed manually and / or remotely and transmitting this signal to the equipment. The method includes the steps of calculating a predetermined temperature value of the liquefied hydrogen produced in the storage vessel in response to the signal, before transferring the liquid hydrogen from the storage vessel to the tank, and filling the storage vessel with the liquefied hydrogen at the predetermined temperature. The method includes the steps of filling two separate storage containers with liquefied hydrogen at different temperatures before transferring the liquid hydrogen from the storage containers to the tank, calculating a predetermined liquefied hydrogen temperature value in response to this signal, and filling the tank at this predetermined temperature via a mixture of liquefied hydrogen coming from these storage containers.

[0015] Furthermore, the invention may relate to any alternative device or method including any combination of the above or below features within the scope of the claims.

[0016] Other particular features and advantages will become apparent from the following description, given with reference to the drawings. [Brief description of the drawings]

[0017] [Figure 1] FIG. 1 is a schematic partial diagram illustrating an example of the structure and operation of an embodiment of a liquefied hydrogen distribution facility according to the present invention. [Diagram 2] FIG. 2 shows a detailed diagram of such an installation in a first alternative embodiment with control of the temperature of the produced and stored liquid hydrogen. [Diagram 3] FIG. 3 shows a detailed view of such an installation in a second alternative embodiment with withdrawal of liquid at different levels of the storage vessel. [Figure 4] FIG. 4 shows a detailed view of such an installation in a third alternative embodiment using several storage vessels. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0018] The liquefied hydrogen distribution facility 1 shown in FIG. 1 includes a source of gaseous hydrogen 2 , a liquefier 3 , and at least one liquid hydrogen storage vessel 4 .

[0019] Source 2 may include a hydrogen supply network and / or hydrogen production equipment (eg, an electrolyser).

[0020] The liquefier 3 is, for example, a liquefier with a cycle gas (e.g. containing hydrogen and / or helium) undergoing a thermodynamic cycle occurring at one end of the cycle cold gas placed in heat exchange with a hydrogen stream to be cooled for the purpose of liquefying the hydrogen.

[0021] The liquefier 3 thus includes an inlet connected to the source 2 and an outlet connected to the inlet of the storage vessel 4 via a liquid circuit 5 for storing the liquefied hydrogen produced by the liquefier 3 in the storage vessel 4.

[0022] Furthermore, the installation 1 includes a liquid filling circuit 12 provided with a first end connected to the bottom of the storage vessel 4 and a second end intended to be detachably connected to a first end of a mobile liquid tank 6 (e.g. a semi-trailer) to be filled in order to transfer the liquid hydrogen to the mobile liquid tank 6.

[0023] Furthermore, the equipment 1 includes a gas recovery circuit 7 (for recovering the evaporated gas contained in the tank 6 to be filled) having a first end intended to be detachably connected to a second end (typically the upper end) of this storage container 4, and a second end connected to a receiving member of the equipment 1.

[0024] The gas recovery circuit 7 comprises a pressure and / or flow regulating member 8 (e.g. a valve) capable of reducing the pressure in the transfer liquid tank 6 to a predefined filling pressure Pr. This pressure and / or flow regulating member 8 is adjustable, i.e. a residual pressure level in the tank 6 (controlled degassing) can be set.

[0025] For example, the second end is connected to the inlet of a liquefier 3 in order to recover gaseous hydrogen in the liquefier circuit to be liquefied.

[0026] For this purpose, the gas recovery circuit 7 preferably comprises a compression member 11 (e.g. a compressor) (or compression unit) arranged between the pressure and / or flow regulating members 8. The compressor 11 may thus be configured to compress the gas flow coming from the first end to a predetermined pressure, for example with a view to reinjecting the gas into the circuit of the hydrogen to be liquefied of the liquefier 3.

