Method and apparatus for liquefying hydrogen

Abstract

The present invention relates to a hydrogen liquefaction method and apparatus, wherein a first gaseous hydrogen stream (1) is pre-cooled to a first temperature and then fed into a cooling vessel (8) where it is cooled to a second temperature lower than 40 K, the cold necessary to cool said first hydrogen stream from said first temperature to said second temperature being entirely produced by expansion of a second hydrogen stream (2) through at least one expansion mechanism (10) located inside said cooling vessel (8), said second hydrogen stream (2) being gaseous at a first pressure extracted from a hydrogen distribution piping network (11, 3) connected to at least one user (13), said hydrogen distribution piping network (11, 3) having at least one hydrogen pipe (3) at a pressure comprised between 50 and 200 bars, said second hydrogen stream (2) being at a second pressure level lower than said first pressure after expansion in said at least one expansion mechanism (10), at least a first portion (122) of said second hydrogen stream (2) at said second pressure level being at least partially provided to pipes (3) of said hydrogen distribution piping network (11, 3) connected to said at least one user (13) at a pressure level corresponding to said second pressure level.

Description

Technical Field

[0001] This invention relates to a method and apparatus for hydrogen liquefaction.

[0002] More specifically, the present invention relates to a method for hydrogen liquefaction, wherein a first gaseous hydrogen stream from a first source, with a pressure between 15 and 50 bar absolutes, preferably between 17 and 30 bar absolutes, is fed into an insulated precooling container, in which the first hydrogen stream is precooled to a first temperature, for example, equal to 80 K, by means of a precooling device; the precooled first hydrogen stream is then fed into an insulated cooling container, in which the precooled first hydrogen stream is cooled from the first temperature to a second temperature below 40 K, for example, about or equal to 20 K; the first hydrogen stream cooled to the second temperature is then liquefied.

[0003] Hydrogen liquefaction requires a pressurized supply of gaseous hydrogen, for example, at a pressure between 15 and 30 absolute bar. To liquefy the hydrogen, a first pre-cooling step is performed, for example, using a first cycle (N2, mixed refrigerant, etc.). Optionally, a second pre-cooling step can be incorporated before cooling to the final temperature.

[0004] Cooling typically utilizes a refrigeration cycle of recirculated gas, such as a hydrogen cycle, to cool the hydrogen to near its liquefaction temperature. High-pressure recirculated gas (e.g., 60 bar) can be expanded in a turbine (in series and / or parallel) to approximately 7 bar abs. A portion of the recirculated hydrogen can be expanded to a relatively low pressure (e.g., between 1 and 1.5 bar abs). This low pressure can be equal to or lower than the pressure of the storage tank containing the produced liquid. Helium or neon refrigeration cycles can also be used to cool the hydrogen.

[0005] The present invention may include using and / or recovering the pressure of a gaseous stream (e.g., gaseous hydrogen or gaseous nitrogen) from a high-pressure source, such as a high-pressure pipeline (50 to 200 bar absolute), by expanding the gaseous stream to its operating pressure and using it to (completely) replace the refrigeration cycle of a hydrogen liquefaction unit.

[0006] Therefore, according to the method of the invention, which otherwise conforms to the general definition given in the preceding preamble, its main feature is that the cooling capacity for cooling the first hydrogen gas stream from the first temperature to the second temperature is generated entirely by a second gas stream in a gaseous state at a first pressure between 50 and 200 bar through at least one expansion mechanism, such as a turbine expansion, located within the cooling container. This second gas stream in the gaseous state at the first pressure is extracted from a second source comprising a hydrogen distribution pipeline network connected to at least one user, the hydrogen distribution pipeline network having at least one hydrogen pipe at a pressure between 50 and 200 bar. After expansion in the at least one expansion mechanism and supplying cooling capacity to the first hydrogen gas stream, the expanded second hydrogen gas stream is at a second pressure level below the first pressure, for example, the second pressure level is between 5 and 20 absolute bar. At least a first portion of the second hydrogen gas stream at the second pressure level is at least partially supplied to a pipe in the hydrogen distribution pipeline network connected to the at least one user at a pressure level corresponding to the second pressure level.

