COOLING METHOD FOR LIQUEFYING A FEED GAS

Abstract

The present invention pertains to a cooling method for liquefying a feed gas, comprising the steps of providing a cooling cycle with a refrigerant stream; dividing the refrigerant stream into a first partial stream and a second partial stream; expanding the first partial stream in a first expansion device; and transferring cooling energy from the expanded first partial stream to a feed gas stream to be cooled, particularly comprising hydrogen and/or helium. Further the method comprises the steps of guiding the expanded first partial stream to a suction inlet of an ejector; and guiding the second partial stream to a propellant inlet of the ejector such that, upon expanding the second partial stream in the ejector, the expanded first partial stream is compressed and merged with the expanded second partial stream.

Claims

1. Cooling method for liquefying a feed gas, comprising the steps of: providing a cooling cycle with a refrigerant stream; dividing the refrigerant stream into a first partial stream and a second partial stream; expanding the first partial stream in a first expansion device; and, transferring cooling energy from the expanded first partial stream to a feed gas stream to be cooled, wherein the method further comprises the steps of: guiding the expanded first partial stream to a suction inlet of an ejector; and, guiding the second partial stream to a propellant inlet of the ejector such that, upon expanding the second partial stream in the ejector, the expanded first partial stream is compressed and merged with the expanded second partial stream.

2. Method according to claim 1, wherein, by transferring cooling energy from the expanded first partial stream to the feed gas stream to be cooled, particularly by means of a first heat exchanger, the feed gas stream is cooled to a temperature below the critical temperature of hydrogen, particularly below 24 K, so as to provide a liquid product stream comprising hydrogen.

3. Method according to claim 1, wherein an expanded refrigerant stream is provided by merging the compressed first partial stream with the expanded second partial stream in the ejector, and wherein the method further comprises the step of guiding the expanded refrigerant stream through a compressor unit, particularly comprising or consisting of at least one piston compressor so as to compress the expanded refrigerant stream, thereby providing the refrigerant stream.

4. Method according to claim 1, further comprising the step of guiding the expanded refrigerant stream and the first partial stream such that heat is transferred, particularly by means of a second heat exchanger, between the expanded refrigerant stream and the first partial stream and particularly the feed gas stream.

5. Method according to claim 1, further comprising the step of partially expanding the second partial stream in a second expansion device particularly a Joule-Thomson-valve and/or an expansion turbine, prior to being guided to the ejector and/or the step of guiding the second partial stream) into the ejector, particularly by bypassing the second expansion device.

6. Method according to claim 1, wherein the refrigerant stream is further separated into at least one third partial stream, particularly at different temperature levels, and the method further comprises the steps of: expanding the at least one third partial stream in at least one third expansion device, particularly in at least one expansion turbine; and guiding the at least one expanded third partial stream and the first partial stream such that heat is transferred, particularly by means of at least one third heat exchanger, between the at least one expanded third partial stream and the first partial stream and particularly the feed gas stream; and, feeding the at least one expanded third partial stream to the expanded refrigerant stream.

7. Method according to claim 1, wherein the expanded first partial stream is guided into a gas liquid separator arranged downstream of the first expansion device and configured to store the refrigerant in a liquid and gaseous phase, and wherein the expanded first partial stream in a liquid phase is guided from the separator, particularly through the first heat exchanger acting as an evaporator, to the suction inlet of the ejector.

8. Method according to claim 1, wherein the refrigerant stream) is precooled by means of a closed precooling cycle having a further refrigerant stream comprising or consisting of nitrogen, wherein in particular the further refrigerant stream is expanded in a fourth expansion device prior to being supplied to a fourth heat exchanger for transferring cooling energy to the refrigerant stream and particularly to the feed gas stream.

