Hydrogen liquefaction process and installation

Abstract

The invention relates to a method and a hydrogen liquefaction installation in which a first flow of gaseous hydrogen (1) is pre-cooled to a first temperature and then sent into a cooling enclosure (8) where it is cooled to a second temperature below 40K, the cold for cooling the first flow of hydrogen from the first temperature to the second temperature being produced exclusively by the expansion by at least one expansion member (10) in the cooling enclosure (8) of a second flow of hydrogen (2), the second flow of gaseous hydrogen (2) at the first pressure being taken from a network (11, 3) of hydrogen distribution pipes to at least one user (13) having at least one hydrogen pipe (3) at a pressure between 50 and 200 bars, after its expansion in the at least one expansion member (10), the second expanded hydrogen flow (2) is at a second pressure level lower than the first pressure,at least a first fraction (122) of this second hydrogen flow (2) at the second pressure level being at least partly supplied to a pipeline (3) of the network (11, 3) of hydrogen distribution pipelines towards the at least one user (13) which has a pressure level corresponding to the second pressure level. Abstract figure: Fig. 1,

Description

Title of the invention: Method and installation for liquefying hydrogen

[0001] The invention relates to a method and an installation for liquefying hydrogen.

[0002] The invention relates more particularly to a method for liquefying hydrogen in which a first flow of gaseous hydrogen at a pressure between 15 and 50 bar abs, preferably between 17 and 30 bar abs, coming from a first source, is sent into a thermally insulated pre-cooling enclosure, the first flow of hydrogen being pre-cooled in the pre-cooling enclosure to a first temperature, for example equal to 80K, by means of a pre-cooling device, the first flow of pre-cooled hydrogen then being sent into a thermally insulated cooling enclosure in which it is cooled from the first temperature to a second temperature lower than 40K and for example of the order of or equal to 20K, the first flow of hydrogen cooled to the second temperature then being liquefied.

[0003] The liquefaction of hydrogen requires a feed flow of pressurized hydrogen gas, for example at a pressure between 15 and 30 bar abs. To liquefy the hydrogen, a first pre-cooling step is carried out, for example, using a first cycle (N2, mixed refrigerants, etc.). Optionally, a second pre-cooling step may be provided before cooling to the final temperature.

[0004] Cooling generally uses a cycle gas refrigeration cycle, for example a hydrogen cycle to cool the hydrogen almost to the liquefaction temperature. The high pressure cycle gas (for example 60 bar) can be expanded in turbines (in series and / or in parallel) to about 7 bar abs. A portion of the cycle hydrogen can be expanded to a relatively low pressure (for example between 1 and 1.5 bar abs). This low pressure can be equal to or lower than the pressure of the product liquid storage. It is also possible to use helium or neon refrigeration cycles to cool the hydrogen.

[0005] The invention may consist of using and / or enhancing the pressure of a gas flow, for example gaseous hydrogen or gaseous nitrogen, from a high pressure source, for example a high pressure network (50 to 200 bar abs), by expanding it to its operating pressure and using it to (totally) replace a refrigeration cycle of a hydrogen liquefier.

[0006] To this end, the method according to the invention, moreover in accordance with the generic definition given in the preamble above, is essentially characterized in that that the cold for cooling the first flow of hydrogen from the first temperature to the second temperature is produced exclusively by the expansion by at least one expansion member such as a turbine located inside the cooling enclosure of a second flow of gaseous hydrogen at a first pressure of between 50 and 200 bars, the second flow of gaseous hydrogen at the first pressure being taken from a second source comprising a hydrogen distribution pipeline network to at least one user, the hydrogen distribution pipeline network having at least one hydrogen pipeline at a pressure of between 50 and 200 bars, in which, after its expansion in the at least one expansion member and the supply of cold to the first flow of hydrogen, the second expanded hydrogen flow is at a second pressure level lower than the first pressure, for example the second pressure level is between 5 and 20 bar abs,at least a first fraction of this second hydrogen flow at the second pressure level being at least partly supplied to a pipeline of the hydrogen distribution pipeline network towards the at least one user who has a pressure level corresponding to the second pressure level.

