PLANT FOR HYDROGEN PURIFICATION AND METHOD FOR HYDROGEN PURIFICATION

Abstract

Hydrogen purification. A plant and a method for hydrogen purification are provided, comprising an oscillation adsorption stage (sa) and a recycling of purged gaseous impurities.

Description

1 / 17 PLANT FOR HYDROGEN PURIFICATION AND METHOD FOR HYDROGEN PURIFICATION TECHNICAL FIELD

[0001] The present invention relates to a plant and a method for hydrogen purification, comprising an Oscillation Adsorption (SA) step and a recycling of purged gaseous impurities. FUNDAMENTALS

[0002] Hydrogen production in a steam reforming process requires a purification step. In steam reforming, this is done by Pressure Swing Absorption (PSA). However, PSA will also retain some of the hydrogen, which is why this technology typically yields 80 to 90% hydrogen. The remaining hydrogen is lost in a low-pressure waste gas, which is better used for heating in other parts of the plant.

[0003] A hydrogen separation technology more efficient than PSA is desirable, which can avoid the over-design of steam reforming plants. SUMMARY

[0004] A plant for supplying a stream of H2-rich gas from a hydrocarbon feed is provided, said plant comprising: - a section of the reformer designed to receive said hydrocarbon feed and reform it in at least one reforming stage conducted at an initial pressure to provide a synthesis gas stream; - a CO2 removal stage, designed to receive the synthesis gas stream from the aforementioned section of the reformer. Petition 870260073078, dated 07 / 22 / 2026, page 10 / 39 2 / 17 and separate CO2 from the synthesis gas stream, in order to provide a CO2-rich stream and a CO2-poor stream; - an Oscillation Adsorption (SA) stage, said SA stage comprising an adsorption material and a first purge stream with a pressure equal to or greater than the first pressure; and being arranged to receive the CO2-poor stream from the CO2 removal stage; - where the aforementioned SA stage comprises a first state (A) and a second state (B), in which; In the aforementioned first state (A), the CO2-poor stream is arranged to contact the adsorption material so that; at least a portion of the gaseous impurities from said CO2-deficient stream, and a portion of the hydrogen from said CO2-deficient stream CO2 are adsorbed onto the aforementioned adsorption material, thus providing a stream rich in H2; in said second state (B), the first purge stream is arranged to contact the adsorption material so that at least a portion of the adsorbed gaseous impurities and at least a portion of said adsorbed hydrogen are released from said adsorption material and into the first purge stream; thus providing a first recycling stream comprising said first purge stream, hydrogen and said gaseous impurities; - the aforementioned plant being arranged to recycle the aforementioned first recycling stream to the section of Petition 870260073078, dated 07 / 22 / 2026, page 11 / 39 3 / 17 reformer as feed for the reforming stage.

[0005] The present technology also provides a method for supplying a H2-rich gas stream from a hydrocarbon feed. The method comprises the general steps of: i. provide a plan as described in this document; ii. feed the hydrocarbon feed to the reformer section and reform it in at least one reforming stage conducted at an initial pressure to provide a synthesis gas stream; iii. feed the synthesis gas stream from the aforementioned section of the reformer to the CO2 removal stage, and separate CO2 from the synthesis gas stream, so as to provide a CO2-rich stream and a CO2-poor stream; iv. feeding the CO2-poor stream from the CO2 removal phase to the Oscillation Adsorption (SA) phase comprising an adsorption material and a first purge stream with pressure equal to or greater than the first pressure, wherein said SA phase comprises a first state (A) and a second state (B), in which; - In the aforementioned first state, the CO2-poor stream contacts the adsorption material in such a way that at least a portion of the gaseous impurities from said CO2-poor stream, and a portion of the hydrogen from said CO2-poor stream, CO2 are adsorbed onto the aforementioned adsorption material, thus providing a stream rich in H2; Petition 870260073078, dated 07 / 22 / 2026, page 12 / 39 4 / 17 - in said second state, the first purge stream contacts the adsorption material such that at least a portion of the adsorbed gaseous impurities and at least a portion of said adsorbed hydrogen are released from said adsorption material and into the first purge stream; thus providing a first recycling stream comprising said first purge stream, hydrogen and said gaseous impurities; and v. recycle the aforementioned first recycling stream to the reformer section as feed for the reforming stage.