9. Cooling system for liquefying a feed gas, having a cooling circuit with a refrigerant line for circulating a refrigerant stream, wherein the cooling circuit further comprises: an expansion device configured to expand a first partial stream flowing through a first junction line branching off from the refrigerant line; and, a heat exchanger for transferring cooling energy from the expanded first partial stream to a feed gas stream to be cooled, wherein the cooling circuit further comprises an ejector having a suction inlet connected to the first junction line for receiving the expanded first partial stream and a propellant inlet connected to a second junction line branching off from the refrigerant line for receiving a second partial stream, wherein the ejector is configured to, upon expanding the second partial stream in the ejector, compress the expanded first partial stream and merge it with the expanded second partial stream.

10. Cooling system according to claim 9, wherein the heat exchanger is configured to transfer cooling energy from the expanded first partial stream to the feed gas stream to be cooled such that the feed gas stream is cooled to a temperature below the critical temperature of hydrogen, particularly below 24 K, so as to provide a liquid product stream comprising hydrogen.

11. Cooling system according to claim 9, wherein the cooling system further comprises a compressor unit configured to compress an expanded refrigerant stream output by the ejector and formed by merging the compressed first partial stream with the expanded second partial stream so as to provide the refrigerant stream, and wherein the compressor unit comprises or consists of at least one piston compressor.

12. Cooling system according to claim 9, further comprising a second heat exchanger configured to transfer heat between the expanded refrigerant stream and the first partial stream and particularly the feed gas stream.

13. Cooling system according to claim 9, further comprising a second expansion device, particularly a Joule-Thomson-valve and/or an expansion turbine, arranged upstream of the ejector and configured to partially expand the second partial stream flowing through the second junction line, wherein particularly a bypass line is provided through which at least a part of the second partial stream is guided and which is configured for bypassing the second expansion device and guiding the second partial stream flowing therethrough into the ejector.

14. Cooling system according to claim 9, further comprising: at least one third expansion device configured to expand at least one third partial stream flowing through at least one third junction line which branches off from the refrigerant line at different temperature levels, at least one third heat exchanger for transferring heat between the at least one expanded third partial stream and the first partial stream and particularly the feed gas stream; and, at least one supply line arranged downstream of the at least one third heat exchanger for feeding the at least one expanded third partial stream to the expanded refrigerant stream.

15. Cooling system according to claim 9, further comprising: a gas liquid separator arranged downstream of the first expansion device and configured to receive the expanded first partial stream and to store the refrigerant of the expanded first partial stream in a liquid and gaseous phase, an ejector supply line for guiding the expanded first partial stream in a liquid phase from the separator, particularly evaporated in the first heat exchanger, to the suction inlet of the ejector, and/or a closed precooling cycle for precooling the refrigerant stream of the cooling cycle, wherein the closed precooling cycle has a further refrigerant stream, particularly comprising or consisting of nitrogen or liquid natural gas, a fourth expansion device for expanding the further refrigerant stream, and a fourth heat exchanger configured to transfer heat between the expanded further refrigerant stream and the refrigerant stream and particularly the feed gas stream.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0039] The present disclosure will be more readily appreciated by reference to the following detailed description when being considered in connection with the accompanying drawings in which:

[0040] FIG. 1 is a schematic thermodynamic process diagram illustrating an industrial hydrogen liquefaction plant with a cooling system which uses a cooling method according to an embodiment of the present invention: and

[0041] FIG. 2 is a schematic thermodynamic process diagram illustrating a further industrial hydrogen liquefaction plant with a cooling system which uses the cooling method according to a further embodiment of the present invention.

DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS

[0042] In the following, the invention will be explained in more detail with reference to the accompanying figures. In the figures, like elements are denoted by identical reference numerals and repeated description thereof may be omitted in order to avoid redundancies.

[0043] FIG. 1 illustrates a process design for an industrial hydrogen liquefaction plant for hydrogen liquefaction on a large-scale. The depicted industrial hydrogen liquefaction plant comprises a hydrogen cooling and liquefaction unit 10, to which a feed gas stream 12 comprising hydrogen is supplied. Upon flowing through the hydrogen cooling and liquefaction unit 10, the hydrogen feed gas stream 12 is cooled and thereby liquefied so as to generate a liquid product stream 14.