[0027] As shown, downstream of the compressor 11, the recovered evaporative gas stream may circulate in the passage of a set of exchangers cooling a liquefier 3 away from the main circuit 5 for liquefying hydrogen provided by a source. In other words, the evaporative gas stream may be liquefied separately from the main hydrogen stream. This recovered and cooled evaporative gas may be transported as it leaves the liquefier 3 in a pipe 17 (possibly provided with a valve 27) connectable to the liquid circuit 5 (e.g. after leaving the liquefier 3 at or just before the inlet to the storage vessel 4). As shown, this cooled (if necessary at least partially liquefied) gas may be mixed with the liquid hydrogen of the liquid circuit 5, e.g. downstream of the final expansion element 15 (e.g. turbine and / or valve) of the liquid circuit 5.

[0028] As further shown, the upper end of the storage vessel 4 may be connected to the inlet of a compressor 11 via a pipe 14, preferably provided with a valve 24, so that the compressor can further recover evaporated gases from the storage vessel 4 for reuse and liquefaction, if desired.

[0029] The installation 1 may include a set of valves and appropriate components which are not shown for the sake of simplicity.

[0030] The equipment 1 includes an electronic control unit 10 including a microprocessor (e.g. a computer or programmable electronic calculator) configured to control all or part of the equipment 1. This control unit 10 may be housed on the equipment 1 and / or remotely and may consist of one or several electronic units.

[0031] The electronic control unit 10 is arranged to receive at least one signal 13 requesting the filling of a transfer liquid tank 6 to be filled.

[0032] The electronic control unit 10 is configured to control the pressure and / or flow regulating member 8 and to regulate the pressure level in the filled transfer liquid tank 6 to a predefined filling pressure Pr in response to the received request signal 13. This allows to regulate the pressure of the tank 6 to be filled at an optimum pressure, in particular with respect to the subsequent delivery, taking into account the requirements and constraints of the transfer tank 6. Thus, the filling pressure Pr may be calculated to correspond to the optimum thermodynamic conditions in order not to exceed the limits specified by the customer whose liquefied gas is to be delivered by the tank 6.

[0033] The predetermined filling pressure Pr is selected between a predetermined minimum pressure Pmini and a predetermined maximum pressure Pmax.

[0034] This predetermined minimum pressure Pmini is, for example, equal to a predetermined fixed value (for example 1.05 bar), in particular when part of the boil off gas (BOG) is discharged from the tank 6 (additional pressure reduction before leaving the filling tank 6).

[0035] If there is complete recovery of this evaporated gas from the tank 6 in the installation 1, this minimum pressure Pmini may be equal to the minimum suction pressure of the compression unit 11 plus the pressure loss that has to be overcome by the return of this evaporated gas between the tank 6 and the inlet of the compression unit 11.

[0036] The predetermined maximum pressure Pmax is equal to the value of the pressure in the storage vessel 4, optionally reduced by the value of the pressure loss between the storage vessel 4 and the second end of the liquid filling circuit 12. In other words, if no transfer pump is available to transfer the liquid to the liquid filling circuit, this predetermined maximum pressure Pmax may be specified by the pressure in the storage vessel 4 of the installation 1 minus the pressure loss between the storage vessel 4 and the tank 6 (trailer).

[0037] Conversely, if a transfer pump is available in the liquid filling circuit, this predetermined maximum pressure Pmax may be dictated by the pressure in the storage vessel 4 of the installation.

[0038] Thus, the electronic control unit 10 is arranged to receive at least one signal 13 requesting filling of the transfer liquid tank 6 specifying at least one filling parameter.

[0039] This signal 13 may, for example, include at least one of the following filling parameters: the maximum pressure level permitted in the tank 6, the required fluid pressure level at the receiving points from which the tank 6 needs to deliver liquefied hydrogen after filling, the amount of liquefied hydrogen to be filled into the tank 6, the distance the tank 6 needs to travel after filling and then deliver liquefied hydrogen to the receiving points, the number of receiving points from which the tank 6 needs to deliver liquefied hydrogen after filling, the volume of the tank 6).

[0040] The electronic control unit 10 is configured to calculate the optimum predetermined filling pressure level Pr depending on these parameters.

[0041] In other words, the installation 1 optimizes and adapts the filling pressure for the mobile tank 6 depending on the main logistic parameters of the upcoming delivery (eg distance and customer expectations to which the liquid hydrogen should be delivered).

