Method and system for feeding a hydrogen-containing gas stream into a pipeline

Abstract

The invention relates to a method for feeding a hydrogen-containing gas stream (1) into a pipeline (2). A carbon-containing energy carrier stream (3) is supplied to a syngas reactor assembly (4) in order to obtain a fresh syngas stream (5) comprising hydrogen and carbon dioxide, wherein the fresh syngas stream (5) is supplied to a shift device (6a-c) in order to obtain a shift syngas stream (7), a water-gas shift reaction is carried out in the shift device (6a-c) in order to react at least one part of the carbon monoxide of the fresh syngas stream (5) with vapor of the fresh syngas stream (5) in order to form carbon dioxide and hydrogen, the shift syngas stream (7) is supplied to a compressor assembly (8) in order to increase the pressure and obtain a high-pressure syngas stream (9), the high-pressure syngas stream (9) is supplied to a carbon dioxide scrubbing process (10) in order to scrub at least one part of the carbon dioxide out of the high-pressure syngas stream (9) and obtain the hydrogen-containing gas stream (1), and the hydrogen-containing gas stream (1) is fed into the pipeline (2). The invention likewise relates to a corresponding system for feeding a hydrogen-containing gas stream 1 into a pipeline 2.

Description

[0001] Method and system for feeding a hydrogen-containing gas stream into a pipeline

[0002] The invention relates to a method for feeding a hydrogen-containing gas stream into a pipeline and to a system for feeding a hydrogen-containing gas stream into a pipeline.

[0003] Hydrogen can not only be used as a starting material for the production of energy sources such as ammonia, but is also an energy source in itself, which can not only be burned directly and without CO2 emissions, but can also be used, for example, in fuel cells.

[0004] One difficulty in providing hydrogen in large quantities is that it is often not available in the locations where it is to be used, or can only be obtained under unfavorable conditions. For example, electrolysis requires large quantities of electrical power, which should ideally be generated without CO2 emissions. Since the transmission of large quantities of electrical energy over long distances is also problematic, electrolysis is preferably carried out where emission-free energy is available—for example, near large hydroelectric power plants—rather than where the hydrogen is needed. However, such large hydroelectric power plants are usually not located near industrial centers.

[0005] In addition to electrolysis, larger quantities of hydrogen can also be produced from synthesis gas, which in turn is produced from natural gas. This process is also preferably carried out close to the natural gas source. In order to achieve a CO2 footprint with this approach that is comparable to or even lower than electrolysis, further measures are required, such as separating the CO2 before transport and storing the CO2, which preferably takes place at the natural gas reservoir. For both methods of hydrogen production, the problem arises of being able to transport the produced hydrogen over long distances to where it is needed. A particularly attractive approach to transporting the hydrogen, especially over long distances, is to feed it into a pipeline.

[0006] However, this requires the hydrogen to be brought to a high pressure. This is problematic with high-purity hydrogen due to its low molecular weight and low density. The low molecular weight and low density mean that just to increase the pressure to, say, 100 bar, approximately 10% of the heat content of the hydrogen stream must be consumed for the pressure increase itself. Furthermore, turbo compressors cannot be used for the pressure increase; instead, a larger number of piston compressors are required, which are associated with higher costs due to their number and more complex design.

[0007] Based on the prior art, the object of the invention is therefore to provide a solution in which hydrogen can be obtained from a synthesis gas stream, which in turn was obtained from a carbon-containing energy carrier stream, in such a way that it can be fed into a pipeline without the use of piston compressors.

[0008] With respect to a method for feeding a hydrogen-containing gas stream into a pipeline, this object is achieved by the features of patent claim 1. With respect to a system for feeding a hydrogen-containing gas stream into a pipeline, this object is achieved by the features of patent claim 16.

[0009] The invention is based on the finding that increasing the pressure of the synthesis gas stream with turbocompressors is possible if this pressure increase occurs before the carbon dioxide scrubbing step. Before this step, the synthesis gas stream contains sufficient amounts of other components besides hydrogen, which increases the density and average molecular weight compared to pure hydrogen.