[0007] Furthermore, embodiments of the present invention may include one or more of the following features: - After expansion in at least one expansion mechanism and supplying cooling to the first hydrogen gas stream, a second portion of the second hydrogen gas stream, which is at the second pressure level, is expanded to a third pressure level below the second pressure level to generate additional cooling, for example, the third pressure level being between 1 and 5 absolute bar. This expanded second portion of the second hydrogen gas stream is used to cool the first hydrogen gas stream to the second temperature, and is then discharged or recycled. - The at least one expansion mechanism and the supply of cooling energy to the first hydrogen gas flow, wherein a second portion of the second hydrogen gas flow at the second pressure level is expanded to a third pressure level below the second pressure level to generate additional cooling energy, for example, the third pressure level being between 1 and 5 absolute bar, the expanded second portion of the second hydrogen gas flow being used to cool the first hydrogen gas flow to the second temperature, and then being discharged or recycled. - The expanded second portion of the second hydrogen stream, which has been used to cool the first hydrogen stream to the second temperature, is either released into the atmosphere, or, after possible compression, fed into the gaseous first hydrogen stream and / or into the pipeline network connecting to the at least one user. - The first hydrogen gas stream, cooled to the second temperature, undergoes a final expansion, the method including the steps of recovering flash gas that may be generated during the final expansion and transferring the recovered flash gas to a second portion of the second hydrogen gas stream. The method includes recovering a vaporization gas stream from at least one liquid hydrogen storage tank (e.g., a liquid hydrogen storage tank storing a first liquefied hydrogen gas stream) and / or from a mobile liquid hydrogen storage tank into a second portion of the second hydrogen gas stream. - The first hydrogen gas flow is provided at least partially by the second source. - This portion of the first hydrogen gas flow provided by the second source and the second hydrogen gas flow originate from the same hydrogen feed stream provided by the second source, which is precooled to an intermediate temperature between 100K and 80K by the precooling device and purified in a common cryogenic purification unit, such as an adsorber configured to purify the hydrogen to a predetermined degree of purity. - The precooling device includes at least one of the following: a liquefied gas source, such as liquid nitrogen or liquefied natural gas; a refrigeration cycle refrigerator, such as a mixture of nitrogen, CO2, or refrigerant. - The precooling device includes at least one high-pressure gas source, such as nitrogen or natural gas, with a pressure higher than 50 bar, which is expanded to generate precooling cold.

[0008] The present invention also relates to a hydrogen liquefaction apparatus, comprising: a supply circuit configured to supply a first gaseous hydrogen stream from a first source of gaseous hydrogen at a pressure between 15 and 50 bar, preferably between 17 and 30 bar; and a thermally adiabatic... The device includes an insulated precooling container; a precooling apparatus configured to precool the first hydrogen gas stream to a first temperature, for example, equal to 80 K, in the precooling container; an insulated cooling container and a cooling apparatus configured to cool the first hydrogen gas stream from the first temperature to a second temperature below 40 K, for example, about or equal to 20 K, in the cooling container; the apparatus comprising a gaseous hydrogen distribution pipeline network connected to at least one user, the pipeline including at least one gaseous hydrogen pipe with a pressure between 50 and 200 bar, constituting a second source of gaseous hydrogen under pressure; the cooling apparatus comprising at least one expansion mechanism, such as a turbine, located inside the cooling container and a loop of a second gaseous hydrogen stream supplied by the second source, the loop being configured to supply the at least one expansion mechanism with a second gaseous hydrogen feed stream at a first pressure between 50 and 200 bar for expansion, thereby generating a cooling capacity for cooling the first hydrogen gas stream to the second temperature; the apparatus including a transfer line for transferring at least a first portion of the second hydrogen gas stream expanded by the at least one expansion mechanism to a pipe connected to the hydrogen distribution pipeline network connected to the at least one user.