[0006] Further details of the technology are presented in the following detailed description, in the figures and in the attached claims. CAPTIONS

[0007] Fig. 1 illustrates a schematic configuration of a hydrogen plant according to the present invention. DETAILED REVELATION

[0008] When a section, unit, or stage is arranged to receive a particular gas from another section, unit, or stage, it is normally arranged to receive it directly. However, under certain circumstances, an intermediate section, unit, or stage is present through which the specific gas may be passed. Specific modalities

[0009] Hereafter, the abbreviation % vol should be used to mean the percentage by volume for a gas.

[00010] A hydrogen plant is provided, that is, a plant to supply a gas stream rich in H2 from a hydrocarbon feed. The term rich Petition 870260073078, dated 07 / 22 / 2026, page 13 / 39 5 / 17 in H2 should be understood as meaning on the order of 95% by volume or more.

[00011] The hydrocarbon feed is typically selected from natural gas, town gas, naphtha, or biogas, and natural gas is preferred. The hydrocarbon feed is characterized by containing a majority (i.e., more than 50%) of hydrocarbons, for example, methane, ethane, propane, butane, and the like. In addition, nitrogen, argon, and carbon dioxide, among others, may be present. Note that the hydrocarbon feed will be mixed with streams containing hydrogen, steam, carbon dioxide, and / or oxygen within the reformer section to facilitate the reforming reaction.

[00012] Generally, the plant comprises: - a reformer section; - a stage of CO2 removal; and - a stage of Oscillation Adsorption (SA).

[00013] The reformer section is arranged to receive hydrocarbon feed and reform it in at least one reforming stage to provide a synthesis gas stream. Reforming hydrocarbons into synthesis gas is a known procedure and does not need to be discussed in detail in this document.

[00014] Typically, and as shown in Figure 1, the reformer section comprises one or more primary reformer units and, optionally, one or more pre-reformer units arranged in the hydrocarbon feed upstream of said reformer unit(s). If no pre-reformer unit is Petition 870260073078, dated 07 / 22 / 2026, page 14 / 39 6 / 17 present, the hydrocarbon feed is received by the primary reformer unit. If pre-reformer units are present, the hydrocarbon feed is received by the pre-reformer unit(s). One or more primary reformer units may be selected from an autothermal reformer (ATR), a steam methane reforming reactor (SMR), a convective reforming reactor and / or a catalytic oxidation reforming reactor (CATOX).

[00015] The CO2 removal stage is arranged to receive the synthesis gas stream from the aforementioned reformer section and separate the CO2 from the synthesis gas stream, so as to provide a CO2-rich stream and a CO2-poor stream. The CO2 content in the CO2-poor steam will typically be below 2%, while the CO2-rich stream may comprise more than 90% CO2. A CO2 removal stage is understood to be a unit that uses a process, such as chemical absorption, to remove CO2 from the process gas. In chemical absorption, the gas containing CO2 passes through a solvent that reacts with the CO2 and thus binds it. Most chemical solvents are amines, classified as primary amines such as monoethanolamine (MEA) and digylcolamine (DGA), secondary amines such as diethanolamine (DEA) and diisopropanolamine (DIPA), or tertiary amines such as triethanolamine (TEA) and methyldiethanolamine (MDEA), but ammonia and liquid alkaline carbonates such as K2CO3 and NaCO3 can also be used.

[00016] The Oscillation Adsorption (SA) stage comprises an adsorption material and a first purge stream. The adsorption material can be selected from Petition 870260073078, dated 07 / 22 / 2026, page 15 / 39 7 / 17 starting from a zeolite, activated carbon, or metal-organic structure or mixtures thereof. The adsorption material is typically in the form of an adsorption bed within the SA stage. Oscillation Adsorption refers to a unit for adsorbing selected compounds. In this type of equipment, a dynamic equilibrium is established between the adsorption and desorption of gas molecules onto an adsorption material. The adsorption of gas molecules can be caused by steric, kinetic, or equilibrium effects. The exact mechanism will be determined by the adsorbent used, and the equilibrium saturation will depend on the temperature and pressure. Typically, the adsorbent material is treated in the mixed gas until near saturation of the heavier compounds and subsequently requires regeneration. Regeneration can be done by altering the pressure or temperature, or by purging with another stream.In practice, this means that a process with at least two units is used, saturating the adsorbent at high pressure or low temperature initially in one unit and then switching units, now desorbing the adsorbed molecules from the same unit, decreasing the pressure or increasing the temperature or purging with another stream.

