Method and system for processing syngas

Abstract

Disclosed herein is a method for processing syngas comprising receiving syngas generated by a biomass reactor from pyrolysing biomass, reacting at least a portion of the syngas with a catalyst to substantially remove oxygen from the syngas, and reacting at least a portion of the syngas in a water-gas shift reactor for substantially converting carbon monoxide in the syngas into carbon dioxide and hydrogen.

Description

[0001] METHOD AND SYSTEM FOR PROCESSING SYNGAS TECHNICAL FIELD

[0002] This invention relates generally to a method and system for processing syngas. Specifically, this invention relates generally to a method and system for processing syngas generated from pyrolyzing biomass.

[0003] Background

[0004] The demand for sustainable and renewable energy sources has led to the increased use of biomass as a feedstock for energy generation. Pyrolysis, a process involving the thermal decomposition of organic materials at high temperatures in the absence of oxygen, has emerged as an effective method for converting biomass into useful products, including syngas (synthesis gas). Syngas, primarily composed of hydrogen (H₂), carbon monoxide (CO), carbon dioxide (CO₂), and small amounts of methane (CH₄), can serve as a valuable intermediate in various chemical processes and as a fuel source for power generation.

[0005] Despite the potential benefits of syngas derived from biomass, its utilization is often hindered by impurities, particularly sulfur-containing compounds and oxygen. These contaminants, if not properly removed, can lead to significant operational problems in downstream processes, such as catalytic conversion, fuel cell applications, and energy production systems. Current methods to clean syngas of these impurities are often energy-intensive and insufficient, failing to meet the high purity requirements for many industrial processes. As a result, there is a pressing need for an improved method of syngas purification that addresses these challenges, enhancing its usability across a range of applications while minimizing costs, equipment damage, and environmental impact. There is therefore a need for a practical and energy-efficient solution to address the foregoing issues.

[0006] Summary

[0007] In accordance with a first aspect of the invention, there is disclosed a method for processing syngas comprising receiving syngas generated by a biomass reactor from pyrolysing biomass, reacting at least a portion of the syngas with a catalyst to substantially remove oxygen from the syngas, and reacting at least a portion of the syngas in a water-gas shift reactor for substantially converting carbon monoxide in the syngas into carbon dioxide and hydrogen.

[0008] In accordance with a second aspect of the invention, there is disclosed a system for processing syngas comprising a biomass reactor for generating syngas from pyrolysing biomass, an oxygen-removal reactor for reacting at least a portion of syngas received from a pyrolysis reactor with a catalyst to substantially remove oxygen from the syngas, and a water-gas shift reactor converting carbon monoxide in the syngas into carbon dioxide and hydrogen.

[0009] Brief Description of the Drawings

[0010] FIG. 1 shows an exemplary process flow diagram of a method for processing syngas in accordance with one aspect of the invention;

[0011] FIG. 2 shows an exemplary system flow diagram of a system for processing syngas in accordance with one aspect of the invention and utilizing the method for processing syngas of FIG. 1;

[0012] FIG. 3 shows an exemplary process flow' diagram of a method for processing syngas in accordance with one aspect of the invention where hydrogen is separated from the processed syngas;

[0013] FIG. 4 shows an exemplary system flow diagram of a system for processing syngas in accordance with another aspect of the invention and utilizing the method for processing syngas of FIG. 3;

[0014] FIG. 5 shows an exemplary system flow diagram of a first embodiment of a system for processing syngas in accordance utilizing the method for processing syngas of FIG. 3; FIG. 6 shows an exemplary system flow diagram of a second embodiment of a system for processing syngas in accordance utilizing the method for processing syngas of FIG. 3;

[0015] FIG. 7 shows an exemplary system flow diagram of a third embodiment of a system for processing syngas in accordance utilizing the method for processing syngas of FIG. 3;

[0016] FIG. 8 shows an exemplary process flow diagram of a method for processing syngas in accordance with one aspect of the invention where green ammonia is generated from the processed syngas;

[0017] FIG. 9 shows an exemplary system flow diagram of a system for processing syngas in accordance with another aspect of the invention and utilizing the method for processing syngas of FIG. 8;

[0018] FIG. 10 shows an exemplary system flow diagram of a fourth embodiment of a system for processing syngas in accordance utilizing the method for processing syngas of FIG. 8;

[0019] FIG. 11 shows an exemplary process flow diagram of a method for processing syngas in accordance with one aspect of the invention where one of methane and methanol is generated from the processed syngas;