[0042] These optimal thermodynamic packing conditions may be determined automatically by a programming tool.

[0043] For example, a customer (delivery point) may set a fill temperature limit to only purchase cryogenic hydrogen at a particular temperature. For example, the saturation pressure (and therefore temperature) in the mobile tank 6 increases with distance traveled (linearly for a given tank 6 liquid level). A customer may specify a maximum allowable delivery temperature for the receiving station.

[0044] Furthermore, the installation 1 may receive information regarding the number of stations receiving the delivery (the rate of increase of the pressure increases with the number of stations receiving the delivery and with the decrease in the liquid level in the mobile delivery tank 6).

[0045] The electronic control unit 10 is configured to calculate the optimum thermodynamic charge point (pressure between Pmin and Pmax) so as not to exceed limits specified by the customer.

[0046] This information or these parameters may be transmitted manually and / or via a remote transmission system, for example, logistics and tank (trailer) data to an electronic control unit 10 which subsequently calculates the optimum filling pressure Pr.

[0047] Instead, the optimum filling pressure for the tank 6 is transmitted by the tank 6, for example via an operator in charge of filling the tank 6, for example at a loading dock.

[0048] Several types of packings can reach this calculated optimum thermodynamic packing point.

[0049] For example, the electronic control unit 10 may calculate the ideal filling pressure for the tank 6 taking into account the next planned delivery of liquid. Preferably, the optimum pressure value is the maximum value that ensures compliance with customer requirements and road laws. Selecting the highest possible pressure (often 1.15 bara) instead of a lower default value allows to limit the amount of evaporative gases generated due to flash when filling the tank 6. This also promotes the reuse of evaporative gases (less required pressure reduction).

[0050] Thus, the filling pressure for the tank 6 may be adjusted by opening the pressure and / or flow regulating member 8 (the degree to which it is open and / or the length of time it is open) to reduce the pressure within the tank 6 to be filled that is connected to the equipment 1.

[0051] If the installation 1 comprises several filling lines allowing the simultaneous filling of several mobile tanks 6, preferably each element 8 (eg valve) is individually controllable.

[0052] For example, this or these valves 8 may be controlled with a variable set point and / or may be automatic. Thus, the pressure set point of this member 8 may be controlled, for example, via a "PIC" value controller 18 (pressure independent automatic balancing and control valve). Of course, any other type of suitable valve and controller may be contemplated.

[0053] This step of controlled depressurization of the tank 6 is preferably carried out before the step of filling with liquid, and is carried out to the ideal calculated pressure as described above, thereby avoiding discharge to the atmosphere and facilitating the recycling of the evaporated gases within the installation 1. Furthermore, the depressurization step is shorter than in the prior art.

[0054] Depending on the planned frequency of filling of the tanks 6 , the logistics, and the number of loading docks, the installation 1 may include one or more gas recovery circuits 7 (adiabatic return lines) leading to the liquefier 3 .

[0055] For example, for a liquefier 3 of relatively small size or capacity, a single tank 6 may be depressurized / filled at one time and a single return line 7 may be sufficient. On the other hand, if filling operations of several tanks 6 are possible (potentially at different optimal thermodynamic filling points), separate gas return lines 7 may be envisaged.

[0056] Thus, the set point for filling the tank 6 affects the pressure set point of the associated return line 7. Several return lines benefit from the same insulation.

[0057] If the expected delivery conditions are uniform over a relatively long period (for example several days, in particular more than 15 days), the installation 1 may be configured to modify the predetermined pressure in the storage vessel 4 containing the liquid from the liquefier 3, so that the installation 1 can also adapt, if necessary, to the optimum pressure for filling the tank 6.

[0058] If a filling pump is available in the liquid filling circuit 12 , preferably this target pressure for the storage vessel 4 is equal to the filling pressure for the tank 6 .