[0007] Furthermore, embodiments of the invention may include one or more of the following features: - after its expansion in the at least one expansion member and the supply of cold to the first hydrogen flow, a second fraction of the second hydrogen flow at the second pressure level is expanded to a third pressure level lower than the second pressure level, to produce additional cold power, for example the third pressure level is between 1 and 5 bar abs, this second fraction of the second expanded hydrogen flow being used to cool the first hydrogen flow to the second temperature and is then evacuated or recovered, - the at least one expansion member and the supply of cold to the first hydrogen flow, a second fraction of the second hydrogen flow at the second pressure level is expanded to a third pressure level lower than the second pressure level, to produce additional cold power, for example the third pressure level is between 1 and 5 bar abs,this second fraction of the second expanded hydrogen flow being used to cool the first hydrogen flow to the second temperature and then being evacuated or recovered, - the second fraction of the second hydrogen flow expanded and which was used to cool the first hydrogen flow to the second temperature is evacuated to the atmosphere or is sent, after possible compression, into the first gaseous hydrogen flow and / or into a pipeline from the hydrogen distribution pipeline network to at least one user, - the first flow of hydrogen cooled to the second temperature undergoes a final expansion, the method comprising a step of recovering any "flash" gas produced during this final expansion and transferring this recovered flash gas into the second fraction of the second flow of hydrogen, - the method comprises a step of recovering, in the second fraction of the second flow of hydrogen, a flow of vaporization gas recovered in at least one liquid hydrogen storage, for example a liquid hydrogen storage storing the first flow of liquefied hydrogen and / or a mobile liquefied hydrogen storage, - the first flow of hydrogen is provided at least in part by the second source, - the second hydrogen flow and the part of the first hydrogen flow supplied by the second source come from the same hydrogen flow supplied by the second source which is pre-cooled to an intermediate temperature of between 100K and 80K by the pre-cooling device and which is purified in a common cryogenic purification member, such as an adsorber configured to purify the hydrogen to a determined degree of purity, - the pre-cooling device comprises at least one of: a source of liquefied gas such as liquid nitrogen, liquefied natural gas, a refrigerator with a cycle gas refrigeration cycle, for example nitrogen, CO2, a refrigerant mixture, - the pre-cooling device comprises at least one source of high pressure gas greater than 50 bar, for example nitrogen or natural gas which is expanded to produce pre-cooling cold power.

[0008] The invention also relates to a hydrogen liquefaction installation comprising a supply circuit configured to supply, from a first source of gaseous hydrogen, a first flow rate of gaseous hydrogen at a pressure between 15 and 50 bar abs, preferably between 17 and 30 bar abs, a thermally insulated pre-cooling enclosure, a pre-cooling device configured to pre-cool the first flow rate of hydrogen in the pre-cooling enclosure to a first temperature, for example equal to 80K, a thermally insulated cooling enclosure and a cooling device configured to cool the first flow rate of hydrogen in the cooling enclosure from the first temperature to a second temperature lower than 40K and for example of the order of or equal to 20K, the installation comprising a pipeline network for distributing gaseous hydrogen to at least one user,said network comprising at least one pipeline, of gaseous hydrogen at a pressure of between 50 and 200 bars constituting a second source of pressurized gaseous hydrogen, the cooling device consisting of at least one expansion member such as a turbine located inside the cooling enclosure and a circuit of a second flow of gaseous hydrogen supplied by the second source configured to supply a second flow of gaseous hydrogen at a first pressure of between 50 and 200 bars to the at least one expansion member for the purpose of its expansion to produce cold to cool the first flow of hydrogen to the second temperature, the installation comprising a transfer pipe of at least a first fraction of this second flow of hydrogen expanded by the at least one expansion member to a pipe of the network of hydrogen distribution pipes to the at least one user.