[0009] According to other possible features, the second source includes a gaseous hydrogen conduit connected to a user at a pressure between 50 and 200 bar, the conduit including a pressure reducing valve configured to reduce the pressure of the gaseous hydrogen supplied to the user to a predetermined level, the loop of the gaseous second hydrogen flow being connected upstream of the pressure reducing valve to the conduit, and a transfer line for transferring at least a first portion of the second hydrogen flow expanded by the at least one expansion mechanism (10) being connected downstream of the pressure reducing valve to the conduit.

[0010] The present invention may also relate to any alternative apparatus or method that includes any combination of the above or the following features within the scope of the claims.

[0011] Other features and advantages will become apparent after reading the following description with reference to the accompanying drawings, in which: Brief description of the attached figures The invention will be better understood after reading the following description, which is by way of example only and with reference to the accompanying drawings, in which: Figure 1 This is a partial schematic diagram illustrating the structure and possible operation of a first possible embodiment of the device according to the invention. Figure 2 This is a partial schematic diagram illustrating the structure and possible operation of a second possible embodiment of the device according to the invention. Detailed Implementation

[0012] In all the accompanying drawings, the same reference numerals refer to the same elements.

[0013] In this specific description, the following embodiments are examples. Although the specification refers to one or more embodiments, this does not mean that these features are only applicable to a single embodiment. Simple features of different embodiments may also be combined and / or interchanged to provide other embodiments.

[0014] The hydrogen liquefaction apparatus shown in a non-limiting embodiment includes a supply loop configured to supply a first gaseous hydrogen stream 1 from a first source of gaseous hydrogen. The source may include, for example, an electrolyzer (particularly an electrolyzer using renewable energy), a gaseous hydrogen delivery network, or a methane reformer.

[0015] The pressure of the first gaseous hydrogen flow 1 is, for example, between 15 and 50 bar, preferably between 17 and 30 bar (and is, for example, at ambient temperature).

[0016] The equipment includes an insulated precooling container 7 (also called a precooling box) and at least one precooling device 9. The precooling device 9 is configured to precool the first hydrogen gas flow 1 to a first temperature, for example, equal to 80K, in the precooling container 7.

[0017] The precooling device 9 may include at least one of the following: a liquefied gas source, such as liquid nitrogen or liquefied natural gas; a circulating gas refrigeration cycle refrigeration unit 26 (with compression 24 and expansion 25), such as nitrogen, CO2, a refrigerant mixture, or others.

[0018] As a variation or combination, the precooling device 9 may include at least one high-pressure gas source, such as nitrogen or natural gas, with a pressure higher than 50 bar, which is expanded to generate precooling capacity.

[0019] The device may include a purification unit 12 for the first hydrogen flow 1, for example, after the first hydrogen flow 1 has been pre-cooled.

[0020] The device includes an insulated cooling container 8 and a cooling device. The cooling device is configured to cool the first hydrogen gas stream 1 from the first temperature to a second temperature below 40K, for example, about or equal to 20K, within the cooling container 8.

[0021] like Figure 2 As shown, the first hydrogen stream 1, cooled to the second temperature, preferably undergoes a final expansion 16 (e.g., preferably a Joule Thomson type valve and / or turbine). This final expansion 16 is preferably preceded by an upstream expansion (e.g., valve 222) downstream of purification 12. That is, the first expansion 222 can bring the first hydrogen stream 1 to a pressure, for example, between 30 and 15 absolute bar, and then the second expansion (valve 16 and / or turbine) brings the first hydrogen stream 1 to a lower pressure, (at the cold end) for example, to produce a liquid (LH2) at a pressure of about 1.5 absolute bar.

[0022] The equipment includes a network of gaseous hydrogen distribution pipelines connected to at least one user 13. This one or more users may include, for example, plants such as steel mills, industrial furnaces, glass furnaces, aluminum or copper foundries, oil refineries, ammonia production units, fertilizer production units, cement plants, heating equipment, or any other equivalent equipment.

[0023] The pipeline network includes at least one gaseous hydrogen pipeline 3, 20 with a pressure between 50 and 200 absolute bar, constituting a second source of gaseous hydrogen under pressure.

[0024] The cooling device further includes at least one expansion mechanism 10, 15, such as at least one turbine 10 located within the cooling container 8. The cooling device includes a loop for a second gaseous hydrogen stream 2 supplied by the second source, the loop being configured to supply the at least one expansion mechanism 10 with a first pressure between 50 and 200 absolute bar for expansion, thereby generating cooling.