[00017] The SA stage is organized to receive the CO2-poor stream from the CO2 removal stage. The SA stage comprises a first state (A) and a second state (B) and is interchangeable between these states. The change between states may involve opening or closing streams to the SA stage. In one aspect, the change between states involves a change in temperature. Petition 870260073078, dated 07 / 22 / 2026, page 16 / 39 8 / 17 of the SA stage, that is, the SA stage is a Temperature Swing Adsorption (TSA) stage. In this respect, therefore, the temperature of the SA stage in the second state (B) is higher than in the aforementioned first state (A).

[00018] Appropriately, the SA stage is arranged to alternate between the aforementioned first (A) and second (B) states. To improve efficiency and reduce fluctuations in production, the SA stage may have several parallel adsorption reactions in different stages (A, B) at a given time.

[00019] In the first state (A), the CO2-poor stream is arranged to come into contact with the adsorption material so that; at least a portion (and preferably all) of the gaseous impurities from said CO2-poor stream, and a portion of the hydrogen from said CO2-poor stream, are adsorbed onto said adsorption material. Since only a portion of the hydrogen from the CO2-poor stream is adsorbed, this leaves unadsorbed H2 to continue through the SA stage, thus providing an H2-rich stream.

[00020] Gaseous impurities are typically one or more of the following gases: CO2, CO, Ar, H2O, N2 and CH4.

[00021] The second state (B) is the purge state, in which the impurities in the adsorption material will be replaced by the purge. In the second state (B) of stage SA, the first purge stream is arranged to come into contact with the adsorption material so that at least Petition 870260073078, dated 07 / 22 / 2026, page 17 / 39 9 / 17 A portion (and preferably all) of the adsorbed gaseous impurities and at least a portion (and preferably all) of said adsorbed hydrogen is released from said adsorption material and into the first purge stream. In this way, a first recycling stream is provided comprising the first purge stream, hydrogen, and said gaseous impurities in a mixture. As illustrated in Figure 1, the plant is arranged to feed the first recycling stream to the reformer section. The plant may be arranged to feed the first recycling stream upstream of one or more pre-reformer units, if present.

[00022] Stage SA may comprise a second purge stream and a third state (C). In this third state, the second purge stream is arranged to purge in contact with the adsorption material subsequent to purging with the first purge recycling stream so that at least a portion of the gaseous impurities are released from said adsorption material; thus providing a second recycling stream that is recycled upstream of the reforming stage of said reforming section. In this way, the adsorption material is washed with a preferred gas phase before returning to state A and, consequently, contamination of the H2-rich stream by the first purge stream used in state B is avoided. The second purge stream may advantageously be hydrogen. In a particular embodiment, the second purge stream has a pressure equal to or greater than the first pressure.

[00023] In a preferred aspect, the first current of Petition 870260073078, dated 07 / 22 / 2026, p. 18 / 39 10 / 17 purge is a superheated steam stream. Steam is a particularly attractive purge stream because it is needed as co-feed for the hydrocarbon feed to the reformer section, and therefore the combined stream of the first purge stream with hydrogen and gaseous impurities can be collectively recycled. As illustrated in Figure 1, additional steam can be added to the recycle to exactly match the steam addition needed at the reformer section. Another advantage of using steam is that it can be easily removed from the H2-rich stream subsequently by condensation. The superheated steam stream can be arranged to provide at least part of the temperature increase of the SA stage from the first state (A) to the second state (B).Superheated steam can be obtained from any part of the plant, for example, other units such as the waste heat boiler and / or steam superheaters in heaters / waste heat sections.

[00024] In an alternative aspect, the first purge stream is a fraction of the hydrocarbon feed, in the form of natural gas. This allows the combined stream of the first purge stream with hydrogen and gaseous impurities to be collectively recycled to the reformer section.