[0009] According to other possible features, the second source comprises a pipeline of gaseous hydrogen at a pressure of between 50 and 200 bars connected to a user, said pipeline comprising a pressure reducer configured to lower the pressure of the gaseous hydrogen supplied to the user to a determined level, the circuit of the second flow of gaseous hydrogen being connected to said pipeline upstream of the pressure reducer, the transfer line of at least a first fraction of the second flow of hydrogen expanded by the at least one expansion member (10) being connected to this pipeline downstream of the pressure reducer.:

[0010] The invention may also relate to any alternative device or method comprising any combination of the above or below features within the scope of the claims.

[0011] Other features and advantages will appear on reading the description below, given with reference to the figures in which: Brief description of the figures

[0012] The invention will be better understood on reading the following description given solely by way of example and with reference to the appended drawings in which:

[0013] [Fig. 1] is a schematic and partial view illustrating the structure and possible operation of a first possible embodiment of an installation according to the invention,

[0014] [Fig.2] is a schematic and partial view illustrating the structure and possible operation of a second possible embodiment of an installation according to the invention. Detailed description

[0015] In all the figures, the same references refer to the same elements.

[0016] In this detailed description, the following embodiments are examples. Although the description refers to one or more embodiments, this does not mean that the features apply only to a single embodiment. Single features of different embodiments may also be combined and / or interchanged to provide other embodiments.

[0017] The hydrogen liquefaction installation illustrated in the non-limiting examples comprises a supply circuit configured to supply, from a first source of gaseous hydrogen, a first flow rate 1 of gaseous hydrogen. The source may comprise, for example, an electrolyzer in particular using renewable energy, a gaseous hydrogen transport network, a methane reformer.

[0018] The first flow of gaseous hydrogen 1 is at a pressure for example between 15 and 50 bar abs, preferably between 17 and 30 bar abs (and for example at ambient temperature).

[0019] The installation comprises a thermally insulated pre-cooling enclosure 7 (also called a pre-cooling cold box) and at least one pre-cooling device 9. The pre-cooling device 9 is configured to pre-cool the first flow of hydrogen 1 in the pre-cooling enclosure 7 to a first temperature, for example equal to 80K.

[0020] The pre-cooling device 9 may comprise at least one of: a source of liquefied gas such as liquid nitrogen, liquefied natural gas, a cycle refrigerator 26 for refrigerating a cycle gas (compression 24 and expansion 25), for example nitrogen, CO2, a refrigerant mixture or other.

[0021] Alternatively or in combination, the pre-cooling device 9 may comprise at least one source of high pressure gas greater than 50 bar abs, for example nitrogen or natural gas which is expanded to produce a pre-cooling cold power.

[0022] The installation may comprise a device 12 for purifying the first flow of hydrogen 1, for example after its pre-cooling.

[0023] The installation comprises a thermally insulated cooling enclosure 8 and a cooling device. The cooling device is configured to cool the first flow of hydrogen 1 in the cooling enclosure 8 from the first temperature to a second temperature less than 40K and for example of the order of or equal to 20K.

[0024] As illustrated in [Fig.2], the first flow of hydrogen 1 cooled to the second temperature preferably undergoes a final expansion 16 (valve(s) preferably of the Joule Thomson type for example and / or turbine(s)).

[0025] The installation comprises a network of pipelines for distributing gaseous hydrogen to at least one user 13. The user(s) may comprise, for example: a factory, for example a steelworks, an industrial furnace, a glass furnace, a aluminum or copper smelter, a refinery, an ammonia production unit, a fertilizer production unit, a cement plant, a heating installation or any other equivalent installation.

[0026] This network comprises at least one pipeline 3, 20 of gaseous hydrogen at a pressure of between 50 and 200 bar abs constituting a second source of gaseous hydrogen under pressure.