[0059] If the filling of the tank 6 is carried out without a pump, a sufficient pressure differential is maintained between the storage vessel 4 and the tank 6 to overcome pressure losses in the piping of the filling circuit 12 and maintain the desired liquid filling flow rate. This pressure differential may be between 100 and 500 mbar, more preferably between 200 and 300 mbar (e.g. depending on the length and diameter of the piping of the circuit 12).

[0060] Preferably, the evaporation management system should be flexible to take advantage of higher boiling pressures.

[0061] Thus, although simple and cheap in construction, the invention makes it possible to optimize the entire chain from the liquefier 3 to the receiving station where the mobile tank 6 delivers the liquefied gas. The invention makes it possible to adapt the filling of the tank 6 (trailer) to optimal thermodynamic conditions in order to meet the requirements of the end customer delivering the liquid, while minimizing the costs of the installation 1 (in particular without unnecessary liquefaction and cooling powers).

[0062] The equipment and methods allow for cryogenic liquid delivery tank 6 for optimal logistics chains, particularly minimization of vaporization during filling of tank 6.

[0063] Additionally, as discussed above, the thermodynamic conditions (eg, pressure and / or temperature) in the storage vessel 4 may be adjusted to take into account the subsequent delivery.

[0064] In the case of a liquefier 3 of the type capable of producing flexible liquefied hydrogen in subcooled conditions, as shown diagrammatically in FIG. 2, the installation 1 can be further controlled by modifying the temperature Tl of the liquid produced depending on the above-mentioned parameters.

[0065] For example, if the facility 1 includes a single available storage vessel 4 for a given filling pressure of the tank 6 (e.g. between 1.15 bara and 2 bara, preferably between 1.15 and 1.5 bara), the temperature of the liquefied hydrogen will affect the resulting pressure when the tank 6 is moved.

[0066] Specifically, the tank 6 filled with subcooled liquid hydrogen reaches equilibrium during the movement of the tank 6 and the pressure drops to the saturation pressure. The optimum temperature of the liquid hydrogen entering the tank 6 may be determined by the programmed electronic control unit 10. The temperature of the product liquid hydrogen (subcooled or otherwise) may be adjusted taking into account the parameters of the filling request (next delivery or multiple deliveries) and injected into the bottom of the storage vessel 4. Specifically, the subcooled hydrogen is stored at the bottom of the storage vessel 4 by stratification of the hydrogen within the storage vessel 4.

[0067] Thus, for example, if a customer requires relatively high quality liquid hydrogen, the required amount of subcooled hydrogen must be produced and injected into the bottom, whereas for a less demanding customer, the production of saturated liquid hydrogen may be sufficient to meet the customer's requirements.

[0068] The filling rate of the tank 6 is generally greater than that of the storage vessel 4. It is therefore preferable to predict the filling of the storage vessel 4, especially from a temperature point of view.

[0069] Therefore, preferably, the bottom of the storage vessel 4 is filled with subcooled liquid hydrogen before the tank 6 is filled. At the end of the filling of the storage vessel 4, the amount of produced subcooled hydrogen delivered to the bottom of the storage vessel 4 must at least correspond to the mass filled in the tank 6. This mass can be optimized to further compensate for the heat input from the circuit lines. Based on the production rate of the liquid hydrogen (which may vary in temperature) and the expected mass in the tank 6 to be filled, the installation 1 (e.g. unit 10) may be configured to determine, for example, the start time and duration of the production of optimal subcooled hydrogen.

[0070] As shown diagrammatically in Figure 3, in the case of production of subcooled hydrogen with small fluctuations, the liquid filling circuit 12 may include one or more other outlets of the storage vessel 4 connected to different heights of the storage vessel 4 via separate lines 121, 122. This allows liquid to be drawn off from the storage vessel 4 by exploiting the stratification of hydrogen in the storage vessel 4 (subcooled hydrogen is at the bottom while saturated hydrogen is at the top closer to the liquid / gas interface).

[0071] For example, if the optimum temperature required for filling is the saturation temperature, the intermediate storage vessel outlet 121 may be used to exit the liquid. The outlet may be connected via an independent line (and / or connected to a common pipe).