[0010] This not only ensures the use of turbo compressors, but also significantly reduces the energy required for compression, regardless of the compressor design, for physical reasons. For example, compressing methane requires only a fifth of the energy required to compress ultrapure hydrogen. The subsequent carbon dioxide scrubbing process can also be carried out at this increased pressure and involves only a minor pressure loss, so that the gas stream obtained from the carbon dioxide scrubbing process has a sufficiently high pressure for feeding into the pipeline.

[0011] The preferred embodiment of subclaim 9 relates to the possibility of generating the synthesis gas through autothermal reforming. In this variant, the synthesis gas can be generated at a higher pressure than, for example, with a steam reformer. The effort required to compress the synthesis gas to a pressure sufficient for feeding hydrogen into a pipeline is correspondingly lower.

[0012] The preferred embodiments of subclaims 10 to 12 relate to the possibility of providing multiple stages for the water gas shift reaction. By providing such a multi-stage system, and in particular by having the water gas shift reaction take place in a different temperature range in each stage, a very extensive conversion of the CO in the gas stream into CO2 can be achieved, which CO2 can then be removed in the subsequent carbon dioxide scrubbing stage. As a result, the gas stream can be very extensively purified of all carbon oxides.

[0013] Further details, features, embodiments, objects and advantages of the present invention are explained below with reference to the drawings, which merely represent exemplary embodiments. In the drawing,

[0014] Fig. 1 schematically shows the flow diagram of a proposed plant for carrying out the proposed method according to a first embodiment,

[0015] Fig. 2 shows a schematic flow diagram of a proposed plant for carrying out the proposed method according to a second exemplary embodiment, and Fig. 3 shows a schematic flow diagram of a proposed plant for carrying out the proposed method according to a third exemplary embodiment.

[0016] The proposed method, which will initially be described using the exemplary embodiment in Fig. 1, serves to feed a hydrogen-containing gas stream 1 into a pipeline 2, wherein a carbon-containing energy carrier stream 3 is fed to a synthesis gas reactor arrangement 4 for obtaining a fresh synthesis gas stream 5 containing hydrogen and carbon oxides. Unless specifically stated, the respective exemplary embodiment in Fig. 2 and Fig.

[0017] 3 is identical to that of Fig. 1. The respective differences are explicitly stated.

[0018] In principle, the carbon-containing energy carrier stream 3 can be any such energy carrier stream. Preferably, the carbon-containing energy carrier stream 3 is a natural gas stream 3a that comprises natural gas or consists essentially of natural gas. Feeding the hydrogen-containing gas stream 1 into the pipeline 2 means introducing the gas stream 1 into the pipeline 2 for the purpose of transport.

[0019] According to the proposed method, the fresh synthesis gas stream 5 is fed to a shift device 6a-c to obtain a shift synthesis gas stream 7, wherein a water gas shift reaction takes place in the shift device 6a-c to convert at least a portion of the carbon monoxide of the fresh synthesis gas stream 5 with steam from the fresh synthesis gas stream 5 into carbon dioxide and hydrogen. The fresh synthesis gas stream 5 does not have to be the entire synthesis gas obtained from the synthesis gas reactor arrangement 4. Rather, it can be a portion of the synthesis gas obtained from the synthesis gas reactor arrangement 4. Likewise, the fresh synthesis gas stream 5 can undergo further treatment before being fed to the shift device 6a-c.

[0020] Furthermore, according to the proposed method, the shift synthesis gas stream 7 is fed to a compressor arrangement 8 for increasing the pressure and obtaining a high-pressure synthesis gas stream 9. It is preferred that the compressor arrangement 8 comprises or consists of at least one turbocompressor. Alternatively or additionally, the compressor arrangement 8 may comprise or consist of at least one centrifugal, axial, piston, or combined piston and axial compressor.