[0025] As shown in the figure, the gaseous second hydrogen stream 2 can be precooled by the precooling device and purified in the purification device 12 as needed, for example after its precooling (e.g., to remove trace amounts of N2, CO, Ar, etc.).

[0026] The cooling capacity for cooling the first hydrogen gas stream from the first temperature to the second temperature is generated entirely by the expansion of the second hydrogen gas stream 2 in a gaseous state at a first pressure between 50 and 200 absolute bar through the expansion mechanism 10, 15 located within the cooling container 8.

[0027] In other words, there is no refrigeration cycle refrigerator containing circulating hydrogen and / or helium to generate the cooling capacity required to reach the second temperature. The first hydrogen flow is cooled to the second temperature solely through the free expansion of the second hydrogen flow provided by a second gas source under high pressure supplied by the pipeline network. That is, the at least one turbine 10 and / or valve 15 does not belong to the refrigeration cycle of an additional refrigeration cycle refrigerator. Therefore, the turbine 10 and / or valve 15 are independent of any possible refrigeration cycle. Furthermore, no compressor is required to compress the second hydrogen flow 2 before it expands.

[0028] After expanding in the at least one expansion mechanism 10, 15 and providing cooling 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, for example, between 6 and 10 bar.

[0029] Furthermore, at least a first portion 122 of the second hydrogen flow 2 at the second pressure level is at least partially supplied to a pipe 3 of a hydrogen distribution pipeline network connected to the at least one user 13 at a pressure level corresponding to the second pressure level.

[0030] As shown in the figure, for this purpose, the device may include a transfer line for transferring the first portion 122 of the expanded second hydrogen stream 2 to a pipeline 3 in a hydrogen distribution pipeline network connected to the at least one user 13.

[0031] For example, the second source includes gaseous hydrogen pipelines 3 and 20 with pressures between 50 and 200 absolute bar, which are connected to user 13 via a pressure reducing valve 23 configured to reduce the pressure of the gaseous hydrogen supplied to user 13 to a predetermined level below the network pressure. For example, gaseous hydrogen is supplied to the user at a pressure below 20 absolute bar, such as between 6 and 10 absolute bar.

[0032] The circuit for the gaseous second hydrogen flow 2 can be connected upstream of the pressure reducing valve 23 to the pipe 3, 20 to extract high-pressure hydrogen therein, while the transfer line for transferring the first portion 122 of the second hydrogen flow expanded by the at least one expansion mechanism 10 can be connected downstream of the pressure reducing valve 23 to the pipe 3.

[0033] Therefore, the second pressure level can be adapted to the pressure required by the user 13 (e.g., between 12 and 4 absolute bar, preferably between 8 and 5 absolute bar).

[0034] As shown, after expansion to the second pressure level in at least one expansion mechanism 10, a second portion 123 of the second hydrogen flow 2 at the second pressure level can be extracted (e.g., via a bypass line) to be expanded, for example in valve 15, to a third pressure level below the second pressure level to generate additional cooling. This expansion of the second portion 123 of the second hydrogen flow 2 to the lower third pressure level can be specifically configured to provide the residual cooling required at the cold end of the cooling device to bring the first hydrogen flow from 40K to 20K.

[0035] The third pressure level is, for example, between 1 and 5 absolute bar. After being used to cool the first hydrogen gas stream to the second temperature, the second portion 123 can be discharged or recycled. For example, the second portion 123 of the second hydrogen gas stream 2, which has been used to cool the first hydrogen gas stream to the second temperature, can be discharged into the atmosphere, or it can be fed into the gaseous first hydrogen gas stream 1 and / or into the pipeline of the hydrogen distribution pipeline network connected to the at least one user 13 after possible compression (cryogenic compression or after reheating).

[0036] Therefore, the second part 123 can be compressed to a pressure suitable for that part of the device receiving the second part 123.

[0037] Preferably, the second portion 123 accounts for less than 50% of the second hydrogen flow 2 at the second pressure level, and more preferably between 5% and 25%, with the remaining portion (95% to 75%) consisting of the first portion 122.