[0072] As shown diagrammatically in FIG. 4, if two (or more) storage vessels 4 are available at the facility 1, one of the storage vessels 4 may be filled with saturated hydrogen at saturation temperature Tl1, while another storage vessel 4 may be filled with subcooled liquid hydrogen (temperature Tl2).

[0073] The electronic control unit 10 may be configured (programmed) to determine the appropriate mixture of hydrogen from these storage vessels 4 to fill the tanks 6 at an optimal target temperature. Regulation may be achieved by a set of control valves that control the flow rate out of the storage vessels 4.

[0074] A storage vessel 4 containing subcooled liquid may be used to compensate for flash and cooling losses, and can be used to fill tank 6 with very cold hydrogen as needed to achieve the required optimum thermodynamic fill point.

[0075] Thus, in this variant, the installation 1 is able to produce subcooled hydrogen at an optimal temperature and in an optimal amount, which may be stored at the bottom of the storage vessel 4 to be used to fill the tank 6 in order to reach the optimal thermodynamic filling point.

[0076] The tank 6 may be filled by active pumping and / or a simple passive connection using a pressure differential.

[0077] Thus, for the purpose of filling the tank with liquid, the installation 1 can bring the tank to a filling pressure via the controlled opening of the pressure regulating member 8. After filling, this pressure regulating member 8 (which may form part of the transfer tank 6) may be opened to further reduce the pressure of this tank 6 to a second, lower pressure, which is suitable for example for transport or delivery.

Claims

1. A facility for distributing liquefied hydrogen, comprising a source of gaseous hydrogen (2), a liquefier (3) and at least one liquid hydrogen storage vessel (4), the liquefier (3) having an inlet connected to the source (2) and an outlet connected to the inlet of the storage vessel (4) via a liquid circuit (5) for storing the liquefied hydrogen produced by the liquefier (3) in the storage vessel (4), the facility (1) comprising a liquid filling circuit (12) provided with a first end connected to the storage vessel (4) and a second end intended to be removably connected to a first end of a mobile liquid tank (6) (e.g. a semi-trailer) to be filled, the facility (1) being provided with a second end of the tank (6) for storing the liquefied hydrogen produced by the liquefier (3) in the storage vessel (4), the first end of the tank (6) being removably connected to a second end of the tank (6) for storing the liquefied hydrogen produced by the liquefier (3) in the storage vessel (4), the second end of the tank (6) being removably connected to a first ... a gas recovery circuit (7) provided with a first end intended to be detachably connected to an end of the gas recovery circuit (7) and a second end connected to a receiving member of the equipment (1) (e.g. an inlet of the liquefier (3)), the gas recovery circuit (7) comprising a pressure and / or flow regulating member (8) (e.g. a valve) capable of reducing the pressure in the transfer liquid tank (6) to a predetermined filling pressure (Pr); the equipment (1) comprising an electronic control unit (10) including a microprocessor configured to control all or part of the equipment (1), the electronic control unit (10) being configured to receive at least one signal (13) requesting filling of the transfer liquid tank (6), CHARACTERIZED IN THAT said pressure and / or flow regulating member (8) is adjustable and said electronic control unit (10) is configured to control said pressure and / or flow regulating member (8) and to regulate the pressure level in the mobile liquid tank (6) to a predetermined filling pressure (Pr) in response to a received filling request signal (13).

2. 2. The installation according to claim 1, characterized in that the gas recovery circuit (7) comprises a compression member (11) arranged between the pressure and / or flow regulating member (8) and the second end connected to the liquefier, the compression member (11) being configured to compress the flow of gas coming from the first end to a predetermined pressure in order to reinject the gas into the liquefier circuit (3).

3. 3. Installation according to claim 1 or 2, characterized in that the predetermined filling pressure (Pr) is selected between a predetermined minimum pressure (Pmini) and a predetermined maximum pressure (Pmax).

4. 4. Installation according to claim 3, characterized in that said predetermined minimum pressure (Pmini) is equal to 1.05 bar.