[0020] FIG. 12 shows an exemplary system flow diagram of a system for processing syngas in accordance with another aspect of the invention and utilizing the method for processing syngas of FIG. 11;

[0021] FIG. 13 shows an exemplary system flow diagram of a fifth embodiment of a system for processing syngas in accordance utilizing the method for processing syngas of FIG. 8; and

[0022] FIG. 14 shows an exemplary system flow diagram of a sixth embodiment of a system for processing syngas in accordance utilizing the method for processing syngas of FIG. 8. Detailed Description

[0023] An exemplary embodiment of the present invention, a method for processing syngas 100 (“syngas method 100"), implementable with a system for processing syngas 20 (“syngas system 20”), is described hereinafter with reference to FIG. 1 to FIG. 14. In the syngas system 20. biomass 22, for example cellulosic material, is heated in a biomass reactor 24 to thermally degenerate the biomass 22 by pyrolysis in a step 110. The biomass 22 releases syngas 26 when undergoing pyrolysis.

[0024] Preferably, the biomass 22 comprises at least one of woodchips, wood pellets, biomass and biowaste. An example of the at least one of woodchips and wood pellets is woody biomass. Examples of biowaste includes food waste, plant fibre, rice husks, agricultural biomass and the like cellulose-containing and hemicellulose-containing materials and articles.

[0025] Within the biomass reactor 24 and prior to being discharged therefrom, at least a portion of the generated syngas 26 may be filtered of impurities such as tar and soot and may be reformed through reaction with catalytic material disposed within the biomass reactors 24. Upon being discharged from the biomass reactor 24, the syngas 26 comprises at least one of hydrogen, methane, carbon monoxide, and carbon dioxide.

[0026] Referring to FIGS 1 and 2, the syngas system 20 can comprise the biomass reactor 24. Alternatively, the biomass reactor 24 does not form part of the syngas system 20 with the syngas system 20 be provided to process the syngas 26 generated by the biomass reactor or by, additionally or alternatively, any other reactors or upstream process where syngas 26 may be generated. In an exemplary implementation, biomass 22 is heated in the biomass reactor 24 to a high temperature with by-products of, for example, biochar, bio-oil and wood vinegar before being subsequently cooled.

[0027] Any number of processes and unit operations may be employed to cool the syngas 26 within this control volume including use of a chiller or a chiller compressor with the objective being to reduce the temperature of the syngas 26 prior to processing the syngas 26 to remove impurities therefrom.

[0028] Once the syngas 26 has been received from the biomass reactor 24 or any upstream process in a step 112, the syngas 26 has to be purified by removing impurities such as oxygen and sulfur. At this point prior to the processing of the syngas 26, the syngas 26 has an exemplary composition comprising a hydrogen concentration ranging of 29.69 volume percent on a dry basis, a carbon monoxide concentration of 27.79 volume percent on a dry basis, a carbon dioxide concentration ranging of 6.38 volume percent on a dry basis, and a methane concentration of 6.81 volume percent on a dry basis.

[0029] The syngas system 20 further comprises an oxygen -removal reactor 30 for substantially removing oxygen therefrom. Substantial oxygen removal is performed by reacting at least a portion of the syngas 26 with a catalyst within the oxygen-removal reactor 30 in a step 114. The syngas system 20 further comprises a water-gas shift reactor 32 converting carbon monoxide in the syngas 26 into carbon dioxide 34 and hydrogen 36 in a step 116.

[0030] The syngas system 20 further comprises a root blower 40 for increasing pressure of the syngas 26 generated from the biomass reactor 24 to within a range of 0.1psi and 25psi, or preferably to substantially 20psi, in a step 120, prior to provision of the syngas 26 for reaction with the catalyst in the oxygen-removal reactor 30.

[0031] The syngas system 20 can also comprise at least one buffer tank 42 for receiving and buffering the syngas 26 pressurized by the root blower 40, in a step 122, prior to provision thereof for reaction with the catalyst in the oxygen-removal reactor 30.