[0038] Figure 2 equipment and Figure 1The main difference in the equipment is that the first hydrogen stream 1 is supplied by a second source. That is, the second hydrogen stream 2 and the first hydrogen stream 1 can be supplied by a second source, for example, from the same hydrogen feed stream 20 supplied by a second source 11. This hydrogen feed stream 20 is pre-cooled to an intermediate temperature between 80 and 100 K by a pre-cooling device 9, and is purified in a common cryogenic purification unit 12. The purification unit includes, for example, an adsorber configured to purify the hydrogen to a predetermined purity.

[0039] As in Figure 2 As schematically illustrated, the method may include the recovery 17 of flash vapor that may be generated during the final expansion 16. This flash vapor may be transferred via pipeline to a second portion 123 of the second hydrogen flow, particularly downstream of expansion 15.

[0040] Similarly, as in Figure 2 As schematically illustrated, the device can be configured to recover (pipelines 19, 20) at least one vaporized gas stream recovered in at least one liquid hydrogen storage tank in the second section 123. For example, recovering the vaporized gas from liquid hydrogen storage tank 18 storing the liquefied first hydrogen stream 1 generated by the device and / or the vaporized gas from mobile liquid hydrogen storage tank 21 supplying liquid hydrogen at the device. As shown, the vaporized gas is preferably recovered downstream of expansion valve 15, which expands the second section to a third pressure level.

[0041] In another configuration, if the cooling capacity for lowering the first hydrogen stream from a first temperature to a second temperature cannot be entirely generated by the expansion of the second gaseous hydrogen stream 2, the equipment must include an additional refrigeration unit, such as a refrigeration cycle refrigeration unit, whose circulating gas includes hydrogen and / or helium. In the case of a hydrogen refrigeration cycle, the cycle can also recover the flash vapor or evaporated gas described above. Furthermore, when needed, the cycle can feed into the first section 122 that is returned to the pipeline network.

[0042] The first and / or second source may be or include an electrolyzer that generates gaseous hydrogen at a pressure between 50 and 200 bar.

[0043] Precooling container 7 and cooling container 8 are preferably separate.

[0044] The first and second hydrogen streams can have different hydrogen contents.

[0045] [Table 1] illustrates the performance of a hydrogen liquefaction unit that produces 29 tpd (tons per day) of liquid hydrogen by cooling and liquefying a first stream of hydrogen from a first source (e.g., PSA). Under base conditions, the first stream is pre-cooled by a nitrogen refrigeration cycle, followed by cooling by a low-pressure (LP) hydrogen refrigeration cycle and a high-pressure (HP) hydrogen refrigeration cycle. It can be observed that the method uses 9 kWh to produce one kilogram of liquid hydrogen.

[0046] To reduce energy consumption, the other three embodiments use a second hydrogen flow at three different pressures (60 bar, 80 bar, and 120 bar), which is the circulation pressure of the pipe 11 from which the second hydrogen flow 2 is extracted.

[0047] In each case, the pressure of the second flow from pipe 11 is expanded 23 to the pressure of 5 absolute bar required by user 13, and the resulting cooling is used to cool the gaseous first hydrogen flow 1.

[0048] In each case, the nitrogen cycle performs precooling, and the circulating compressor for the hydrogen refrigeration cycle is no longer needed. It can be observed that the energy consumption for liquefying one kilogram of hydrogen is significantly reduced.