[0044] In order to provide cooling energy for cooling and liquefaction of the hydrogen gas stream, the industrial hydrogen liquefaction plant is thermally coupled to a cooling system 16 comprising a precooling cycle 18 and a main cooling cycle 20 in form of closed-loop refrigeration cycles. The precooling cycle 18 and the main cooling cycle 20 may be provided in one or two separate vacuum insulated cold-box vessels. In the embodiment shown in FIG. 1, the cooling system comprises a precooling cold-box 22 and a main cooling cold-box 24.

[0045] At first, the main cooling cycle 20 is described in more detail. In the main cooling cycle 20, a refrigerant comprising a cryogenic suitable gas, i. e. hydrogen, circulates, thereby successively passing a compressor unit 26, the precooling cold-box 22 and the main cooling cold-box 24. Prior to entering the precooling cold-box 22, the refrigerant is compressed to high pressure, thereby providing a refrigerant stream 28 flowing through a refrigerant line 30 with a pressure typically below 30 bar, e.g. 10 bar, but may also have a pressure up to 70 bar or at least 25 bar and particularly with an ambient temperature, e.g. 303 K. In general, proper operation may be ensured as soon as the refrigerant is compressed to a level allowing for enough enthalpy removal in the further process. In some configurations, this may be achieved at a pressure level of 10 bar. The higher the pressure level of the refrigerant, the higher the heat removal in the turbine, but at the same time, heat exchangers grow in thickness, which may affect their efficiency.

[0046] Thereafter, the refrigerant stream 28 is guided through the precooling cold-box 22, where it is precooled to a lower precooling temperature of, e.g. at most 100 K and preferably 80 K. Also, the precooling temperature may be 115 K, for example, when the cooling energy for precooling the refrigerant stream 28 is provided by means of a liquid natural gas (LNG) as a cooling fluid. If temperature of the refrigerant is kept above 80 K and the refrigerant comprises hydrogen, then additional effort may be required for the purification of the hydrogen prior to entering into the cold-box 24, since impurities may freeze out in the heat exchanger.

[0047] Upon flowing through the main cooling cold-box 24, the refrigerant stream 28 is divided into a first partial stream 32 flowing through a first junction line 34 and a second partial stream 36 flowing through a second junction line 38. In the first junction line 34, the first partial stream 32 is expanded in a first expansion device 40, i.e. through a Joule-Thomson throttle valve, and thereby cooled. In this way, the high pressure first partial stream 32 is processed so as to generate a low pressure expanded first partial stream with a pressure particularly between 1.1 bar to 8 bar and a temperature sufficiently low to ensure a proper cooling of the feed gas stream 12, e.g. between 20 K and 24 K. Thereafter, the expanded first partial stream is supplied to a gas liquid separator 44 arranged downstream of the first expansion device 40 and configured to store the refrigerant in a liquid and gaseous phase. From the separator 44, a liquid expanded first partial stream 42, i.e. the expanded first partial stream 32 comprising hydrogen in a liquid phase, is guided through a first heat exchanger 46.

[0048] Specifically, the first heat exchanger 46 is provided in form of a plate-fin heat exchanger through which both the feed gas stream 12 and the expanded first partial stream 42 in its liquid phase are guided. Accordingly, the first heat exchanger 46 is configured to transfer cooling energy from the expanded first partial stream 42 to the feed gas stream 12 to be cooled. More specifically, cooling energy is transferred from the expanded first partial stream 42 to the feed gas stream 12 such that the feed gas stream 12 is cooled to a temperature below the critical temperature of hydrogen, particularly below 24 K, thereby ensuring that the liquid product stream 14 is output from the hydrogen cooling and liquefaction unit 10. At the same time, heat of reaction from the ortho para conversion is removed in preferably every heat exchanger passage of the liquefaction unit 10 following the absorber 104. In a further development, the ortho para conversion may be integrated into the absorber 104.