[0021] Preferably, the high-pressure synthesis gas stream 9 essentially corresponds in composition to the shift synthesis gas stream 7, but has a higher pressure. The shift synthesis gas stream 7 also does not have to be the entire synthesis gas stream obtained from the shift device 6a-c. Likewise, the shift synthesis gas stream 7 can undergo additional treatment before being fed to the compressor arrangement 8.

[0022] According to the proposal, the high-pressure synthesis gas stream 9 is fed to a carbon dioxide scrubber 10 to scrub at least a portion of the carbon dioxide from the high-pressure synthesis gas stream 9 and to obtain the hydrogen-containing gas stream 1. The high-pressure synthesis gas stream 9 does not have to be the entire synthesis gas stream obtained from the compressor arrangement 8. Likewise, the high-pressure synthesis gas stream 9 can undergo additional treatment before being fed to the carbon dioxide scrubber 10.

[0023] Finally, the hydrogen-containing gas stream 1 is fed into pipeline 2.

[0024] The proposed plant serves to feed the hydrogen-containing gas stream 1 into the pipeline 2, wherein the plant comprises the synthesis gas reactor arrangement 4 for obtaining the fresh synthesis gas stream 5 containing hydrogen and carbon oxides from the carbon-containing energy carrier stream 3.

[0025] The proposed plant further comprises the shift device 6a-c, to which the fresh synthesis gas stream 5 is fed to obtain the shift synthesis gas stream 7. In the shift device 6a-c, a water-gas shift reaction takes place to convert at least a portion of the carbon monoxide of the fresh synthesis gas stream 5 with steam from the fresh synthesis gas stream 5 into carbon dioxide and hydrogen. The proposed plant also comprises the compressor arrangement 8 for pressure increase, to which the shift synthesis gas stream 7 is fed to obtain the high-pressure synthesis gas stream 9, and the carbon dioxide scrubber 10, to which the high-pressure synthesis gas stream 9 is fed to obtain the hydrogen-containing gas stream 1. In the carbon dioxide scrubber 10, at least a portion of the carbon dioxide is scrubbed out of the high-pressure synthesis gas stream 9.

[0026] Finally, the proposed plant comprises a pipeline connection 17 to which the hydrogen-containing stream 1 is fed for feeding into the pipeline 2.

[0027] A preferred embodiment of the proposed method and the proposed plant is characterized in that the hydrogen-containing gas stream 1, after being obtained from the carbon dioxide scrubber 10, is fed into the pipeline 2 without any pressure increase. In other words, no pressure increase takes place in the process between the carbon dioxide scrubber 10 and the feed into the pipeline 2. In particular, no pressure increase takes place in the process downstream of the compressor arrangement 8. Preferably, only a drop in pressure takes place in the process between the compressor arrangement 8 and the feed into the pipeline 2. This eliminates the need for an additional compressor stage and, in particular, the need for piston compressors. Because the hydrogen-containing gas stream 1 is obtained from synthesis gas and the carbon dioxide scrubber with methanol, no additional drying is required before feeding into the pipeline 2.

[0028] A further preferred embodiment of the proposed method and the proposed plant is characterized in that the compressor arrangement 8 increases the pressure such that the high-pressure synthesis gas stream 9 has a pressure of at least 80 bar. Preferably, the high-pressure synthesis gas stream 9 has a pressure of at least 100 bar and in particular of at least 120 bar. It is further preferred that a pressure loss of the hydrogen-containing gas stream 1 compared to the high-pressure synthesis gas stream 9 is less than 10 bar and preferably less than 5 bar. At this pressure, the pressure of the hydrogen-containing gas stream 1 is high enough to be fed into the pipeline 2 without further pressure increase. In principle, the hydrogen-containing gas stream 1 can contain any molar proportion of hydrogen as well as other substances such as, in particular, carbon monoxide, carbon dioxide, or methane.According to a preferred embodiment of the proposed process and the proposed plant, the hydrogen-containing gas stream 1 has a molar methane content of less than 2% and in particular less than 1%. Here, the hydrogen-containing gas stream 1 may also have a molar carbon monoxide content of less than 1% and, more particularly, less than 0.5%.