[0027] The cooling device further comprises at least one expansion member 10, 15 such as at least one turbine 10 located inside the cooling enclosure 8. The cooling device comprises a circuit of a second flow of gaseous hydrogen 2 supplied by the second source configured to supply a second flow of gaseous hydrogen at a first pressure of between 50 and 200 bar abs to the at least one expansion member 10 for the purpose of its expansion to produce cold.

[0028] As illustrated, the second flow of gaseous hydrogen 2 can be pre-cooled by the pre-cooling device and, if necessary, purified in a purification device 12, for example after its pre-cooling (to remove traces of N2, CO, Ar, etc., for example).

[0029] The cold for cooling the first flow of hydrogen from the first temperature to the second temperature is produced exclusively by the expansion by the at least one expansion member 10, 15 located inside the enclosure 8 for cooling the second flow of gaseous hydrogen 2 to a first pressure of between 50 and 200 bar abs.

[0030] That is to say that there is no refrigerator with a refrigeration cycle of a cycle gas containing hydrogen and / or helium to produce the cold necessary for cooling to the second temperature. The first flow of hydrogen is cooled to the second temperature only by this free expansion of the second flow of hydrogen supplied by the second source of high-pressure gas supplied by the network. That is to say that the at least one turbine 10 and / or valve 15 does not belong to a refrigeration cycle of a refrigerator with an additional refrigeration cycle. The turbine 10 and / or valve 15 is thus independent of any refrigeration cycle. In addition, no compressor is necessary to compress the second flow of hydrogen 2 before its expansion.

[0031] After its expansion in the at least one expansion member 10, 15 and the supply of cold to the first hydrogen flow 1, the second expanded hydrogen flow 2 is at a second pressure level lower than the first pressure, for example the second pressure level is between 5 and 20 bar abs, for example between 6 and 10 bar abs.

[0032] In addition, at least a first fraction 122 of this second flow of hydrogen 2 at the second pressure level is at least partly supplied to a pipe 3 of the hydrogen distribution pipeline network to the at least one user 13 which has a pressure level corresponding to the second pressure level.

[0033] As illustrated, the installation may comprise for this purpose a pipe for transferring this first fraction 122 of this second flow of expanded hydrogen 2 into a pipe 3 of the hydrogen distribution pipe network to the at least one user 13.

[0034] For example, the second source comprises a pipe 3, 20 of gaseous hydrogen at a pressure of between 50 and 200 bar abs connected to a user 13 via a pressure reducer 23 configured to lower the pressure of the gaseous hydrogen supplied to the user 13 to a determined level lower than the network pressure. For example, the user is supplied with gaseous hydrogen at a pressure of less than 20 bar abs, for example between 6 and 10 bar abs.

[0035] The circuit of the second flow of gaseous hydrogen 2 can be connected to said pipe 3, 20 upstream of the expander 23 to take the high-pressure hydrogen therefrom, while the transfer pipe of the first fraction 122 of the second flow of hydrogen expanded by the at least one expansion member 10 can be connected to this pipe 3 downstream of the expander 23.

[0036] Thus, the second pressure level can be adapted to the pressure required by the user 13 (for example between 12 and 4 bar abs, preferably between 8 and 5 bar abs).

[0037] As illustrated, after its expansion in the at least one expansion member 10 to the second pressure level, a second fraction 123 of the second hydrogen flow 2 at the second pressure level can be taken (for example via a bypass line) to be expanded, for example in a valve 15, to a third pressure level lower than the second pressure level to produce additional cold power. This expansion of the second fraction 123 of the second hydrogen flow 2 to the third lower pressure level can in particular be configured to provide the residual cold power necessary at the cold end of the cooling device to bring the first hydrogen flow from 40K to 20K.

