Process for producing liquid hydrocarbons

Abstract

The Fischer-Tropsch (FT) process with a hybrid membrane / PSA configuration provides high component recovery rates from FT off-gas with minimal power consumption. Syngas from the syngas generation zone is reacted within the FT reaction zone to form a liquid stream and an off-gas stream. The off-gas from the FT reaction zone containing hydrogen, carbon monoxide, and methane reactants is recycled to the syngas generation zone. The purge stream from the recycle loop is sent to a membrane separation unit where it is separated into a permeate stream and a residue stream. The residue stream is separated within a pressure swing adsorption (PSA) unit into a fuel gas stream and a second stream. The second stream can be compressed and recycled to the syngas generation zone.

Description

[Technical Field]

[0001] (Statement of priority) This application claims priority to U.S. Provisional Patent Application No. 63 / 370,387, filed August 4, 2022, which is incorporated herein by reference in its entirety. [Background technology]

[0002] The Fischer-Tropsch (FT) process can be used to produce sustainable aviation fuel (SAF) and other liquid hydrocarbon fuels. The FT process converts synthesis gas into liquid hydrocarbons, which can be upgraded to fuels such as jet fuel in a fuel refinery zone. The off-gas from the FT reaction zone contains valuable hydrogen, carbon monoxide, and methane reactants and is recycled to the synthesis gas production zone within the process. However, the FT off-gas also contains inert gases such as nitrogen and argon. These inert gases accumulate within the process and must be purged from the system. The purge stream also contains hydrogen and carbon-containing reactants (carbon monoxide and methane), resulting in the loss of valuable reactants to the fuel and carbon emissions to the atmosphere.

[0003] Therefore, there is a need for a process to efficiently and selectively purge inert components from the FT process without excessive loss of hydrogen and carbon-containing reactants to the fuel gas and without increasing carbon emissions from the process. [Brief explanation of the drawings]

[0004] [Figure 1] 1 is an illustration of one embodiment of the process of the present invention. DETAILED DESCRIPTION OF THE INVENTION

[0005] The present invention relates to a Fischer-Tropsch (FT) process for producing sustainable aviation fuel (SAF) or other hydrocarbon liquid fuels from syngas. The process includes a syngas production zone where syngas is produced. The syngas is reacted in the FT reaction zone, which contains an FT reactor. A liquid stream from the FT reaction zone can be sent to a fuel refinery zone for further processing into various fuel products, such as jet fuel. The off-gas from the FT reaction zone contains valuable hydrogen (molecular hydrogen), carbon monoxide, and methane reactants and is recycled to the syngas production zone within the process. A purge stream is removed from the recycle loop to prevent the accumulation of inert gases such as nitrogen and / or argon. An efficient recovery system for the purge stream has been developed to recover hydrogen, methane, and carbon monoxide while selectively rejecting nitrogen into the fuel gas stream.

[0006] A hybrid membrane / pressure swing adsorption (PSA) configuration provides high component recoveries with minimal power consumption. A unique PSA design was developed to selectively recover both methane and carbon monoxide over nitrogen from the membrane retentate gas. Adsorbents include, but are not limited to, activated carbon and sodium Y zeolite. Other adsorbents may include activated alumina, silica gel, 5A zeolite, and 13X zeolite. For example, a layer of activated carbon (20-80% by volume) at the feed end of the bed, followed by sodium Y zeolite (20-80% by volume) at the product end of the bed, was found to provide high methane and carbon monoxide recoveries relative to nitrogen. This scheme retains the high H2 recovery benefits of membrane separation while also providing high methane and carbon monoxide recoveries within the PSA unit. Adsorbent splitting and PSA cycle parameters can be optimized for selective methane and carbon monoxide recovery over nitrogen.

[0007] Syngas is produced in a syngas production zone from a feedstream comprising a hydrocarbon or carbonaceous feedstock, suitable feedstreams including, but not limited to, natural gas, liquefied petroleum gas, naphtha, coal, biomass, and the like, or combinations thereof.

[0008] The syngas production zone includes a syngas reactor, including, but not limited to, a steam reforming unit with an optional gas-heated reformer, an autothermal reforming unit with an optional gas-heated reformer, or a gasification unit, or a partial oxidation (POX) unit, a dry reforming unit, or combinations thereof.