[0029] According to a further preferred embodiment of the proposed process and the proposed plant, it is provided that the hydrogen-containing gas stream 1 has a molar proportion of carbon dioxide of less than 1% and in particular of less than 1 per mille.

[0030] It is preferred that the hydrogen-containing gas stream has a molar nitrogen content of less than 0.5%. It is also preferred that the hydrogen-containing gas stream has a molar argon content of less than 0.2%.

[0031] A preferred embodiment of the proposed process and the proposed plant is characterized in that the hydrogen-containing gas stream 1 has a molar proportion of hydrogen of at least 98% and preferably of at least 99%.

[0032] Such a high molar fraction of hydrogen and / or such a low molar fraction of carbon monoxide, carbon dioxide or methane in the hydrogen-containing gas stream 1 can eliminate the need to increase the purity of the hydrogen-containing gas stream 1, for example by means of a pressure swing adsorption device - also referred to as pressure swing adsorption or PSA.

[0033] Therefore, a further preferred embodiment of the proposed process and the proposed plant is characterized in that the hydrogen-containing gas stream 1 is fed into the pipeline 2 essentially with the composition with which it was obtained from the carbon dioxide scrubber 10. Consequently, no further purification of the hydrogen-containing gas stream 1 takes place in the process between the carbon dioxide scrubber 10 and the feed into the pipeline 2. The degree of hydrogen purity achieved in this way is usually sufficient for feeding into the pipeline 2.

[0034] Likewise, no gas stream with a different composition is added to the hydrogen-containing gas stream 1 during the process between the carbon dioxide scrubber 10 and the feed into the pipeline 2. This essential retention of the composition from the carbon dioxide scrubber 10 corresponds to the first two embodiments of Figs. 1 and 2.

[0035] However, it is also possible for the hydrogen-containing stream 1 to be fed to a high-pressure pressure swing adsorption device 21 between the carbon dioxide scrubber 10 and the feed into the pipeline 2 to increase the purity of the hydrogen. This corresponds to the embodiment of Fig. 3. In this case, the proposed plant preferably comprises the high-pressure pressure swing adsorption device 21.

[0036] Accordingly, in the first embodiment of Fig. 1, the hydrogen-containing gas stream 1 at the far end of the pipeline 2 is used without further treatment for ammonia synthesis 18. Alternatively, the hydrogen-containing gas stream 1 can also be used for the generation of electricity with a low CO2 footprint or for a chemical synthesis that does not require a very high purity of the hydrogen stream.

[0037] In the embodiment of Fig. 2—which otherwise corresponds to the embodiment of Fig. 1—and in the embodiment of Fig. 3, an even higher degree of hydrogen purity is desired at the far end of the pipeline 2. Therefore, in the embodiment of Fig. 2, the hydrogen-containing gas stream 1 is first fed to a pressure swing adsorption system 19 and then to a system 20 in which a chemical synthesis takes place, which requires a high degree of purity of the hydrogen stream. Alternatively, the hydrogen-containing gas stream 1 can also be fed to a power plant that meets particularly stringent requirements for a low CO2 footprint.

[0038] In the embodiment of Fig. 3, however, the high degree of purity is already present in the pipeline 2, which is why the hydrogen-containing gas stream 1 from the pipeline 2 is fed to the plant 20 without further treatment.

[0039] In principle, the fresh synthesis gas stream 5 can be obtained from the energy carrier stream 3 by any process in the synthesis gas reactor arrangement 4. According to a preferred embodiment of the proposed method and the proposed system, the synthesis gas reactor arrangement 4 obtains the fresh synthesis gas stream 5 from the energy carrier stream 3 by autothermal reforming. During autothermal reforming, a particularly catalytic partial oxidation provides the heat required for the endothermic reforming reactions. Furthermore, during autothermal reforming, synthesis gas can be obtained at a higher pressure than, for example, in steam reforming, so that the power required for the compressor arrangement 8 is lower. The corresponding costs are therefore also lower.