[0032] The syngas system 20 further comprises a piston compressor 44 for increasing the pressure of the syngas 26 to a range of between 1.0bars and 25 bars, or preferably to substantially 25bars, in a step 124, subsequent to substantially removing oxygen therefrom. Sulfur has to be removed from the syngas 26 following oxygen removal from the syngas 26. Hence, in a step 126, the syngas 26 passages through a sulfur trap 46 to substantially remove sulfur and sulfide therefrom. Preferably, the sulfur trap 46 utilises or comprises a sorbent for substantially trapping sulfur and sulfide from the syngas 26. In some implementations, the piston compressor 44 may be configured after the sulfur trap 46 with the step 126 of removing the sulfur or sulfide from the syngas 26 occurring prior to the step 124 of increasing the pressure of the syngas 26 by the piston compressor 44.

[0033] Once the syngas 26 has been processed to this point, the syngas 26 has an exemplary composition comprising a hydrogen concentration ranging of 95.09 volume percent on a dry basis, a carbon monoxide concentration of 0 volume percent, a carbon dioxide concentration ranging of 2.08 volume percent on a dry basis, and a methane concentration of 0 volume percent.

[0034] Hydrogen

[0035] Once the syngas 26 has been processed and depending on downstream process and use requirements, hydrogen 36 may be separated from the syngas 26. Hence, if hydrogen 36 needs to be separated from the syngas 26, the syngas system 26 can further comprise a pressure swing adsorption separator 50 for separating hydrogen 36 from the syngas 26 in a step 130 and as shown in FIGS. 3 and 4. The syngas 26 is then discharged to a a downstream process, for example to a gas generator, while the separated hydrogen 36 is provided to one of a buffer, a storage and a downstream process. Prior to being discharged to the one of a buffer, a storage and a downstream process, the pressure of the hydrogen 36 may be increased, in a step 132 and by a load diaphragm compressor 52, to a range of betw'een 15 bars and 200 bars, or preferably to substantially 200 bars, to obtain pressurized hydrogen 36 therefrom.

[0036] In a first exemplary embodiment of the syngas system 20 with hydrogen separation as shown in FIG 5, four pairs of the biomass reactor 24, making a total of eight of the biomass reactor 24, are used for generating syngas 26 to be fed to four of the root blower 40. Each pair of biomass reactor 24 forms a module for generating syngas 26 at 300 Nm3 / hr at 0 psi to be fed to a corresponding one of the four root blowers 40. Each of the root blowers 40 increases the pressure of the syngas 26 to 10 psi at 20 °C before feeding the syngas 26 to the buffer tank 42. The separate flow pathways of the syngas 26 through the four root blowers 40 are merged at the buffer tank 42. The buffer tank 42 normalises the pressure and nominal flow rate of the syngas 26 received from the four root blowers 40 before providing the syngas 26 to the oxygen-removal reactor 30 for substantially removing oxygen therefrom, followed by the piston compressor 44 for increasing the pressure of the syngas 26 to 14 bar and then to the sulfur trap 46 for substantial removal of sulfur from the syngas 26. The syngas 26 from the sulfur trap 46 the undergoes water gas shift in the water gas shift reactor 32 for converting the carbon monoxide in the syngas 26 into carbon dioxide 34 and hydrogen 36. The hydrogen 36 is then separated from the syngas 26 in the pressure swing adsorption separator 50 before being pressurized from 12 bar to 350 bar by the load diaphragm compressor 52. In the first exemplary embodiment, there is only a single flow pathway from the buffer tank 42 to the water gas shift reactor 32 and eventually through the pressure swing adsorption separator and the load diaphragm compressor 52.

[0037] In a second exemplary embodiment of the syngas system 20 with hydrogen separation as shown in FIG 6, four pairs of the biomass reactor 24, making a total of eight of the biomass reactor 24, are used for generating syngas 26 to be fed to four of the root blower 40. Similar to the first exemplary embodiment of the syngas system 20, each pair of biomass reactor 24 forms a module for generating syngas 26 at 300 Nm3 / hr at 0 psi to be fed to a corresponding one of the four root blowers 40. Each of the root blowers 40 increases the pressure of the syngas 26 to 10 psi at 20 °C but are not fed to the buffer tank 42 used in the first exemplary embodiment. Instead, two of the oxygen-removal reactor 30 are provided with each pair of root blowers 40 providing the pressurized syngas 26 to a corresponding one of the two oxygen-removal reactor 30, effectively merging four flow pathways from the root blowers 40 into two flow pathways from the oxygen-removal reactor 30. Each of the oxygen-removal reactor 30 substantially removes oxygen from the syngas, followed by the piston compressor 44, or low-pressure compressor, for increasing the pressure of the syngas 26 to 14 bar. Each of the oxygen-removal reactors 30 has a corresponding piston compressor 44, or low-pressure compressor. The substantially oxygen removed syngas 26 are then provided to the sulfur trap 46 for substantial removal of sulfur from the syngas 26. The two flow pathways from the piston compressor 44, or low-pressure compressor, are merged into a single flow pathway at the sulfur trap 46 before undergoing water gas shift in the water gas shift reactor 32 for converting the carbon monoxide in the syngas 26 into carbon dioxide 34 and hydrogen 36. The hydrogen 36 is then separated from the syngas 26 in the pressure swing adsorption separator 50 before being pressurized from 12 bar to 350 bar by the load diaphragm compressor 52. In the second exemplary embodiment, there is only a single flow pathway from the sulfur trap 46 to the water gas shift reactor 32 and eventually through the pressure swing adsorption separator and the load diaphragm compressor 52.