[00025] In another aspect, the first and / or second purge streams are hydrogen streams. In this way, contamination of the H2-rich stream by the first purge stream is avoided.

[00026] A preferred setting is to use steam as the Petition 870260073078, dated 07 / 22 / 2026, page 19 / 39 11 / 17 first purge stream and no second purge stream. An alternative preferred configuration is to use natural gas as the first purge stream and hydrogen as the second purge stream.

[00027] The plant may further comprise a displacement section disposed in said synthesis gas stream between said reformer section and said CO2 removal stage. The displacement section is designed to adjust the content of the synthesis gas stream; particularly the H / CO ratio, depending on the desired plant output and / or the type of hydrocarbon feed.

[00028] Note that suitable heat exchangers / temperature regulation stages and water removal stages are applied as needed to facilitate the process. The details of these have not been described, as a technical person in the field of chemical process design considers them easily adaptable.

[00029] The present technology also provides a method for supplying a H2-rich gas stream from a hydrocarbon feed. The method comprises the general steps of: i. provide a plan as described in this document; ii. feed the hydrocarbon feed to the reformer section and reform it in at least one reforming stage conducted at an initial pressure to provide a synthesis gas stream; iii. feed the synthesis gas stream from the aforementioned section of the reformer to the CO2 removal stage, and Petition 870260073078, dated 07 / 22 / 2026, page 20 / 39 12 / 17 separate CO2 from the synthesis gas stream, in order to provide a CO2-rich stream and a CO2-poor stream; iv. feeding the CO2-poor stream from the CO2 removal stage to the Oscillation Adsorption (SA) stage comprising an adsorption material and a first purge stream with a pressure equal to or greater than the first pressure, wherein said SA stage comprises a first state (A) and a second state (B), in which; - In the aforementioned first state, the CO2-poor stream contacts the adsorption material in such a way that at least a portion of the gaseous impurities from said CO2-poor stream, and a portion of the hydrogen from said CO2-poor stream, CO2 are adsorbed onto the aforementioned adsorption material, thus providing a stream rich in H2; - in said second state, the first purge stream contacts the adsorption material such that at least a portion of the adsorbed gaseous impurities and at least a portion of said adsorbed hydrogen are released from said adsorption material and into the first purge stream; thus providing a first recycling stream comprising said first purge stream, hydrogen and said gaseous impurities; and v. recycle the aforementioned first recycling stream to the reformer section as feed for the reforming stage.

[00030] Appropriately, in the aforementioned method, stage SA is initially in the aforementioned first state (A) and, in Petition 870260073078, dated 07 / 22 / 2026, p. 21 / 39 13 / 17 then alternates between the aforementioned first (A) and second (B) states. As above, it is preferred that the temperature of stage SA in the second state (B) be higher than in the aforementioned first state (A).

[00031] All the plant details above are relevant to the method described in this document, mutatis mutandis.

[00032] The present invention is based on the recognition that it is possible to recycle part of the hydrogen produced in the Oscillation Adsorption stage and use it as feed in the reforming stage in order to increase the total hydrogen yield of the plant. The present invention is further based on the recognition that it is feasible to supply the first purge stream from the Oscillation Adsorption stage at a pressure equal to or greater than the reforming reaction pressure and that, therefore, the recycling of the hydrogen-rich stream from the Oscillation Adsorption stage to the reforming stage can be carried out without any need for a compressor.

[00033] In particular, the first purge stream may be a portion of the hydrocarbon feed to be fed to the reforming stage or a portion of the superheated steam to be fed to the reforming stage, and both streams are available at pressures equal to or greater than the reforming stage pressure. Furthermore, the first purge stream may be a hydrogen stream, which may, for example, be a high-pressure stream from a separate process or a portion of the first hydrogen-rich recycle stream from the SA stage, which is available at a pressure equal to or greater than the Petition 870260073078, dated 07 / 22 / 2026, page 22 / 39 14 / 17 pressure of the reforming stage or at a pressure slightly lower than the pressure of the reforming stage, in which case the required compression is minimal.