[0040] It is further preferred that during autothermal reforming in the synthesis gas reactor arrangement 4, a molar steam-to-carbon ratio of at least 1.5, preferably of at least 1.6, more preferably a molar steam-to-carbon ratio of at least 2, and in particular a molar steam-to-carbon ratio of at least 2.4 exists. The higher the steam-to-carbon ratio, the lower the methane slip and the more effectively carbon monoxide can be converted into carbon dioxide in a subsequent water gas shift reaction. Accordingly, these measures also result in less methane remaining in the hydrogen-containing gas stream 1 in the pipeline 2. In this way, a high hydrogen purity can be achieved even without a high-pressure pressure swing adsorption device.

[0041] The following table shows various process parameters that occur at different molar steam-to-carbon ratios and an autothermal reforming process operated at 65 bar.

[0042] It is evident that with a higher steam-to-carbon ratio, the methane slip decreases. Likewise, the proportion of carbon dioxide and hydrogen compared to carbon monoxide in the synthesis gas increases.

[0043] In principle, the fresh synthesis gas stream 5 can be fed to only a single shift device 6a-c. According to a further preferred embodiment of the proposed method and the proposed plant, in order to further increase the purity of the hydrogen-containing gas stream 1, the fresh synthesis gas stream 5 is fed to a plurality of shift devices 6a-c, preferably arranged at a distance from one another in terms of process technology, and a water-gas shift reaction takes place in each of the shift devices 6a-c to convert at least a portion of the carbon monoxide of the fresh synthesis gas stream 5 with steam from the fresh synthesis gas stream 5 into carbon dioxide and hydrogen. In this way, the proportion of carbon monoxide converted into carbon dioxide can be increased compared to the use of only one shift device. The proposed plant preferably comprises the plurality of shift devices 6a-c.

[0044] A process-technically spaced arrangement of the shift devices 6a-c means that, in process terms, at least one further device, which is not a shift device 6a-c, is arranged between two shift devices 6a-c. In this way, it is possible to bring the fresh synthesis gas stream 5 from one shift device 6a-c to the next to a different, adjusted temperature.

[0045] In principle, essentially identical process parameters and, in particular, temperatures may be present in the plurality of shift devices 6a-c. However, a preferred embodiment of the proposed method and the proposed system is characterized in that the water gas shift reaction in the shift devices 6a-c takes place in a temperature range that decreases in the process direction. In other words, the temperature in a downstream shift device 6a-c is lower than in an upstream shift device 6a-c.

[0046] A further preferred embodiment of the proposed process and the proposed plant is characterized in that the shift devices 6a-c comprise an HT shift device 11 for a high-temperature water-gas shift reaction and an MT shift device 12 for a medium-temperature water-gas shift reaction. It is further preferred that the shift devices 6a-c comprise an LT shift device 13 for a low-temperature water-gas shift reaction. In this case, the MT shift device 12 is located downstream of the HT shift device 11 in terms of process technology.

[0047] The high-temperature water gas shift reaction takes place at a temperature between 300°C and 450°C. The medium-temperature water gas shift reaction takes place at a temperature between 220°C and 270°C. The low-temperature water gas shift reaction takes place at a temperature between 180°C and 250°C. Although the high-temperature water gas shift reaction has a poorer reaction equilibrium for the conversion to CO2, it has a better reaction rate. The high molar steam-to-carbon ratio improves the reaction equilibrium. By cascading the shift devices 6a-c, a rapid degradation of carbon monoxide can be achieved initially, with the subsequent stages successively converting the remaining carbon monoxide. Since the carbon monoxide concentration has already been reduced, a longer reaction time can be accepted.

[0048] In principle, the carbon dioxide can be scrubbed out in the carbon dioxide scrubber 10 using any desired approach. Preferably, the carbon dioxide scrubber 10 is a physical scrub. However, the carbon dioxide scrubber 10 can also be a chemical scrub. According to a preferred embodiment of the proposed method and the proposed system, the carbon dioxide is scrubbed out in the carbon dioxide scrubber 10 using a scrubbing medium comprising methanol.