[0038] The third pressure level is for example between 1 and 5 bar abs. After use to cool the first flow of hydrogen to the second temperature, this second fraction 123 can be evacuated or recovered. For example, this second fraction 123 of the second flow of hydrogen 2 which has been used to cool the first flow of hydrogen to the second temperature can be evacuated to the atmosphere or can be sent, after possible compression (cryogenic compression or after reheating), into the first flow of gaseous hydrogen 1 and / or into a pipeline of the network of hydrogen distribution pipelines to the at least one user 13.

[0039] Thus, this second fraction 123 can be compressed to a pressure adapted to the pressure required by the part of the installation that receives it.

[0040] Preferably this second fraction 123 represents less than 50% and preferably between 5 and 25% of the second hydrogen flow rate 2 at the second pressure level, the remainder (95 to 75%) being constituted by the first fraction 122.

[0041] The installation of [Fig. 2] differs from that of [Fig. 1] essentially in that the first hydrogen flow 1 is supplied by the second source. That is to say that the second hydrogen flow 2 and the first hydrogen flow 1 can be supplied by the second source, for example from the same hydrogen flow 20 supplied by the second source 11 which is pre-cooled to an intermediate temperature between 100K and 80K by the pre-cooling device 9 and which is purified in a common cryogenic purification member 12. The purification member comprises for example an adsorber configured to purify the hydrogen to a determined degree of purity.

[0042] As also illustrated schematically in [Fig.2], the method may comprise a recovery 17 of the possible “flash” gas produced during the final expansion 16. This flash gas may be transferred via a pipe into the second fraction 123 of the second hydrogen flow, in particular downstream of the expansion 15.

[0043] Similarly, as illustrated schematically in [Fig.2], the installation can be configured to recover (lines 19, 20), in the second fraction 123 at least one stream of vaporization gas recovered in at least one liquid hydrogen storage. For example, the vaporization gas from a liquid hydrogen storage 18 storing the first flow 1 of liquefied hydrogen produced by the installation and / or the vaporization gas from a mobile liquefied hydrogen storage 21 which is supplied with liquid hydrogen at the installation is recovered. As illustrated, the vaporization gases are preferably recovered downstream of the expansion valve 15 which expands the second fraction to a third pressure level.

[0044] In another configuration, if the cold for cooling the first flow of hydrogen from the first temperature to the second temperature cannot be produced exclusively by the expansion of the second flow of gaseous hydrogen 2, the installation must then comprise an additional refrigerator, for example with a refrigeration cycle whose cycle gas comprises hydrogen and / or helium. In the case of a hydrogen refrigeration cycle, this cycle can also recover the flash or vaporization gases described above. In addition, this cycle can feed, if necessary, into the first fraction 122 returned to the network.

[0045] The first and / or the second source may be or comprise an electrolyzer producing hydrogen gas at a pressure between 50 and 200 bar abs.

[0046] The pre-cooling 7 and cooling 8 enclosures are preferably separate.

[0047] The first and second hydrogen flows may have different hydrogen contents.

[0048] [Table 1] illustrates the performance of a hydrogen liquefier producing 29 tpd (tonne per day) of liquid hydrogen by cooling and liquefying a first flow of hydrogen from a first source, for example a PSA. In the base case, a nitrogen refrigeration cycle precools the first flow and then a low pressure (LP) hydrogen refrigeration cycle and a high pressure (HP) hydrogen refrigeration cycle cool the first flow. It can be seen that the process uses 9 kWh to produce one kg of liquid hydrogen.

[0049] In order to reduce energy consumption, three other examples use a second flow of hydrogen at three different pressures (60 bar abs, 80 bar abs, 120 bar abs) which is the circulation pressure of a pipe 11 from which the second flow 2 is drawn.

[0050] In each case, the second flow rate is expanded 23 from the pressure of the pipe 11 to a pressure of 5 bar abs required for the user 13 and the frigories produced participate in cooling the first flow rate of gaseous hydrogen 1.

[0051] In each case, the nitrogen cycle performs the pre-cooling and the cycle compressor of the hydrogen refrigeration cycle is no longer necessary. It can be seen that the energy consumption for liquefying one kilogram of hydrogen is greatly reduced.