[0049] In the main cooling cycle 20, the cooling system 16 comprises an ejector 48 having a propellant inlet and a suction inlet. After passing the first heat exchanger 46, the expanded first partial stream 42 is guided to the suction inlet of the ejector 48. Further, the second partial stream 36, after being partially expanded in a second expansion device 50 comprising a throttle valve and an expansion turbine, is guided to the propellant inlet of the ejector 48. Accordingly, the suction inlet of the ejector 48 is connected to the first junction line 34 for receiving the expanded first partial stream 42 and the propellant inlet of the ejector 48 is connected to the second junction line 38 for receiving a partially expanded second partial stream 52. Additionally, for control purposes, the second partial stream 36 at least partially may be guided directly into the ejector 48 by bypassing the second expansion device 50. Compared to the expanded first partial stream 42, the partially expanded second partial stream 52 has an intermediate pressure level that is higher than the low-pressure level of the expanded first partial stream 42.

[0050] In this configuration, the ejector 48 functions as a pumping device which is driven by the partially expanded second partial stream 52 and configured to compress the expanded first partial stream 42. More specifically, the partially expanded second partial stream 52 constitutes a propellant medium which, upon flowing through the ejector 48 and due to a momentum transfer induced by the geometric configuration of the ejector 48, compresses the expanded first partial stream 42 which constitutes a suction medium.

[0051] In the following, the configuration and operation of the ejector 48 is described in more detail. The ejector 48 comprises the propellant inlet for receiving the pressurized propellant that is supplied to a nozzle, i.e. a laval nozzle, communicating to a suction chamber of the ejector 48. The ejector further comprises the suction inlet which opens into the suction chamber and is configured to supply the suction fluid into the suction chamber, wherein the suction fluid has a pressure lower than a pressure of the propellant fluid supplied to the propellant inlet. The suction chamber communicates to a fluid outlet of the ejector 48 via a convergent-divergent diffuser.

[0052] In operation of the ejector 48, the pressurized propellant fluid, i.e. the partially expanded second partial stream 52 enters the propellant inlet of the ejector 48 and is then accelerated to a high velocity through the nozzle which discharges a high velocity jet stream of the fluid through the suction chamber into the convergent-divergent diffuser. As a result, a reduced pressure in the chamber is generated causing a draw in of the expanded first partial stream 42 which is entrained by and drawn into the convergent-divergent diffuser with the high velocity fluid stream. The thus combined fluid undergoes compression as it passes through a convergent inlet portion of the diffuser and, thereafter, deceleration and expansion as it passes through the divergent outlet portion of the diffuser.

[0053] In this way, upon expanding the partially expanded second partial stream in the ejector 48, the expanded first partial stream 42 is compressed and merged with the expanded second partial stream, thereby generating an expanded refrigerant stream 54 output by the ejector 48 into a recirculation line 56. In this configuration, the ejector 48 is provided such that the expanded refrigerant stream 54 output by the ejector 48 has a medium pressure level that is higher than the low pressure level of the expanded first partial stream 42 and lower than the intermediate pressure level of the partially expanded second partial stream 52.

[0054] Further, the expanded refrigerant stream 54, the first partial stream 32 and the feed gas stream 12 are guided through a second heat exchanger 58 such that heat is transferred therebetween. Specifically, the cooling system 16 comprises the second heat exchanger 58 in form a plate-fin heat exchanger, through which the expanded refrigerant stream 54, the first partial stream 32 and the feed gas stream 12 are guided and which is configured to transfer cooling energy from the expanded refrigerant stream 54 to both the first partial stream 32 and the feed gas stream 12.

[0055] In the main cooling cycle 20, the refrigerant stream 28 is further divided, at different temperature levels, into a third partial stream 60 flowing through a third junction line 62 and a fourth partial stream 64 flowing through a fourth at junction line 65. In the third junction line 62, a third expansion device 66 is arranged which is configured to expand the third partial stream 60 so as to generate an expanded third partial stream 68. Specifically, the third expansion device 66 comprises, for example, two expansion turbines connected in series in the third junction line 62. In an alternative embodiment, the third expansion device may also comprise one or more expansion turbines connected in series and/or in parallel.