[0038] In a third exemplary embodiment of the syngas system 20 with hydrogen separation as shown in FIG 7, four pairs of the biomass reactor 24, making a total of eight of the biomass reactor 24, are used for generating syngas 26 to be fed to four of the root blower 40. Similar to the first exemplary embodiment of the syngas system 20, each pair of biomass reactor 24 forms a module for generating syngas 26 at 300 Nm3 / hr at 0 psi to be fed to a corresponding one of the four root blowers 40. Each of the root blowers 40 increases the pressure of the syngas 26 to 10 psi at 20 °C but are not fed to the buffer tank 42 used in the first exemplary embodiment. Instead, two of the oxygen-removal reactor 30 are provided with each pair of root blowers 40 providing the pressurized syngas 26 to a corresponding one of the two oxygen-removal reactor 30, effectively merging four flow pathways from the root blowers 40 into two flow pathways from the oxygen-removal reactor 30. Each of the oxygen -removal reactor 30 substantially removes oxygen from the syngas, followed by the piston compressor 44, or low-pressure compressor, for increasing the pressure of the syngas 26 to 14 bar. Each of the oxygen-removal reactors 30 has a corresponding piston compressor 44, or low-pressure compressor. The substantially oxygen removed syngas 26 are then provided to the sulfur trap 46 for substantial removal of sulfur from the syngas 26. The syngas 26 is then fed to a corresponding one of two sulfur traps 46 before undergoing water gas shift in a corresponding one of the water gas shift reactor 32 for converting the carbon monoxide in the syngas 26 into carbon dioxide 34 and hydrogen 36. The hydrogen 36 is then separated from the syngas 26 in a corresponding one of two pressure swing adsorption separators 50 before being fed into one of the buffer tank 42. The two flow pathways in the third embodiment are maintained from the oxygen-removal reactor 30 to the pressure swing adsorption separators 50 before being merged into a single flow pathway at the buffer tank 42. The hydrogen 36 from the buffer tank 42 is then being pressurized from 12 bar to 200 bar at 40 °C by the load diaphragm compressor 52.

[0039] Besides hydrogen 36, ammonia 60 may also be produced from the initially processed syngas 26. To generate ammonia 60, the pressure of the syngas 26 is first increased to substantially 250 bars by a boost compressor 62 in a step 140 while the temperature of the syngas 26 is increased to substantially 450° C by a heater 64 in a step 142, with reference to FIGS. 8 and 9. Next, the syngas 26 is reacted with a catalyst in a nitrogen reactor 66 in a step 144 one of subsequent and during the temperature and pressure increase to obtain ammonia therefrom. Additional nitrogen is introducible to the syngas 26 during reaction thereof with the catalyst in the nitrogen reactor 66 to obtain the ammonia.