[0009] The composition of syngas can vary depending on the process used to produce it. For example, a typical syngas composition (dry basis) from a biomass gasification unit can be 20-50 mole percent carbon monoxide, 20-40 mole percent molecular hydrogen, 0-10 mole percent methane, 10-30 mole percent carbon dioxide, 0-2 mole percent nitrogen, and 0-0.5 mole percent argon.

[0010] The syngas production zone may also include at least one processing zone. A syngas processing unit may be used to adjust the H:CO molar ratio and / or remove contaminants upstream of the FT reactor. Suitable processing zones include, but are not limited to, a water-gas shift reactor, a carbon dioxide capture unit, a contaminant removal zone, or a combination thereof.

[0011] Carbon dioxide is captured from the syngas (for sequestration) in a carbon dioxide capture unit. Suitable carbon dioxide capture units include, but are not limited to, an amine separation unit, a cryogenic separation unit, or a carbon dioxide PSA unit, or combinations thereof.

[0012] Suitable contaminant removal zones include, but are not limited to, sulfur removal zones, including, but not limited to, hydrodesulfurization reactors, sulfur guard beds (e.g., guard beds containing zinc oxide), or combinations thereof.

[0013] The H2:CO molar ratio in the syngas from the syngas reactor is adjusted in one or more of the processing zones within the syngas production zone so that the syngas is suitable for the FT reaction zone. The H2:CO molar ratio ranges from 0.5 to 3.0, or 1.0 to 3.0, or 1.5 to 3.0, or 0.5 to 2.5, or 1.0 to 2.5, or 1.5 to 2.5, or 1.7 to 2.2.

[0014] The synthesis gas is converted to liquid hydrocarbons in the FT reactor. Hydrocarbon products derived from the Fischer-Tropsch reaction range from methane to high-molecular-weight paraffin wax containing more than 50 carbon atoms. Numerous catalysts incorporating active metals, such as iron, cobalt, ruthenium, and rhenium, have been used to carry out the reaction, and both saturated and unsaturated hydrocarbons can be produced. The synthesis reaction is highly exothermic and temperature-sensitive, requiring temperature control to maintain the desired hydrocarbon product selectivity. Suitable catalysts and reaction conditions can be selected by those skilled in the art.

[0015] The FT reaction zone produces a liquid hydrocarbon stream and an off-gas stream. The liquid hydrocarbon stream may be sent to a fuel refinery zone for refinement to produce various types of fuels, such as jet fuel. The fuel refinery zone may include a hydrotreating zone.

[0016] The FT off-gas stream comprises hydrogen, carbon monoxide, methane, and an inert gas such as nitrogen and / or argon. For example, the off-gas stream may comprise 36 mol% hydrogen, 35 mol% carbon monoxide, 28 mol% methane, 0.4 mol% carbon dioxide, and 0.6 mol% nitrogen (dry basis). The temperature of the FT off-gas stream may be 40-70°C, and the pressure may be 3-5 MPa(g). The majority of the FT off-gas stream is recycled to the synthesis gas production zone or the FT reaction zone (or both) for conversion of residual methane, carbon monoxide, and hydrogen.

[0017] To prevent the accumulation of inert gases in the recycle loop, a purge stream is removed from the recycle off-gas stream. It is sent to a membrane separation unit, where it is separated into a permeate stream and a retentate stream. The permeate stream contains hydrogen. For example, the permeate stream may contain 82 mol% hydrogen, 12 mol% carbon monoxide, 5 mol% methane, 0.8 mol% carbon dioxide, and 0.15 mol% nitrogen. The temperature of the permeate stream may be 40-70°C, and the pressure may be 0.1-1.0 MPa(g). All or a portion of the permeate stream may be recycled to the FT reactor and / or the fuel purification zone. Alternatively, all or a portion of the permeate stream may be used elsewhere in the plant.

[0018] The residue stream comprises carbon monoxide, methane, and inert gases. For example, the residue stream may comprise 2 mole percent hydrogen, 52 mole percent carbon monoxide, 45 mole percent methane, 0.2 mole percent carbon dioxide, and 0.8 mole percent nitrogen. The temperature of the residue stream may be 40-80°C, and after cooling, 30-50°C, and the pressure may be 3-5 MPa(g). The residue stream is separated into a fuel gas stream and a second stream in a pressure swing adsorption (PSA) unit.