[0052] [TAB.l] Precooling LP HP TOTAL Base case 29tpd 1.6 —> 12 bar abs 35000 Nm3 / h N2 6500 Nm3 / h H2 1. —> 6.1 bar abs 6 —> 60 bar abs 62000 Nm3 / h 9.0 kWh / kg Pipeline 60bar abs P 5bars 1.6 —> 12 bar abs 35000 Nm3 / h N2 1.1 —> 6.1 bar abs 6500 Nm3 / h H2 No compressor 3.4 kWh / kg Pipeline 80bar abs P 5b 1.6 —> 12 bar abs 37500 Nm3 / h N2 1.1 —> 6.1 bar abs 6500 Nm3 / h H2 No compressor 3.6 kWh / kg Pipeline 120bar abs P 5b 1.6 —> 12 bar abs 1.1 —> 6.1 bar abs 6500 Nm3 / h H2 No compressor

Claims

Claims

1. A method for liquefying hydrogen in which a first flow of gaseous hydrogen (1) at a pressure between 15 and 50 bar abs, preferably between 17 and 30 bar abs, from a first source is sent into a thermally insulated pre-cooling enclosure (7), the first flow of hydrogen (1) being pre-cooled in the pre-cooling enclosure (7) to a first temperature, for example equal to 80K, by means of a pre-cooling device (9), the first flow of pre-cooled hydrogen then being sent into a thermally insulated cooling enclosure (8) in which it is cooled from the first temperature to a second temperature lower than 40K and for example of the order of or equal to 20K, the first flow of hydrogen cooled to the second temperature then being liquefied,the cold for cooling the first hydrogen flow from the first temperature to the second temperature being produced exclusively by the expansion by at least one expansion member (10) such as a turbine (10) located inside the cooling enclosure (8) of a second flow of gaseous hydrogen (2) at a first pressure of between 50 and 200 bars, the second flow of gaseous hydrogen (2) at the first pressure being taken from a second source comprising a network (11, 3) of hydrogen distribution pipes to at least one user (13), the network (11, 3) of hydrogen distribution pipes having at least one hydrogen pipe (3) at a pressure of between 50 and 200 bars, in which, after its expansion in the at least one expansion member (10) and the supply of cold to the first hydrogen flow (1), the expanded second hydrogen flow (2) is at a second pressure level lower than the first pressure,for example the second pressure level is between 5 and 20 bar abs, at least a first fraction (122) of this second hydrogen flow (2) at the second pressure level being at least partly supplied to a pipe (3) of the network (11, 3) of hydrogen distribution pipes towards the at least one user (13) who has a pressure level corresponding to the second pressure level.,

2. Method according to claim 1, characterized in that, after its expansion in the at least one expansion member (10) and the supply of cold to the first hydrogen flow (1), a second fraction (123) of the second hydrogen flow (2) at the second pressure level is expanded (15) to a third pressure level lower than the second pressure level, to produce additional cold power, for example the third pressure level is between 1 and 5 bar abs, this second fraction (123) of the second expanded hydrogen flow (2) being used to cool the first hydrogen flow to the second temperature and is then evacuated or recovered.

3. Method according to claim 2, characterized in that the second fraction (123) of the second hydrogen flow (2) expanded and which has been used to cool the first hydrogen flow to the second temperature is evacuated to the atmosphere or is sent, after possible compression, into the first gaseous hydrogen flow (1) and / or into a pipe (3) of the network (11, 3) of hydrogen distribution pipes to the at least one user (13).

4. Method according to claim 2 or 3, characterized in that the second fraction (123) of the second hydrogen flow (2) at the second pressure level represents less than 50% and preferably between 5 and 25% of the second hydrogen flow (2) at the second pressure level, the remainder (122) of the second hydrogen flow (2) at the second pressure level being constituted by the first fraction (122).