[0040] In a fourth exemplary embodiment of the syngas system 20 for generating ammonia 60, and specifically green ammonia 60, as shown in FIG 10, four pairs of the biomass reactor 24, making a total of eight of the biomass reactor 24, are used for generating syngas 26 to be fed to four of the root blower 40. Each pair of biomass reactor 24 forms a module for generating syngas 26 at 300 Nm3 / hr at 0 psi to be fed to a corresponding one of the four root blowers 40. Each of the root blowers 40 increases the pressure of the syngas 26 to 10 psi at 20 °C before feeding the syngas 26 to the buffer tank 42. The separate flow pathways of the syngas 26 through the four root blowers 40 are merged at the buffer tank 42. The buffer tank 42 normalises the pressure and nominal flow rate of the syngas 26 received from the four root blowers 40 before providing the syngas 26 to the oxygen-removal reactor 30 for substantially removing oxygen therefrom, followed by the piston compressor 44 for increasing the pressure of the syngas 26 to 14 bar and then to the sulfur trap 46 for substantial removal of sulfur from the syngas 26. The syngas 26 from the sulfur trap 46 the undergoes water gas shift in the w'ater gas shift reactor 32 for converting the carbon monoxide in the syngas 26 into carbon dioxide 34 and hydrogen 36. The pressure of the syngas 26 is then increased to substantially 250 bars by the boost compressor 62 while the temperature of the syngas 26 is increased to substantially 450° C by the heater 64. The syngas 26 is then reacted with a catalyst in the nitrogen reactor 66 to obtain ammonia therefrom. Additional nitrogen is introducible to the syngas 26 during reaction thereof with the catalyst in the nitrogen reactor 66 to obtain the ammonia. In the fourth exemplary embodiment, there is only a single flow pathway from the buffer tank 42 to the water gas shift reactor 32 and eventually through the nitrogen reactor 66.

[0041] If methane 70 or methanol 72 is required instead of ammonia 60, the hydrogen 36 in the syngas 26 is reacted with the carbon dioxide 34 in the syngas 26 in the presence of a catalyst in a carbon dioxide reactor 74 or syngas reactor 76 in a step 150 to obtain one of methanol 72 and methane 70 therefrom, with reference to FIGS. 11 and 12. Additional carbon dioxide 34 is introducible to the syngas 26 during reaction with the catalyst thereof in the carbon dioxide reactor 74 to obtain the one of methanol 72 and methane 70. The syngas reactor 76 is used when the syngas 26 does not undergo the water-gas shift by the water gas shift reactor 32.

[0042] Specifically, methane 70 can be generated using carbon dioxide (CO2) via a process known as methanation, during which hydrogen and CO2 react with one another. Methanation is the conversion of carbon monoxide and carbon dioxide to methane (CH4) through hydrogenation. As the methanation reactions are classified as exothermic, heat generation needs to be safely managed.

[0043] Direct hydrogenation of CO2 with hydrogen over a heterogeneous catalyst through a one-step process can converts CO2 directly to methanol or the like liquid fuels. Liquid methanol is formed from CO2 with the aid of a unique catalyst material consisting of sulfur and molybdenum. Several alternatives for C02 reduction to methanol involving homogeneous, enzymatic catalysis, photocatalysis, and electrocatalysis may also be utilized to address the harsh operating condition issues, for example high temperatures, of methanol synthesis from CO2 over heterogeneous catalysts.

[0044] FIG. 13 shows a fifth embodiment of the syngas system 20 for generating methanol 72, specifically green methanol 72. The configuration of the syngas system 20 in the fifth exemplary embodiment is the same as that of the fourth embodiment with the exception that the nitrogen reactor 66 is replaced with the carbon dioxide reactor 74.

[0045] FIG. 14 shows a sixth embodiment of the syngas system 20 for generating methanol 72, specifically green methanol 72. The configuration of the syngas system 20 in the sixth exemplary embodiment is the same as that of the fifth embodiment with the exception that the carbon dioxide reactor 74 is replaced with the syngas reactor 76 and that the water gas shift reactor 32 is absent in the sixth embodiment.

[0046] The temperatures and pressures prescribed in the syngas method 100 and the various embodiments may vary during operations and are subject to changes based on operating and system configuration requirements. Flowrates of the syngas 26 through the biomass system 20 will also vary and is subjected to, among other factors, the density of the biomass 22. To adapt to the amount of biomass 22 that can be processed, for example, within a day, the syngas system 20 and the various embodiments thereof is scalable. For example, the number of biomass reactors 24 may be scaled or increased to meet the processing demands of the biomass which in turn requires elements of the biomass system 20 to be scaled, increased or multiplied to match up or harmonized with output flowrate of the syngas 26 from the biomass reactors 24.

[0047] Aspects of particular embodiments of the present disclosure address at least one aspect, problem, limitation, and / or disadvantage associated with existing syngas processing approaches. While features, aspects, and / or advantages associated with certain embodiments have been described in the disclosure, other embodiments may also exhibit such features, aspects, and / or advantages, and not all embodiments need necessarily exhibit such features, aspects, and / or advantages to fall within the scope of the disclosure. It will be appreciated by a person of ordinary skill in the art that several of the above-disclosed structures, components, or alternatives thereof, can be desirably combined into alternative structures, components, and / or applications. In addition, various modifications, alterations, and / or improvements may be made to various embodiments that are disclosed by a person of ordinary skill in the art within the scope of the present disclosure, which is limited only by the following claims.