[0019] The fuel gas stream comprises an inert gas and a first portion of methane and carbon monoxide. For example, the fuel gas stream may comprise 6 mole percent hydrogen, 90 mole percent carbon monoxide, 2 mole percent methane, 0.0 mole percent carbon dioxide, and 2 mole percent nitrogen. The temperature of the fuel gas stream may be between 30 and 50°C, and the pressure may be between 3 and 5 MPa(g). The fuel gas stream may be recovered and used as fuel gas in various processes within the plant.

[0020] The second stream comprises a second portion of methane and carbon monoxide. More carbon monoxide is present in the second stream than in the fuel gas stream. For example, the second stream may contain more than 50%, or more than 60%, or more than 70%, or more than 80% carbon monoxide in the residue stream. For example, the second stream may comprise 0.4 mol% hydrogen, 41 mol% carbon monoxide, 58 mol% methane, 0.2 mol% carbon dioxide, and 0.4 mol% nitrogen. The temperature of the second stream may be between 0 and 30°C, and the pressure may be between 0.03 and 0.1 MPa(g). The second stream may be compressed and recycled to the synthesis gas production zone.

[0021] In some embodiments where oxygen is required in the synthesis gas production zone, such as autothermal reforming, gasification, or partial oxidation, a water electrolysis unit may be used to produce oxygen and hydrogen, preferably using renewable power. The oxygen may be used in the synthesis gas production zone, and the hydrogen may be used in the FT reaction zone and / or fuel refinery zone.

[0022] Process 100 is shown in the diagram. Feed stream 105 is introduced into synthesis gas production zone 110. Synthesis gas production zone 110 may include one or more reactors and, as discussed above, may optionally include one or more processing zones.

[0023] The effluent 115 from the synthesis gas production zone 110 is sent to a FT reaction zone 120. The FT process produces a liquid hydrocarbon stream 125 and a FT off-gas stream 130. The liquid hydrocarbon stream 125 may be upgraded by refining in a fuel refinery zone 132.

[0024] The FT off-gas stream 130 containing hydrogen, carbon monoxide, methane, and inert gases may be recycled to the synthesis gas production zone 110 .

[0025] A purge stream 135 is removed from the FT off-gas stream 130 and sent to a membrane separation unit 140 where it is separated into a permeate stream 145 and a retentate stream 150. The hydrogen-containing permeate stream 145 can be compressed and recycled to the FT reaction zone 120 or fuel purification zone 132, or can be used elsewhere in the plant.

[0026] Residue stream 150, containing carbon monoxide, methane, and inert gases, is sent to PSA unit 155 where it is separated into fuel gas stream 160 and second stream 165. Fuel gas stream 160, which contains inert gases and some carbon monoxide, is used as fuel gas. Second stream 165, containing carbon monoxide and methane, is sent back to synthesis gas production zone 110 or FT reaction zone 120, or both. [Example]

[0027] A computer simulation was performed for the process shown in the diagram. The synthesis gas production zone included a gasification zone with a biomass feedstock. A water electrolyzer was used to generate oxygen for the gasification reactor, hydrogen for the fuel purification zone, and additional hydrogen for the FT reaction zone. The purge stream from the off-gas recirculation loop was first sent to a membrane unit for selective permeation of hydrogen. This hydrogen in the membrane permeate was combined with the electrolyzer product hydrogen and sent to the FT reaction zone and the fuel purification zone. The membrane residue gas was sent to a PSA unit for selective recovery of methane and carbon monoxide in the PSA tail gas. This tail gas stream was sent to the synthesis gas production zone after compression. A first portion of the inert gas (nitrogen) and carbon monoxide was rejected in the high-pressure product stream from the PSA unit and sent to the fuel.

[0028] The results of the process simulation are shown below in Table 1. The addition of a PSA unit to the residue stream allows for the recovery of valuable methane and carbon monoxide reactants, avoiding the carbon emissions associated with the combustion of these components in the fuel gas stream. Rather, they are recycled within the system and ultimately converted into sustainable aviation fuel.