[0056] The expanded third partial stream 68 together with the expanded refrigerant stream 54, the first partial stream 32 together with the second partial stream 36, and the feed gas stream 12 are guided through a third heat exchanger 70 such that cooling energy is transferred from the expanded refrigerant stream 54 and the expanded first partial stream 68 to the first partial stream 32, the second partial stream 36 and the feed gas stream 12. Specifically, the expanded third gas stream 68 is supplied from the third expansion device 66 via a first supply line 72 to the recirculation line 56 downstream of the third heat exchanger 70. In other words, the first supply line 72 is configured to feed the expanded third partial stream 68 two the expanded refrigerant stream 54 downstream of the third heat exchanger 70.

[0057] In the fourth junction line 65, a fourth expansion device 74 is arranged which is configured to expand the fourth partial stream 64 so as to provide an expanded fourth partial stream 76. In an alternative embodiment, the liquefaction plant 10 may also comprise more or less than four junction lines, i.e. depending on the plant capacity. Specifically, the fourth expansion device 74 comprises, for example, two expansion turbines connected in series in the fourth junction line 65. Each of the expansion devices 50, 66, 74 is configured for or has the function of performing a gas expansion such that mechanical labor is removed from the respective gas stream. For doing so, the design of each expansion device 50, 66, 74 may be adapted to a capacity of the plant 10. Thus, of course, the configuration of these components may differ compared to the present design depending on the specific application. For example, each expansion device may comprise one or more expansion turbines or other expansion units which may be arranged in series and/or in parallel.

[0058] The expanded fourth partial stream 76, the first partial stream 32, the second partial stream 36, the third partial stream 60, the expanded refrigerant stream 54 and the feed gas stream 12 are guided through a fourth heat exchanger 78. The fourth heat exchanger 78 is configured to transfer cooling energy from the expanded fourth partial stream 76, the expanded third partial stream 68 and the expanded refrigerant stream 54 to the first to third partial streams 32, 36, 60 and the feed gas stream 12. Specifically, this is realized by supplying the expanded fourth partial stream 76 via a second supply line 80 from the fourth expansion device 74 to the recirculation line 56 downstream of the fourth heat exchanger 78. In other words, the second supply line 80 is configured to feed the expanded fourth partial stream 76 to the expanded refrigerant stream 54 downstream of the fourth heat exchanger 78.

[0059] The recirculation line 56 is configured to guide the expanded refrigerant stream 54 and the expanded third and fourth partial streams 68, 76 to the compressor unit 26. The compressor unit 26 comprises a piston compressor system 82 which is configured to, upon being flown through with the fluid stream flowing through the recirculation line 56, compress the expanded refrigerant stream together with the expanded third and fourth partial streams 68, 76, thereby providing the refrigerant stream 28. In this way, a closed cooling cycle is provided. Specifically, as depicted in FIG. 1, the piston compressor system 82 comprises two piston compressors. Alternatively, the piston compressors system 82 may comprise one or more piston compressors.

[0060] After being compressed by the piston compressors 82, the refrigerant stream 28 is guided through a fifth heat exchanger 84, which is fed with a cooling water stream 86. Specifically, the fifth heat exchanger 84 is configured to transfer cooling energy from the cooling water stream 86 to the refrigerant stream 28. Downstream of the fifth heat exchanger 84, the cooling water passes through a valve 88.

[0061] Upon flowing through the precooling cold-box 22, the refrigerant stream 28 is precooled by means of the closed precooling cycle 18 which has a further refrigerant stream 90 comprising or consisting of nitrogen or liquefied natural gas (LNG). Specifically, the further refrigerant stream 90 is expanded in a fifth expansion device 92 provided in form of a throttle valve prior to being successively supplied to a further gas liquid separator 94 and a sixth heat exchanger 96. Specifically, the sixth heat exchanger 96 is configured to transfer cooling energy from the further refrigerant stream 90 and the fluid flowing through the recirculation line 56 to the refrigerant stream 28 and the feed gas stream 12. By means of the further separator 94, the further refrigerant stream 90 is separated into a mainly gaseous phase and a many liquid phase, wherein the mainly liquid phase is separately guided through the sixth heat exchanger 96. The third to sixth heat exchangers 70, 78, 84 and 96 are provided in form plate-fin heat exchangers.