Claims

Claims1. A method for processing syngas comprising:receiving syngas generated by a biomass reactor from pyrolysing biomass; reacting at least a portion of the syngas with a catalyst to substantially remove oxygen from the syngas; andreacting at least a portion of the syngas in a water-gas shift reactor for substantially converting carbon monoxide in the syngas into carbon dioxide and hydrogen.

2. The method as in claim 1, further comprising:increasing pressure of the syngas generated from the biomass reactor to within a range of 0.1psi and 25psi by a root blower prior to provision of the syngas for reaction with the catalyst.

3. The method as in claim 2, further comprising:receiving and buffering the syngas being pressurized by the root blower prior to provision thereof for reaction with the catalyst.

4. The method as in claim 1, further comprising:increasing the pressure of the syngas to a range of between 1.0bars and 25 bars by a compressor subsequent to substantially removing oxygen therefrom.

5. The method as in claim 1, further comprising:passaging the syngas through a sulfur trap to substantially remove sulfur and sulfide therefrom,wherein the sulfur trap uses a sorbent for substantially trapping sulfur and sulfide from the syngas.

6. The method as in claim 1, further comprising:separating hydrogen from the syngas for discharge to one of a buffer, a storage and a downstream process.

7. The method as in claim 6, further comprising:increasing pressure of the hydrogen separated from the syngas to a range of between 15bars and 200 bars by a compressor to obtain pressurized hydrogen.

8. The method as in claim 1, further comprising:increasing temperature and pressure of the syngas to respectively substantially 450° C and 250 bars; andreacting the syngas with a catalyst one of subsequent and during the temperature and pressure increase to obtain ammonia therefrom,wherein additional nitrogen is introducible to the syngas during reaction thereof with the catalyst to obtain the ammonia.

9. The method as in claim 1, further comprising:reacting the syngas with a catalyst to obtain one of methanol and methane therefrom,wherein additional carbon dioxide is introducible to the syngas during reaction thereof with the catalyst to obtain the one of methanol and methane.

10. A system for processing syngas comprising:a biomass reactor for generating syngas from pyrolysing biomass; an oxygen-removal reactor for reacting at least a portion of syngas received from a pyrolysis reactor with a catalyst to substantially remove oxygen from the syngas; anda water-gas shift reactor converting carbon monoxide in the syngas into carbon dioxide and hydrogen.

11. The system as in claim 10, further comprising:a root blower for increasing pressure of the syngas generated from the biomass reactor to within a range of 0.1psi and 25psi prior to provision of the syngas for reaction with the catalyst in the oxygen-removal reactor.

12. The system as in claim 10, further comprising:at least one buffer tank for receiving and buffering the syngas being pressurized by the root blower prior to provision thereof for reaction with the catalyst.

13. The system as in claim 10, further comprising:a piston compressor for increasing the pressure of the syngas to a range of between 1.0bars and 25 bars subsequent to substantially removing oxygen therefrom14. The system as in claim 10, further comprising:a sulfur trap for substantially remove sulfur and sulfide from syngas passaging therethrough,wherein the sulfur trap uses a sorbent for substantially trapping sulfur and sulfide from the syngas.

15. The system as in claim 10, further comprising:a pressure swing adsorption separator for separating hydrogen from the syngas for discharge to one of a buffer, a storage and a downstream process.

16. The system as in claim 15, further comprising:a load diaphragm compressor for increasing pressure of the hydrogen separated from the syngas to a range of between 15 bars and 200 bars to obtain pressurized hydrogen.

17. The system as in claim 10, further comprising:a boost compressor for increasing pressure of the syngas to substantially 250 bars:a heater for increasing temperature of the syngas to substantially 450° C; and a nitrogen reactor for reacting the syngas with a catalyst one of subsequent and during the temperature and pressure increase to obtain ammonia therefrom, wherein additional nitrogen is introducible to the syngas during reaction thereof with the catalyst to obtain the ammonia.

18. The system as in claim 10, further comprising;a carbon dioxide reactor for reacting the syngas with a catalyst to obtain one of methanol and methane therefrom,wherein additional carbon dioxide is introducible to the syngas during reaction thereof with the catalyst to obtain the one of methanol and methane.

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