[0029] [Table 1]

[0030] Specific Embodiments While the following will be described in conjunction with specific embodiments, it will be understood that this description is illustrative, but not intended to limit the scope of the preceding description and appended claims.

[0031] A first embodiment of the present invention includes a process for producing a synthesis gas stream comprising a synthesis gas having a hydrogen to carbon monoxide molar ratio in the range of 0.5 to 3.0, reacting the synthesis gas stream in a Fischer-Tropsch (FT) reaction zone comprising a FT reactor to form a liquid hydrocarbon stream comprising liquid hydrocarbons and an FT off-gas stream comprising hydrogen, carbon monoxide, methane, and inert gases, and recycling a portion of the FT off-gas stream to the synthesis gas production zone or the FT reaction zone, or to both the synthesis gas production zone and the FT reaction zone. removing a purge stream from the FT off-gas stream, separating the purge stream in a membrane separation unit to form a permeate stream comprising hydrogen and a residue stream comprising carbon monoxide, methane, and inert gases, separating the residue stream in a pressure swing adsorption (PSA) unit into a fuel gas stream comprising the inert gases and a first portion of the carbon monoxide and methane, and a second stream comprising a second portion of the carbon monoxide and methane, and introducing the second stream into a synthesis gas production zone or an FT reaction zone, or both the synthesis gas production zone and the FT reaction zone. One embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph through the first embodiment of this paragraph, further comprising introducing the permeate stream into an FT reaction zone or a fuel refinery zone, or both the FT reaction zone or a fuel refinery zone. An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph through the first embodiment of this paragraph, wherein the syngas reactor comprises a steam reforming unit with an optional gas-heated reformer, or an autothermal reforming unit with an optional gas-heated reformer, or a gasification unit, or a partial oxidation (POX) unit, or a dry reforming unit, or a combination thereof.An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph through the first embodiment of this paragraph, wherein the syngas production zone further comprises at least one processing zone comprising a water-gas shift reactor, a carbon dioxide capture unit, a pollutant removal zone, or a combination thereof.An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph through the first embodiment of this paragraph, wherein the carbon dioxide capture unit comprises an amine separation unit, or a cryogenic separation unit, or a carbon dioxide PSA unit, or a combination thereof. An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph through the first embodiment of this paragraph, wherein the pollutant removal zone comprises a sulfur material removal zone. An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph through the first embodiment of this paragraph, further comprising introducing an oxygen stream into the synthesis gas production zone. An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph through the first embodiment of this paragraph, further comprising electrolyzing water to form an oxygen stream and a hydrogen stream. An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph through the first embodiment of this paragraph, wherein the inert gas comprises nitrogen or argon, or both. An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph through the first embodiment of this paragraph, wherein the second portion of carbon monoxide is greater than the first portion of carbon monoxide. An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph through the first embodiment of this paragraph, further comprising compressing the second stream prior to introducing the second stream into the synthesis gas production zone or the FT reaction zone, or into both the synthesis gas production zone and the FT reaction zone. An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph through the first embodiment of this paragraph, further comprising refining the liquid hydrocarbon stream in a fuel refining zone to produce jet fuel. An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph through the first embodiment of this paragraph, wherein the fuel refining zone is a hydroprocessing zone. An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph through the first embodiment of this paragraph, further comprising recovering the fuel gas stream.