[0062] At the outlet of the sixth heat exchanger 96, the refrigerant stream 28 is guided through an adsorber 98 to remove impurities present in the refrigerant stream 28. In case the refrigerant stream 28 comprises or consist of LNG, the adsorber 104 may be located further downstream. Further, at the outlet of the fifth heat exchanger 84, a third supply line 100 is provided comprising a valve 102, via which gaseous refrigerant, e. g. hydrogen, for example from a storage tank, particularly a high pressure storage tank and/or a mobile storage tank, can be supplied into the refrigerant line 30.

[0063] In the following, the configuration of the hydrogen cooling and liquefaction unit 10 is described in more detail. After entering the hydrogen cooling and liquefaction unit 10, the feed gas stream 12 is guided through the sixth heat exchanger 96 so as to be precooled to a lower precooling temperature, e.g. 100 K, particularly by the precooling cycle 18. At the outlet of the sixth heat exchanger 96, residual impurities are removed from the precooled hydrogen feed gas 12 by means of adsorber vessels 104. After this feed gas purification by means of the adsorber vessels 104, the precooled feed gas stream 12 is routed back to the sixth heat exchanger 96 through a passage 106 filled with a catalyst. In this way, the precooled feed gas stream 12 is brought into contact with the catalyst being able to catalyze a conversion of ortho hydrogen to para hydrogen. Thereafter, the feed gas stream 12 successively passes the fourth, third and second heat exchangers 78, 70, 58 having integrated catalyst prior to being supplied to a sixth expansion device comprising a throttle valve 108 and a further ejector 110. After passing the sixth expansion device, the feed gas stream 12 is guided through the first heat exchanger 46 and a seventh expansion device 112 so as to generate the liquid product stream 14 having a storage pressure in the range of 1 to 3.5 bar. The thus generated liquid product stream 14 is guided to a storage tank configured to store hydrogen in its liquid and gaseous phase.

[0064] Specifically, the further ejector 110 has a propellant inlet for receiving the feed gas stream 12 and a suction inlet for receiving a gaseous hydrogen stream 114. Preferably, the gaseous hydrogen stream 114 is discharged from the storage tank and supplied to the suction inlet of the further ejector 110.

[0065] Furthermore, downstream of the adsorber vessels 104, a branch line 116 is provided having a throttle valve 118, via which at least a part of the feed gas stream 12 can be branched off and supplied to the recirculating line 56 of the main cooling cycle 20.

[0066] FIG. 2 depicts a process design for an industrial hydrogen liquefaction plant for hydrogen liquefaction on a large-scale according to a further embodiment. The following description of the liquefaction plant particularly involves the differences compared to the previously described embodiment depicted in FIG. 1 so as to omit a repeated description and to avoid redundancies.

[0067] As depicted in FIG. 2, upon flowing through the main cooling cold-box 24, the refrigerant stream 28 is divided into the first partial stream 32 flowing through the first junction line 34 and the second partial stream 36 flowing through the second junction line 38. Prior to being branched off, the refrigerant stream 28 is guided through a seventh heat exchanger 120. The seventh heat exchanger 120 is provided such that the feed gas stream 12 is guided therethrough upstream of the sixth heat exchanger 96 and downstream of the fourth heat exchanger 78 so as to transfer heat from the feed gas stream 12 to the expanded refrigerant stream 56.