[00034] Current technology allows for a high H2 yield, exceeding 85% PSA and likely in the order of +95%. Current technology, therefore, offers a more efficient route for hydrogen production. Based on the overall plant configuration, this technology will allow for the construction of more contact reformers, as the increased yield means less gas needs to be processed to produce a given quantity of H2. This also means the technology offers lower natural gas consumption and lower CO2 emissions compared to modern standards.

[00035] A higher H2 yield can be achieved compared to using a Pressure Swing Absorption (PSA) stage. This will allow for the construction of more compact steam reformers, as overproduction will not be a problem. EXAMPLE 1

[00036] Table 1 summarizes an example of the invention. A given quantity of hydrocarbon feed (101) is reformed in the reformer section (200) to produce a synthesis gas stream (201). CO2 is removed from this stream in the CO2 removal stage (300) to produce a CO2-poor stream (304) and a CO2-rich stream (303). The CO2-poor stream (304) is then separated in an SA stage (400) to produce an H2-rich stream (409). The SA is steam purged (405) and 50% of this stream is recycled back to the reformer. Petition 870260073078, dated 07 / 22 / 2026, page 23 / 39 15 / 17 while the second half is condensed to leave an exhaust gas. In addition, steam and some hydrogen are added to the reformer section to facilitate pre-reforming and reforming in this section. Note that the total feed to the reformer is the mixture of hydrocarbon feed (101), steam and hydrogen after being pre-reformed. Hydrocarbon feed (101) Total feed to the reformer Reformer product Synthesis gas for the CO removal stage? Synthesis gas for SA (304) H2-rich stream (409) First recycle stream (408) Exhaust gas T [°C] 40 650 920 40 40 45 410 30 P [barg = 100 kPa g] 29.0 26.0 24.5 23.4 23.4 22.7 29 0.7 Flow [Nm3 / h] 12784 52318 75775 66195 57143 37830 39752 9657 Composition [% mol] Carbon dioxide 0.1 4.3 3.9 13.4 0.0 0.0 0.0 0.0 Nitrogen 1.0 0.4 0.3 0.3 0.4 0.1 0.2 0.9 Methane 96.6 28.6 4.2 4.8 5.6 0.0 4.0 16.6 Ethane 1.8 0.0 0.0 0.0 0.0 0.0 0.0 0.0 Propane 0.3 0.0 0.0 0.0 0.0 0.0 0.0 0.0 n-Butane 0.1 0.0 0.0 0.0 0.0 0.0 0.0 0.0 Isobutane 0.1 0.0 0.0 0.0 0.0 0.0 0.0 0.0 n-Hexane 0.1 0.0 0.0 0.0 0.0 0.0 0.0 0.0 Hydrogen 0.0 12.8 56.2 73.2 84.8 99.9 13.4 55.2 Carbon monoxide 0.0 0.2 14.7 8.0 9.2 0.0 6.6 27.3 Water 0.0 53.7 20.7 0.3 0.0 0.0 75.7 0.0 EXAMPLE 2

[00037] Table 2 summarizes a comparative example where the first recycle 408 from the SA unit is not returned to the reforming section. Similar to Example 1, a given amount of hydrocarbon feed (101) is reformed in the reformer section (200) to produce a synthesis gas stream (201). CO2 is removed from this Petition 870260073078, dated 07 / 22 / 2026, page 24 / 39 16 / 17 stream in the CO2 removal stage (300) to produce a CO2-poor stream (304). This is then separated in an SA stage (400) to produce an H2-rich stream (409). The SA is, in this case, a more typical PSA, where the waste gas is produced directly. In addition, steam and some hydrogen are added to the reformer section to facilitate pre-reforming and reforming in this section. Note that the total feed to the reformer is the mixture of hydrocarbon feed (101), steam and hydrogen after being pre-reformed. Hydrocarbon feed (101) Total feed to the reformer Reformer product Synthesis gas for CO2 removal stage Synthesis gas for SA (304) H2-rich stream (409) Exhaust gas T [°C] 40.0 650.0 920.0 40.0 40.0 45.0 30.0 P [barg = 100 kPa g] 29.0 26.0 24.5 23.4 23.4 22.7 0.7 Flow [Nm3 / h] 12784 44442 65501 54494 46560 32103 14458 Composition [% mol] Carbon dioxide 0.1 1.5 4.2 14.2 0.0 0.0 0.0 Nitrogen 1.0 0.3 0.2 0.2 0.3 0.1 0.6 Methane 96.6 28.0 2.9 3.5 4.1 0.0 13.2 Ethane 1.8 0.0 0.0 0.0 0.0 0.0 0.0 Propane 0.3 0.0 0.0 0.0 0.0 0.0 0.0 n-Butane 0.1 0.0 0.0 0.0 0.0 0.0 0.0 Isobutane 0.1 0.0 0.0 0.0 0.0 0.0 0.0 n-Hexane 0.1 0.0 0.0 0.0 0.0 0.0 0.0 Hydrogen 0.0 5.4 55.1 75.5 88.3 99.9 62.6 Carbon monoxide 0.0 0.0 12.9 6.3 7.3 0.0 23.6 Water 0.0 64.8 24.7 0.3 0.0 0.0 0.0