[0049] [Table 1] Claims (as amended under Article 19 of the Treaty) 1. A method for liquefying hydrogen, wherein a first gaseous hydrogen stream (1) from a first source, with a pressure between 15 and 50 bar, preferably between 17 and 30 bar, is fed into an insulated precooling container (7), wherein the first hydrogen stream (1) is precooled to a first temperature, for example, equal to 80 K, by a precooling device (9) in the precooling container (7), and the precooled first hydrogen stream is then fed into an insulated cooling container (8), wherein the precooled first hydrogen stream is cooled from the first temperature to a second temperature below 40 K, for example, about or equal to 20 K, and cooled to The first hydrogen gas flow at the second temperature is then liquefied, and the cooling capacity for cooling the first hydrogen gas flow from the first temperature to the second temperature is generated entirely by a second gas flow (2) of gaseous state at a first pressure between 50 and 200 bar through the expansion of at least one expansion mechanism (10), such as a turbine (10), located inside the cooling container (8). This second gas flow (2) of gaseous state at the first pressure is extracted from a second source, the second source comprising a hydrogen distribution pipeline network (11,3) connected to at least one user (13). 3) Having at least one hydrogen pipeline (3) with a pressure between 50 and 200 bar, wherein, after expansion in the at least one expansion mechanism (10) and supplying cooling 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 absolute bar, and at least a first portion (122) of the second hydrogen flow (2) at the second pressure level is at least partially supplied to the pipeline (3) of the hydrogen distribution pipeline network (11, 3) connected to the at least one user (13) at a pressure level corresponding to the second pressure level. 2. The method according to claim 1, characterized in that, after expansion in the at least one expansion mechanism (10) and supplying cooling to the first hydrogen gas stream (1), a second portion (123) of the second hydrogen gas stream (2) at the second pressure level is expanded (15) to a third pressure level below the second pressure level to generate additional cooling, for example, the third pressure level being between 1 and 5 absolute bar, the expanded second portion (123) of the second hydrogen gas stream (2) being used to cool the first hydrogen gas stream to the second temperature and then discharged or recycled. 3. The method according to claim 2, wherein the expanded second portion (123) of the second hydrogen gas stream (2) which has been used to cool the first hydrogen gas stream to the second temperature is discharged into the atmosphere, or is sent into the gaseous first hydrogen gas stream (1) after possible compression and / or into the pipe (3) of the hydrogen distribution pipeline network (11, 3) connected to the at least one user (13). 4. The method according to claim 2 or 3, wherein the second portion (123) of the second hydrogen gas flow (2) at the second pressure level accounts for less than 50%, preferably between 5% and 25%, of the second hydrogen gas flow (2) at the second pressure level, and the remaining portion (122) of the second hydrogen gas flow (2) at the second pressure level is composed of the first portion (122). 5. The method according to any one of claims 2 to 4, characterized in that the first hydrogen gas stream (1) cooled to the second temperature undergoes a final expansion (16), the method comprising the steps of recovering (17) flash vapor that may be generated during the final expansion (16) and transferring the recovered flash vapor to the second portion (123) of the second hydrogen gas stream (2). 6. The method according to any one of the preceding claims, wherein the first hydrogen gas flow (1) is provided at least in part by the second source (11, 3). 7. The method according to the preceding claims, wherein a portion (22) of the second hydrogen stream (2) provided by the second source (11, 3) and a portion (22) of the first hydrogen stream (1) originate from the same hydrogen feed stream (20) provided by the second source (11), the hydrogen feed stream (20) being precooled by the precooling device (9) to an intermediate temperature between 100K and 80K, and purified in a common cryogenic purification unit (12), such as an adsorber configured to purify hydrogen to a predetermined purity. 8. The method according to any one of the preceding claims, characterized in that the precooling device (9) comprises at least one of the following: a liquefied gas source, such as liquid nitrogen or liquefied natural gas; a circulating gas refrigeration cycle refrigeration machine, such as nitrogen, CO2, or a refrigerant mixture. 9. The method according to any one of the preceding claims, characterized in that the precooling device (9) comprises at least one high-pressure gas source, such as nitrogen or natural gas, with a pressure higher than 50 bar, which is expanded to generate precooling cold. 10. A hydrogen liquefaction apparatus comprising: a supply circuit configured to supply a first gaseous hydrogen stream (1) at a pressure between 15 and 50 bar, preferably between 17 and 30 bar, from a first source of gaseous hydrogen; an insulated precooling container (7) and a precooling device (9) configured to precool the first hydrogen stream (1) in the precooling container (7) to a first temperature, for example, equal to 80 K; an insulated cooling container (8) and a cooling device configured to cool the first hydrogen stream (1) from the first temperature to a second temperature below 40 K, for example, about or equal to 20 K, in the cooling container (8), the apparatus comprising a gaseous hydrogen distribution pipeline network (11, 3, 20) connected to at least one user (13), the pipeline network comprising at least one gaseous hydrogen pipeline (3, 20) at a pressure between 50 and 200 bar, constituting a second source of gaseous hydrogen under pressure, the cooling device comprising at least one expansion mechanism (10, 20) located inside the cooling container (8). 15) A circuit configuration, such as a turbine and a second gaseous hydrogen stream (2) supplied by the second source, the circuit being configured to supply the second gaseous hydrogen stream at a first pressure between 50 and 200 bar to the at least one expansion mechanism (10, 15) for expansion, thereby generating all the cooling capacity for cooling the first hydrogen stream (1) to the second temperature, that is, the device being configured such that the cooling capacity for cooling the first hydrogen stream from the first temperature to the second temperature is entirely generated by the expansion of the second gaseous stream through the at least one expansion mechanism (10), the device further comprising a transfer line for transferring at least a first portion (122) of the second hydrogen stream (2) expanded by the at least one expansion mechanism (10) to a pipe (3) connected to the hydrogen distribution pipeline network (11, 3) to the at least one user (13). 11. The device according to claim 10, characterized in that the second source includes a gaseous hydrogen conduit (3, 20) connected to a user (13) at a pressure between 50 and 200 bar, the conduit including a pressure reducing valve (23) configured to reduce the pressure of the gaseous hydrogen supplied to the user (13) to a predetermined level, the loop of the gaseous second hydrogen flow (2) being connected upstream of the pressure reducing valve (23) to the conduit (3, 20), and the transfer line for transferring at least a first portion (122) of the second hydrogen flow (2) expanded by the at least one expansion mechanism (10) being connected downstream of the pressure reducing valve (23) to the conduit (3).