5. Method according to any one of claims 2 to 4, characterized in that the first flow of hydrogen (1) cooled to the second temperature undergoes a final expansion (16), the method comprising a step of recovering (17) any “flash” gas produced during this final expansion (16) and the transfer of this recovered flash gas into the second fraction (123) of the second flow of hydrogen (2).

6. Method according to any one of claims 2 to 5, characterized in that it comprises a step of recovery (19, 20), in the second fraction (123) of the second hydrogen flow (2), of a flow of vaporization gas recovered in at least one storage (18, 20) of liquid hydrogen, for example a storage (18) of liquid hydrogen storing the first flow (1) of liquefied hydrogen and / or a storage (21) of mobile liquefied hydrogen.

7. Method according to any one of the preceding claims in which the first flow of hydrogen (1) is provided at least in part by the second source (11, 3).

8. Method according to the preceding claim in which the second hydrogen flow (2) and the part (22) of the first hydrogen flow (1) supplied by the second source (11, 3) come from the same flow of hydrogen (20) supplied by the second source (11) which is pre-cooled to an intermediate temperature between 100K and 80K by the pre-cooling device (9) and which is purified in a common cryogenic purification member (12), such as an adsorber configured to purify the hydrogen to a determined degree of purity.

9. Method according to any one of the preceding claims, characterized in that the pre-cooling device (9) comprises at least one of: a source of liquefied gas such as liquid nitrogen, liquefied natural gas, a refrigerator with a refrigeration cycle of a cycle gas, for example nitrogen, CO2, a refrigerant mixture.

10. Method according to any one of the preceding claims, characterized in that the pre-cooling device (9) comprises at least one source of high pressure gas greater than 50 bar, for example nitrogen or natural gas which is expanded to produce a cold pre-cooling power.

11. Hydrogen liquefaction installation comprising a supply circuit configured to supply, from a first source of gaseous hydrogen, a first flow of gaseous hydrogen (1) at a pressure between 15 and 50 bar abs, preferably between 17 and 30 bar abs, a thermally insulated pre-cooling enclosure (7), a pre-cooling device (9) configured to pre-cool the first flow of hydrogen (1) in the pre-cooling enclosure (7) to a first temperature, for example equal to 80K, a thermally insulated cooling enclosure (8) and a cooling device configured to cool the first flow of hydrogen (1) in the cooling enclosure (8) from the first temperature to a second temperature lower than 40K and for example of the order of or equal to 20K, the installation comprising a network (11, 3, 20) of hydrogen distribution pipes gaseous towards at least one user (13),said network comprising at least one pipeline (3, 20) of gaseous hydrogen at a pressure of between 50 and 200 bars constituting a second source of gaseous hydrogen under pressure, the cooling device consisting of at least one expansion member (10, 15) such as a turbine located inside the cooling enclosure (8) and a circuit of a second flow of gaseous hydrogen (2) supplied by the second source configured to provide a second flow of gaseous hydrogen at a first pressure of between, between 50 and 200 bars to the at least one expansion member (10, 15) with a view to its expansion to produce the cold to cool the first flow of hydrogen (1) to the second temperature, the installation comprising a transfer pipe of at least a first fraction (122) of this second flow of hydrogen (2) expanded by the at least one expansion member (10) to a pipe (3) of the network (11, 3) of hydrogen distribution pipes to the at least one user (13).

12. Installation according to claim 11, characterized in that the second source comprises a pipe (3, 20) of gaseous hydrogen at a pressure of between 50 and 200 bars connected to a user (13), said pipe comprising a pressure reducer (23) configured to lower the pressure of the gaseous hydrogen supplied to the user (13) to a determined level, the circuit of the second flow of gaseous hydrogen (2) being connected to said pipe (3, 20) upstream of the pressure reducer (23), the transfer pipe of at least a first fraction (122) of the second flow of hydrogen (2) expanded by the at least one expansion member (10) being connected to this pipe (3) downstream of the pressure reducer (23).

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