[00038] By the method of the invention presented in the example 1, it is shown that the size of the H2-rich stream (409) is increased from 32103 Nm3 / h in the base case of example 2 to 39752 Nm3 / h in example 1. Thus, by the method of the invention, the Petition 870260073078, dated 07 / 22 / 2026, page 25 / 39 17 / 17 hydrogen yield from a given amount of hydrocarbon feed (101) is increased by 24%. By increasing the degree of utilization of the purge stream (405) from the 50% used in example 1, the yield can increase even further. Using 70% of the purge stream instead would result in a 29% increase in the yield of the H2-rich stream (409).

[00039] Other references in the figure: - Preheating section 90 - Combustion gas 220 - Hydrodesulfurization (HDS) and sulfur adsorption unit 80 - waste heat exchanger / boiler 209 - displaced synthesis gas stream 201' - displacement section 500

[00040] Although the invention has been described with reference to a number of aspects, examples and embodiments, these aspects, examples and embodiments may be combined by a person skilled in the art, while remaining within the scope of the present invention. Petition 870260073078, dated 07 / 22 / 2026, page 26 / 39

Claims

1 / 6 CLAIMS 1. Plant (100) for hydrogen purification by supplying a H2-rich gas stream (409) from a hydrocarbon feed (101), said plant (100) characterized in that it comprises: - a reformer section (200) arranged to receive said hydrocarbon feed (101) and reforming it in at least one reforming stage conducted at a first pressure to provide a synthesis gas stream (201); - a CO2 removal stage (300), arranged to receive the synthesis gas stream (201) from said reformer section (200) and separate CO2 from the synthesis gas stream (201), so as to provide a CO2-rich stream (303) and a CO2-poor stream (304); - an Oscillation Adsorption (SA) stage (400), said SA stage (400) comprising an adsorption material (401) and a first purge stream (405) with a pressure equal to or greater than the first pressure;and being arranged to receive the CO2-poor stream (304) from the CO2 removal stage (300); - wherein said SA stage (400) comprises a first state (A) and a second state (B), wherein; in said first state (A), the CO2-poor stream (304) is arranged to contact the adsorption material (401) so that; at least a portion of the gaseous impurities (407) of said CO2-poor stream (304), and a portion of the hydrogen from said CO2-poor stream (304) are adsorbed onto said adsorption material (401), thus providing a H2-rich stream (409); in said second state (B), the first purge stream (405) is arranged to contact the adsorption material (401) so that at least a portion of the adsorbed gaseous impurities (407) and at least a portion of said adsorbed hydrogen are released from said adsorption material (401) and into the first purge stream (405);thus providing a first recycling stream (408) comprising said first purge stream (405), hydrogen and said gaseous impurities (407); - said plant (100) being arranged to recycle said first recycling stream (408) to the reformer section (200) as feed for the reforming stage.

2. Plant (100), according to claim 1, characterized in that stage SA (400) is arranged to alternate between said first (A) and second (B) states.

3. Plant (100), according to any of the preceding claims, characterized in that the temperature of stage SA in the second state (B) is higher than in said first state (A).

4. Plant (100), according to any of the preceding claims, characterized in that stage SA (400) has several parallel adsorption reactions in different stages (A, B) at a given time.