Claims

1. A method for liquefying hydrogen, wherein, A first gaseous hydrogen stream (1) from a first source, with a pressure between 15 and 50 bar, preferably between 17 and 30 bar, is introduced into an insulated precooling container (7). The first hydrogen stream (1) is precooled to a first temperature, for example, equal to 80 K, in the precooling container (7) by a precooling device (9). The precooled first hydrogen stream is then introduced into an insulated cooling container (8), where it is cooled from the first temperature to a second temperature below 40 K, for example, about or equal to 20 K. The first hydrogen gas stream is then liquefied, and the cooling capacity for cooling the first hydrogen gas stream from the first temperature to the second temperature is generated entirely by a second gas stream (2) in gaseous state at a first pressure between 50 and 200 bar through the expansion of at least one expansion mechanism (10), such as a turbine (10), located inside the cooling container (8). This second gas stream (2) in gaseous state at the first pressure is extracted from a second source, the second source comprising a hydrogen distribution pipeline network (11,3) connected to at least one user (13). 3) Having at least one hydrogen pipeline (3) with a pressure between 50 and 200 bar, wherein, after expansion in the at least one expansion mechanism (10) and supplying cooling 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 absolute bar, and at least a first portion (122) of the second hydrogen flow (2) at the second pressure level is at least partially supplied to the pipeline (3) of the hydrogen distribution pipeline network (11, 3) connected to the at least one user (13) at a pressure level corresponding to the second pressure level.

2. The method according to claim 1, characterized in that, After expansion in at least one expansion mechanism (10) and supplying cooling to the first hydrogen gas stream (1), a second portion (123) of the second hydrogen gas stream (2) at the second pressure level is expanded (15) to a third pressure level below the second pressure level to generate additional cooling, for example, the third pressure level being between 1 and 5 absolute bar. This expanded second portion (123) of the second hydrogen gas stream (2) is used to cool the first hydrogen gas stream to the second temperature and then discharged or recycled.

3. The method according to claim 2, characterized in that, The expanded second portion (123) of the second hydrogen stream (2) which has been used to cool the first hydrogen stream to the second temperature is discharged into the atmosphere, or, after possible compression, is fed into the gaseous first hydrogen stream (1) and / or into the pipe (3) of the hydrogen distribution pipeline network (11, 3) connected to the at least one user (13).