[0068] The first partial stream 32, after being branched off from the refrigerant stream 28, is successively guided through the fourth, the third and the second heat exchanger 78, 70, 58 and thereafter through an eighth heat exchanger 122 prior to being supplied to the separator 44. The eighth heat exchanger 122 is provided such that the feed gas stream 12 is guided therethrough upstream of the second heat exchanger 58 and downstream of the further ejector 110 so as to transfer heat from the feed gas stream 12 to the expanded refrigerant stream 56.

[0069] The second partial stream 36, after being partially expanded in a second expansion device 50, is guided through the third heat exchanger 70 and thereafter to the propellant inlet of the ejector 48. In a further development, for control purposes, the second partial stream 36 at least partially may be guided directly into the ejector 48 and/or the third heat exchanger 70 by bypassing the second expansion device 50.

[0070] Further, separate to a first suction line for supplying the liquid expanded first partial stream 42 from the separator 44 to the suction inlet of the ejector 48, a second suction line 124 is provided for supplying a gaseous expanded first partial stream 126, i.e. a part of the expanded first partial stream 32 comprising hydrogen in a gaseous phase, from the separator 44 to a further suction inlet of the ejector 48. Compared to the liquid expanded first partial stream 42, the gaseous expanded first partial stream 126 bypasses the first heat exchanger 46. The second suction line may also be provided in the configuration depicted in FIG. 1.

[0071] Upstream of the further ejector 110 and downstream of the first heat exchanger 46, a further branch line 128 is provided having a throttle valve 130, via which at least a part of the feed gas stream 12 can be branched off and supplied to the separator 44.

[0072] It will be obvious for a person skilled in the art that these embodiments and items only depict examples of a plurality of possibilities. Hence, the embodiments shown here should not be understood to form a limitation of these features and configurations. Any possible combination and configuration of the described features can be chosen according to the scope of the invention.

LIST OF REFERENCE NUMERALS

[0073] 10 hydrogen cooling liquefaction unit

[0074] 12 feed gas stream

[0075] 14 liquid product stream

[0076] 16 cooling system

[0077] 18 precooling cycle

[0078] 20 main cooling cycle

[0079] 22 precooling cold-box

[0080] 24 main cooling cold-box

[0081] 26 compressor unit

[0082] 28 refrigerant stream

[0083] 30 refrigerant line

[0084] 32 first partial stream

[0085] 34 first junction line

[0086] 36 second partial stream

[0087] 38 second junction line

[0088] 40 first expansion device

[0089] 42 liquid expanded first partial stream

[0090] 44 gas liquid separator

[0091] 46 first heat exchanger

[0092] 48 ejector

[0093] 50 second expansion device

[0094] 52 partially expanded second partial stream

[0095] 54 expanded refrigerant stream

[0096] 56 recirculation line

[0097] 58 second heat exchanger

[0098] 60 third partial stream

[0099] 62 third junction line

[0100] 64 fourth partial stream

[0101] 65 fourth junction line

[0102] 66 third expansion device

[0103] 68 expanded third partial stream

[0104] 70 third heat exchanger

[0105] 72 first supply line

[0106] 74 second expansion device

[0107] 76 expanded fourth partial stream

[0108] 78 fourth heat exchanger

[0109] 80 second supply line

[0110] 82 piston compressor system

[0111] 84 fifth heat exchanger

[0112] 86 cooling water stream

[0113] 88 throttle valve

[0114] 90 further refrigerant stream

[0115] 92 throttle valve

[0116] 94 further gas liquid separator

[0117] 96 sixth heat exchanger

[0118] 98 adsorber

[0119] 100 third supply line

[0120] 102 throttle valve

[0121] 104 adsorber vessel

[0122] 106 heat exchanger passage

[0123] 108 throttle valve

[0124] 110 further ejector

[0125] 112 seventh expansion device

[0126] 114 gaseous hydrogen stream

[0127] 116 branch line

[0128] 118 throttle valve

[0129] 120 seventh heat exchanger

[0130] 122 eighth heat exchanger

[0131] 124 second suction line

[0132] 126 gaseous expanded first partial stream

[0133] 128 further branch line

[0134] 130 further throttle valve