[0032] A second embodiment of the present invention includes introducing a feed stream comprising a hydrocarbon or carbonaceous feedstock into a synthesis gas production zone comprising a synthesis gas reactor to produce a synthesis gas stream comprising a synthesis gas having a hydrogen to carbon monoxide molar ratio in the range of 0.5 to 3.0; reacting the synthesis gas stream in a Fischer-Tropsch (FT) reaction zone comprising a FT reactor to form a liquid hydrocarbon stream comprising liquid hydrocarbons and an FT off-gas stream comprising hydrogen, carbon monoxide, methane, and inert gases; recycling a portion of the FT off-gas stream to the synthesis gas production zone or the FT reaction zone, or to both the synthesis gas production zone and the FT reaction zone; removing a purge stream from the FT off-gas stream; and separating the purge stream in a membrane separation unit to produce a permeate stream comprising hydrogen. and a residue stream comprising carbon monoxide, methane, and inert gases; separating the residue stream in a pressure swing adsorption (PSA) unit into a fuel gas stream comprising the inert gases and a first portion of the carbon monoxide and methane, and a second stream comprising a second portion of the carbon monoxide and methane, wherein the second portion of the carbon monoxide is greater than the first portion of the carbon monoxide; introducing the second stream to a synthesis gas production zone or an FT reaction zone, or both the synthesis gas production zone and the FT reaction zone; introducing a permeate stream to the FT reaction zone or a fuel purification zone, or both the FT reaction zone or a fuel purification zone; and recovering the fuel gas stream. An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph through the second embodiment of this paragraph, wherein the syngas reactor comprises a steam reforming unit with an optional gas-heated reformer, or an autothermal reforming unit with an optional gas-heated reformer, or a gasification unit, or a partial oxidation (POX) unit, or a dry reforming unit, or a combination thereof.An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph through the second embodiment of this paragraph, wherein the syngas production zone further comprises at least one processing zone comprising a water-gas shift reactor, a carbon dioxide capture unit, a pollutant removal zone, or a combination thereof.An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph up to the second embodiment of this paragraph, wherein the inert gas comprises nitrogen or argon, or both. An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph up to the second embodiment of this paragraph, wherein the second portion of carbon monoxide is greater than the first portion of carbon monoxide. An embodiment of the present invention is one, any, or all of the preceding embodiments of this paragraph up to the second embodiment of this paragraph, further comprising compressing the second stream prior to introducing the second stream into the synthesis gas production zone.

[0033] Without further elaboration, it is believed that, using the preceding description, one skilled in the art can utilize the present invention to its fullest extent and easily ascertain the essential characteristics of the present invention, and can make various changes and modifications to the present invention to adapt it to various uses and conditions, without departing from the spirit and scope of the present invention. The preceding preferred specific embodiments are, therefore, to be construed as merely illustrative, and not limitative of the remainder of the disclosure in any way, and are intended to cover various modifications and equivalent arrangements included within the scope of the appended claims.

[0034] Above, all temperatures are set forth in degrees Celsius and all parts and percentages are by weight unless otherwise indicated.

Claims

1. 1. A process for producing liquid hydrocarbons, comprising: introducing a feed stream (105) comprising a hydrocarbon or carbonaceous feedstock into a synthesis gas production zone (110) comprising a synthesis gas reactor to produce a synthesis gas stream (115) comprising a synthesis gas having a hydrogen to carbon monoxide molar ratio in the range of 0.5 to 3.0; reacting said synthesis gas stream (115) in a Fischer-Tropsch (FT) reaction zone (120) comprising a FT reactor to form a liquid hydrocarbon stream (125) comprising said liquid hydrocarbons and an FT off-gas stream (130) comprising hydrogen, carbon monoxide, methane, and inert gases; recycling a portion of the FT off-gas stream (130) to the synthesis gas production zone (110) or the FT reaction zone (120), or to both the synthesis gas production zone (110) and the FT reaction zone (120); removing a purge stream (135) from said FT off-gas stream (130); separating the purge stream (135) in a membrane separation unit (140) to form a permeate stream (145) comprising hydrogen and a retentate stream (150) comprising the carbon monoxide, the methane, and the inert gas; separating the residue stream (150) in a pressure swing adsorption (PSA) unit (155) into a fuel gas stream (160) comprising the inert gas and a first portion of the carbon monoxide and methane, and a second stream (165) comprising a second portion of the carbon monoxide and methane; introducing said second stream (165) into said synthesis gas production zone (110) or said FT reaction zone (120), or into both said synthesis gas production zone (110) and said FT reaction zone (120).

2. 10. The process of claim 1, further comprising introducing the permeate stream (145) into the FT reaction zone (120) or the fuel refinery zone (132), or both the FT reaction zone (120) and the fuel refinery zone (132).

3. 3. The process of claim 1 or 2, further comprising compressing the second stream (165) prior to introducing the second stream (165) into the synthesis gas production zone (110) or the FT reaction zone (120), or both the synthesis gas production zone (110) and the FT reaction zone (120).

Images