[0049] According to a further preferred embodiment of the proposed method and the proposed plant, the energy carrier stream 3 is fed to a saturation stage 14 before being fed to the synthesis gas reactor arrangement 4. In this saturation stage 14, preheated condensate is added to the energy carrier stream 3. In this way, the stoichiometry suitable for generating the synthesis gas can be achieved. The proposed plant preferably comprises the saturation stage 14.

[0050] A preferred embodiment of the proposed process and the proposed plant is characterized in that the synthesis gas reactor arrangement 4 comprises a pre-reformer for splitting hydrocarbons with at least two carbon atoms into methane. It is further preferred that the energy carrier stream 3 is fed to a desulfurization stage 15 for desulfurizing the energy carrier stream 3 before being fed to the saturation stage 14. The proposed plant preferably comprises the desulfurization stage 15.

[0051] Preferably, an adiabatic steam reforming over a nickel-based catalyst takes place in the pre-reformer. It is preferred that the recovery of the fresh synthesis gas stream 5 consists of the autothermal reforming and the pre-reforming in the pre-reformer. Accordingly, no conventional steam reforming takes place in the recovery of the fresh synthesis gas stream 5.

[0052] A further preferred embodiment of the proposed method and the proposed plant is characterized in that an oxygen stream 16a from an oxygen recovery arrangement 16 is fed to the synthesis gas reactor arrangement 4 to obtain the fresh synthesis gas stream 5. The proposed plant preferably comprises the oxygen recovery arrangement 16. Here, it is further preferred that the synthesis gas reactor arrangement 4 obtains the fresh synthesis gas stream 5 from the energy carrier stream 3 by autothermal reforming with the oxygen stream 16a. By using oxygen instead of ambient air, the proportion of nitrogen in the fresh synthesis gas stream 5 can be significantly reduced. This makes it easier to achieve a high proportion of hydrogen in the hydrogen-containing gas stream 1.

[0053] Preferred embodiments, features and properties of the proposed method described above correspond to preferred embodiments, features and properties of the proposed system and vice versa.

Claims

Patent claims 1. A method for feeding a hydrogen-containing gas stream (1) into a pipeline (2), wherein a carbon-containing energy carrier stream (3) is fed to a synthesis gas reactor arrangement (4) for obtaining a fresh synthesis gas stream (5) comprising hydrogen and carbon oxides, wherein the fresh synthesis gas stream (5) is fed to a shift device (6a-c) for obtaining a shift synthesis gas stream (7), wherein a water-gas shift reaction takes place in the shift device (6a-c) for converting at least a portion of the carbon monoxide of the fresh synthesis gas stream (5) with steam of the fresh synthesis gas stream (5) into carbon dioxide and hydrogen, wherein the shift synthesis gas stream (7) is fed to a compressor arrangement (8) for increasing the pressure and obtaining a high-pressure synthesis gas stream (9),wherein the high-pressure synthesis gas stream (9) is fed to a carbon dioxide scrubber (10) for scrubbing at least a portion of the carbon dioxide from the high-pressure synthesis gas stream (9) and for obtaining the hydrogen-containing gas stream (1), and wherein the hydrogen-containing gas stream (1) is fed into the pipeline (2).

2. Process according to claim 1, characterized in that the hydrogen-containing gas stream (1) is fed into the pipeline (2) without pressure increase after being obtained from the carbon dioxide scrubber (10).

3. Method according to claim 1 or 2, characterized in that the compressor arrangement (8) increases the pressure such that the high-pressure synthesis gas stream (9) has a pressure of at least 80 bar, preferably of at least 100 bar and in particular of at least 120 bar.

4. Process according to one of claims 1 to 3, characterized in that the hydrogen-containing gas stream (1) has a molar proportion of methane of less than 2% and in particular of less than 1%, preferably that the hydrogen-containing gas stream (1) has a molar proportion of carbon monoxide of less than 1% and more particularly of less than 0.5%.