5. 3. The installation according to claim 2, characterized in that the compression member (11) is configured to operate at a minimum suction pressure at the inlet of the compression member (11), and the predetermined minimum pressure (Pmini) is equal to the minimum suction pressure of the compression member (11) increased by a predetermined value corresponding at least to a pressure loss in the gas recovery circuit (7) between the first end and the inlet of the compression member (11).

6. 4. Installation according to claim 3, characterized in that the predetermined maximum pressure (Pmax) is equal to the value of the pressure in the storage vessel (4) reduced, if necessary, by the value of the pressure loss between the storage vessel (4) and the second end of the liquid filling circuit (12).

7. 3. The installation according to claim 1 or 2, characterized in that the electronic control unit (10) is configured to receive at least one signal (13) requesting filling of a mobile liquid tank (6) comprising at least one of the following filling parameters: a maximum pressure level permitted in the tank (6), a required fluid pressure level at a receiving point from which the tank (6) needs to deliver liquefied hydrogen after filling, an amount of liquefied hydrogen to be filled into the tank (6), a distance the tank (6) needs to travel after filling and then deliver liquefied hydrogen to the receiving point, a number of receiving points from which the tank (6) needs to deliver liquefied hydrogen after filling, a temperature of the storage vessel (4), a volume of the tank (6), and the electronic control unit (10) is configured to calculate the predetermined filling pressure level (Pr) depending on the parameters.

8. 3. The installation according to claim 1 or 2, characterized in that the liquefier (3) is of a type having a controlled variable cooling power, i.e. a type capable of varying the temperature (Tl) of the produced liquid hydrogen, in particular of producing liquid hydrogen that is subcooled relative to a saturated state, and the electronic control unit (10) is configured to control the temperature level of the liquid hydrogen produced in the storage vessel (4) in response to the received request signal.

9. 9. The installation according to claim 8, characterized in that the liquid charging circuit (12) comprises two withdrawal pipes (121, 122) connected to two different heights of the storage vessel for withdrawing hydrogen from the storage vessel under different thermodynamic conditions.

10. 9. Installation according to claim 8, characterized in that it comprises two separate storage vessels (4) filled with different liquid hydrogen temperatures, the first end of the liquid filling circuit being connected to the storage vessels, the liquid filling circuit comprising a set of valves configured to fill a tank (6) with a mixture of liquids coming from the storage vessels (4) and to obtain a predetermined liquid temperature.

11. 3. A method for dispensing liquefied hydrogen using equipment as claimed in claim 1 or 2, comprising the steps of generating a signal (13) requesting filling of a transfer liquid tank (6), calculating a predetermined filling pressure level (Pr) in response to said signal, and filling said tank (6) with liquid hydrogen at said predetermined filling pressure level (Pr).

12. 12. A method according to claim 11, characterized in that the predetermined filling pressure level (Pr) is adjusted during the filling step by controlling the opening of a pressure and / or flow regulating member (8).

13. 13. The method according to claim 12, characterized in that the control of the opening of the pressure and / or flow regulating member (8) is performed during and / or before and / or after the transfer of liquid hydrogen into the tank (6), during a degassing operation of the tank (6).

14. 12. The method according to claim 11, characterized in that the step of generating a filling request signal (13) is performed manually and / or remotely and transmitting said signal to the installation (1).

15. 12. The method according to claim 11, characterized in that it comprises the steps of: calculating a predetermined temperature value (Tl) of liquefied hydrogen produced in the storage vessel (4) in response to said signal (13) before transferring liquid hydrogen from the storage vessel (4) to the tank (6); and filling the storage vessel (4) with liquefied hydrogen at said predetermined temperature (Tl).

16. 12. The method according to claim 11, characterized in that it comprises the steps of filling two separate storage vessels (4) with liquefied hydrogen at different temperatures (Tl1, Tl2) before transferring the liquid hydrogen from the storage vessels (4) to the tank (6), calculating a predetermined liquefied hydrogen temperature value (Tl) in response to the signal, and filling the tank (6) at said predetermined temperature via a mixture of liquefied hydrogen coming from the storage vessels (4).

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