5. Plant (100), according to any of the preceding claims, characterized in that stage SA (400) comprises a second purge stream (406) and comprises a third stage (C), wherein the second purge stream (406) is arranged to purge the adsorption material (401) subsequent to purging with the first purge recycling stream (405) so that at least a portion of the gaseous impurities (407) are released from said adsorption material (401); thus providing a second recycling stream that is recycled upstream of the reforming stage of said reformer section (200).

6. Plant (100), according to any of the preceding claims, characterized in that the adsorption material (301) is selected from a zeolite, activated carbon or organic metallic structure, or mixtures thereof.

7. Plant (100), according to any of the preceding claims, characterized in that the first purge stream (405) is a superheated steam stream.

8. Plant (100), according to claim 7, characterized in that the superheated steam stream is arranged to provide at least part of the temperature rise of stage SA (400) from the first state to the second state.

9. Plant (100), according to any of the preceding claims, characterized in that the first purge stream (405) is a fraction of the hydrocarbon feed, in the form of natural gas.

10. Plant (100), according to any of the previous claims, characterized in that the first and / or second purge streams (405, 406) are hydrogen streams.

11. Plant (100), according to any of the preceding claims, characterized in that said reformer section (200) comprises one or more primary reformer units (220) and, optionally, one or more pre-reformer units (221) arranged in the hydrocarbon feed (101) upstream of said reformer unit(s) (220), and wherein said plant (100) is arranged to feed said first recycling stream (408) upstream of one or more pre-reformer units (221).

12. Plant (100), according to any of the preceding claims, characterized in that said one or more primary reformer units (220) are selected from an autothermal reactor (ATR), a steam methane reforming reactor (SMR), a convective reforming reactor and / or a catalytic oxidation type reforming reactor (CATOX).

13. Plant (100), according to any of the preceding claims, characterized in that it further comprises a displacement section (500) disposed in said synthesis gas stream (201) between said reformer section (200) and said CO2 removal stage (300).

14. Method for hydrogen purification by supplying an H2-rich gas stream (405) from a hydrocarbon feed (101), said method characterized by comprising: Petition 870260073078, dated 22 / 07 / 2026, page 30 / 39 5 / 6 i. supplying a plant (100) as defined with any of the preceding claims; ii. feeding the hydrocarbon feed (101) to the reformer section (200) and reforming the same in at least one reforming step conducted at a first pressure to supply a synthesis gas stream (201); iii. feed the synthesis gas stream (201) from said section of the reformer (200) to the CO2 removal stage (300) and separate CO2 from the synthesis gas stream (201), so as to provide a CO2-rich stream (303) and a CO2-poor stream (304); iv.feeding the CO2-poor stream (304) from the CO2 removal stage (300) to the Oscillation Adsorption (SA) stage (400) comprising an adsorption material (401) and a first purge stream (405) with a pressure equal to or greater than the first pressure, wherein said SA stage (400) comprises a first state (A) and a second state (B), wherein - in said first state, the CO2-poor stream (304) contacts the adsorption material (401) so that at least a portion of the gaseous impurities (407) of said CO2-poor stream (304), and a portion of the hydrogen of said CO2-poor stream (304) are adsorbed onto said adsorption material (401), thus providing an H2-rich stream (409); - in the aforementioned second state, the first purge stream (405) contacts the adsorption material (401) in such a way that at least a portion of the adsorbed gaseous impurities (407) and at least a portion of said hydrogen Petition 870260073078, dated 22 / 07 / 2026, page.31 / 39 6 / 6 adsorbed are released from said adsorption material (401) and in the first purge stream (405); thus providing a first recycling stream (408) comprising said first purge stream (405), hydrogen and said gaseous impurities (407); and v. recycle said first recycling stream to the reformer section (200) as feed for the reforming stage.

15. Method according to claim 14, characterized in that stage SA (400) is initially in said first state (A) and then alternates between said first (A) and second (B) states.

16. Method according to claim 14 or 15, characterized in that the temperature of stage SA in the second state (B) is higher than in said first state (A). Petition 870260073078, dated 22 / 07 / 2026, p. 32 / 39

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