5. Process according to one of claims 1 to 4, characterized in that the hydrogen-containing gas stream (1) has a molar proportion of carbon dioxide of less than 1% and in particular of less than 1 per mille.

6. Process according to one of claims 1 to 5, characterized in that the hydrogen-containing gas stream (1) has a molar proportion of hydrogen of at least 98% and preferably of at least 99%.

7. Process according to one of claims 1 to 6, characterized in that the hydrogen-containing gas stream (1) is fed into the pipeline (2) essentially with the composition with which it was obtained from the carbon dioxide scrubbing (10).

8. The method according to any one of claims 1 to 6, characterized in that the hydrogen-containing gas stream (1) is fed, between the carbon dioxide scrubber (10) and the feed into the pipeline (2), to a high-pressure pressure swing adsorption device (21) to increase the purity of hydrogen 9. The method according to any one of claims 1 to 8, characterized in that the synthesis gas reactor arrangement (4) obtains the fresh synthesis gas stream (5) from the energy carrier stream (3) by autothermal reforming.

10. The method according to one of claims 1 to 9, characterized in that the fresh synthesis gas stream (5) is fed to a plurality of shift devices (6a-c), preferably arranged at a distance from one another in terms of process technology, and in that a water gas shift reaction for converting at least part of the carbon monoxide of the fresh synthesis gas stream (5) with steam of the fresh synthesis gas stream (5) into carbon dioxide and hydrogen takes place in each of the shift devices (6a-c).

11. Experience according to claim 10, characterized in that in the shift devices (6a-c) the water gas shift reaction takes place in a temperature range decreasing in the process direction.

12. Experience according to claim 11, characterized in that the shift devices (6a-c) comprise an HT shift device (11) for a high-temperature water-gas shift reaction and an MT shift device (12) for a medium-temperature water-gas shift reaction, preferably that the shift devices (6a-c) comprise an NT shift device (13) for a low-temperature water-gas shift reaction.

13. The method according to any one of claims 1 to 12, characterized in that in the carbon dioxide scrubbing (30) the carbon dioxide is scrubbed out by a scrubbing medium comprising methanol.

14. The method according to any one of claims 1 to 13, characterized in that the energy carrier stream (3) is fed to a saturation stage (11) before being fed to the synthesis gas reactor arrangement (4), in which saturation stage (11) preheated condensate (12) which has accrued in the plant (2) is fed to the energy carrier stream (3) 15. The method according to any one of claims 1 to 14, characterized in that the synthesis gas reactor arrangement (4) has a pre-reformer (13) for splitting hydrocarbons having at least two carbon atoms into methane, preferably that the energy carrier stream (3) is fed to a desulfurization stage (13) for desulfurizing the energy carrier stream (3) before being fed to the saturation stage (11).

16. Plant for feeding a hydrogen-containing gas stream (1) into a pipeline (2), which plant has a synthesis gas reactor arrangement (4) for obtaining a fresh synthesis gas stream (5) with hydrogen and carbon oxides from a carbon-containing energy carrier stream (3), a shift device (6a-c) to which the fresh synthesis gas stream (5) is fed in order to obtain a shift synthesis gas stream (7), wherein in the shift device (6a-c) a water gas shift reaction for converting at least part of the carbon monoxide of the fresh synthesis gas stream (5) with steam of the fresh synthesis gas stream (5) in Carbon dioxide and hydrogen takes place, has a compressor arrangement (8) for increasing the pressure, to which the shift synthesis gas stream (7) is fed in order to obtain a high-pressure synthesis gas stream (9), has a carbon dioxide scrubber (10) to which the high-pressure synthesis gas stream (9) is fed in order to obtain the hydrogen-containing gas stream (1), wherein in the carbon dioxide scrubber (10) at least part of the carbon dioxide is scrubbed out of the high-pressure synthesis gas stream (9) and has a pipeline connection (17) to which the hydrogen-containing stream (1) is fed for feeding into the pipeline (2).

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