4. The method according to claim 2 or 3, characterized in that, The second portion (123) of the second hydrogen flow (2) at the second pressure level accounts for less than 50%, preferably between 5% and 25%, of the second hydrogen flow (2) at the second pressure level, and the remaining portion (122) of the second hydrogen flow (2) at the second pressure level is composed of the first portion (122).

5. The method according to any one of claims 2 to 4, characterized in that, The first hydrogen stream (1) cooled to the second temperature undergoes a final expansion (16), and the method includes the steps of recovering (17) flash vapor that may be generated during the final expansion (16) and transferring the recovered flash vapor to the second portion (123) of the second hydrogen stream (2).

6. The method according to any one of claims 2 to 5, characterized in that, The method includes the step of recovering (19, 20) an evaporated gas stream from at least one liquid hydrogen storage tank (18, 20), such as a liquid hydrogen storage tank (18) and / or a mobile liquid hydrogen storage tank (21) storing the liquefied first hydrogen stream (1), the recovered evaporated gas stream being injected into the second portion (123) of the second hydrogen stream (2).

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

8. The method according to the preceding claim, wherein, The second hydrogen stream (2) provided by the second source (11, 3) and a portion (22) of the first hydrogen stream (1) originate from the same hydrogen feed stream (20) provided by the second source (11), the hydrogen feed stream (20) being precooled to an intermediate temperature between 100K and 80K by the precooling device (9) and purified in a common cryogenic purification unit (12), such as an adsorber configured to purify hydrogen to a predetermined purity.

9. The method according to any one of the preceding claims, characterized in that, The precooling device (9) includes at least one of the following: a liquefied gas source, such as liquid nitrogen or liquefied natural gas; a circulating refrigeration system for circulating gas, such as nitrogen, CO2, or a mixture of refrigerants.

10. The method according to any one of the preceding claims, characterized in that, The precooling device (9) includes at least one high-pressure gas source, such as nitrogen or natural gas, with a pressure higher than 50 bar, which is expanded to generate precooling cold.

11. A hydrogen liquefaction device, comprising: A supply loop is configured to supply a first gaseous hydrogen stream (1) from a first gaseous hydrogen source at a pressure between 15 and 50 bar, preferably between 17 and 30 bar; an insulated precooling container (7) and a precooling device (9) configured to precool the first hydrogen stream (1) to a first temperature, for example, equal to 80 K, in the precooling container (7); an insulated cooling container (8) and a cooling device configured to cool the first hydrogen stream (1) from the first temperature to a second temperature below 40 K, for example, about or equal to 20 K, in the cooling container (8), the equipment including a network of gaseous hydrogen distribution pipes (11, 3, 20) connected to at least one user (13), the network including at least one gaseous hydrogen pipe (3, 20) at a pressure between 50 and 200 bar, constituting a second source of gaseous hydrogen under pressure, the cooling device consisting of at least one expansion mechanism (10, 10, 10) located inside the cooling container (8). 15) A circuit, such as a turbine and a second gaseous hydrogen stream (2) supplied by the second source, is configured to supply the at least one expansion mechanism (10, 15) with a second gaseous hydrogen stream at a first pressure between 50 and 200 bar for expansion, thereby generating a cooling capacity for cooling the first hydrogen stream (1) to the second temperature. The device includes a transfer line for transferring at least a first portion (122) of the second hydrogen stream (2) expanded by the at least one expansion mechanism (10) to a pipe (3) of the hydrogen distribution pipeline network (11, 3) connected to the at least one user (13).

12. The device according to claim 11, characterized in that, The second source includes a gaseous hydrogen conduit (3, 20) connected to a user (13) at a pressure between 50 and 200 bar. The conduit includes a pressure reducing valve (23) configured to reduce the pressure of the gaseous hydrogen supplied to the user (13) to a predetermined level. The loop of the gaseous second hydrogen flow (2) is connected upstream of the pressure reducing valve (23) to the conduit (3, 20). The transfer line for transferring at least a first portion (122) of the second hydrogen flow (2) expanded by the at least one expansion mechanism (10) is connected downstream of the pressure reducing valve (23) to the conduit (3).

Images