How to produce sustainable aviation fuel from CO2 and low-carbon hydrogen

Abstract

A method for producing sustainable aviation fuel (SAF) with low carbon intensity. Jet fuel is produced by reaction of hydrogen obtained from electrolysis of water with captured carbon dioxide. The hydrogen and carbon dioxide react to produce a stream containing carbon monoxide. The hydrogen and carbon monoxide react to produce n-alkanes. The alkanes are hydroisomerized to produce sustainable aviation fuel with low carbon intensity.

Description

[Technical field]

[0001] FIELD OF THEINVENTION The field of the invention is low carbon hydrogen and captured CO 2 The present invention relates to a process for producing synthetic jet fuel or synthetic paraffinic kerosene from [Background technology]

[0002] 2. Background of the Invention Increased carbon dioxide concentrations in the global atmosphere are associated with global climate change. Combustion of fossil fuels in various engines produces carbon dioxide in the atmosphere. Concerns over climate change have led to a major societal shift towards renewable or low-carbon electricity. This has also increased activity towards decarbonizing the transport sector of the economy. As a result, the use of electric vehicles powered by renewable electricity has increased, helping to decarbonize the transport sector. Aviation is one of the most carbon-intensive transport sectors. Nevertheless, aviation accounts for more than 2% of global carbon dioxide emissions. The consumption of petroleum, fossil fuel-derived jet fuel by the aviation sector is a significant part of the total transport carbon dioxide emissions. However, sustainable aviation fuel (SAF) is currently significantly more expensive than fossil fuel-based jet fuel. It is almost impossible to electrify jet aircraft in the foreseeable future. Efficient and economical production of SAF can lead to a significant reduction in carbon dioxide emissions by the aviation sector.

[0003] Jet engines are complex technical devices that have been optimized for over 70 years to run on petroleum-derived jet fuel. Global standards for jet fuel properties have been developed. ASTM D1655 is the US standard for petroleum-derived jet fuel. Since 2009, separate standards have been developed for non-petroleum-derived jet fuels or jet fuel components. ASTM D7566-21 (Reference 1) is the current standard specification for aviation turbine fuels containing synthetic (non-petroleum-derived) hydrocarbons.

[0004] The catalytic hydrogenation of carbon monoxide to produce light gases, liquids and waxes from methane to heavy hydrocarbons (C100 and above) and further oxygenate the hydrocarbons is commonly referred to as Fischer-Tropsch (or FT) synthesis. One of the routes to produce non-petroleum-based synthetic paraffinic kerosene (SPK) permitted by ASTM D7566 is as a fuel obtained by the Fischer-Tropsch process. Conventional low-temperature (<250 °C) FT processes produce a high weight (or wt%) of FT wax (C) primarily from catalytic conversion processes. 24 These FT waxes are hydrocracked and / or further processed to produce diesel, naphtha and other fractions. Light hydrocarbons are also produced during the hydrocracking process. In some embodiments, these light hydrocarbons require additional upgrading to produce usable products. Common catalysts used for FT are cobalt (Co) or iron (Fe) based catalysts.

[0005] There are many routes to producing SPK from FT products, which are described in detail in various publications, including by de Klerk (Ref. 2). de Klerk deals with the hydrogenation of FT straight run kerosene to produce SPK, but the inherently high n-alkane content of the hydrogenated straight run FT product limits the amount of kerosene that can be blended into semi-synthetic jet fuel. This invention overcomes this issue and, although it focuses on straight run kerosene, it overcomes the problems of blending straight run FT kerosene into SPK via hydroisomerization. Hydroisomerization converts n-alkanes to isoparaffins. Elsewhere in de Klerk, Figure 10.3 shows the C 3 -C 5 FIG. 1 shows a route that includes oligomerization of a feed. The oligomerization reactor produces C5+ products that are hydrogenated to produce isoparaffinic kerosene. While the present invention has embodiments that include an oligomerization step, the accompanying invention does not include a C5+ product that results in a kerosene stream. 5 -C 9It has an oligomerization feed for a hydrocarbon stream.

[0006] Hydrocracking to produce jet fuel / SPK is shown in Figure 10.4 of de Klerk. FT wax (C 24+ ) is the main product from the low temperature FT synthesis handled by de Klerk. The wax is hydrocracked to produce a kerosene fraction which is fed into the SPK.

[0007] This is not the case in the present invention. The main liquid product of the present invention is C 9 -C 15 The product of the liquid fuel production reactor is converted to SPK. The hydrocracking reactor in the present invention mainly produces C 16 -C 24 It is used to convert materials.

[0008] Meurer and Kern (Reference 3) address the production of synthetic paraffinic kerosene from a power-to-liquids facility. This paper presents a process configuration for producing hydrogen using renewable electricity, which is used in an FT reactor, and a RWGS reactor to produce kerosene for use as jet fuel, with no CO2 emissions. 2 It is shown that Meurer converts kerosene to CO. However, there is an important difference. The FT process in the Meurer publication is different from the disclosed LFP technology. The Meurer FT system does not exceed 40% kerosene selectivity in any of the disclosed cases. The process in the present invention has a higher kerosene selectivity of 50% to 100%. Summary of the Invention [Problem to be solved by the invention]

[0009] The present invention relates to the production of low-carbon hydrogen and captured CO 2 The objective of the present invention is to provide a method for producing a synthetic paraffinic kerosene (SPK) blendstock for use as a sustainable aviation fuel from a natural gas source. [Means for solving the problem]

[0010] The present invention is a process for producing synthetic paraffinic kerosene for use as jet fuel. Renewable or low carbon electricity is used to convert water to hydrogen and oxygen in an electrolysis device. Carbon dioxide reacts with at least a portion of the hydrogen to produce a stream containing carbon monoxide. In this reaction, the single conversion rate of carbon dioxide is 50%-100%, preferably 60%-100%, and more preferably 70%-100%.

[0011] At least a portion of the produced carbon monoxide is reacted with hydrogen in a liquid fuel production (LFP) reactor to produce a liquid product comprising n-alkanes having carbon numbers between 5 and 24. 9 ~C 15 The fraction is between 40% and 100%, preferably between 45% and 100%, and more preferably between 50% and 100%. The LFP liquid product is further separated into three liquid streams in the LFP separation unit. The light LFP separation product stream is C 5 ~C 8 The middle LFP separation product stream contains C 9 ~C 15 The heavy LFP separation product stream contains C 16 ~C 24 Contains n-alkanes.

[0012] At least a portion of the medium LFP separation unit product stream is fed to a catalytic hydroisomerization unit to produce a hydroisomerization product stream. The hydroisomerization product stream is fed to a hydroisomerization separation unit to produce at least two hydroisomerization products. Among the hydroisomerization products, the heavy hydroisomerization product comprises branched alkanes having 9 to 15 carbon atoms. The heavy hydroisomerization product stream has a freezing point between -40°C and -60°C. In one embodiment, the freezing point is between -48°C and -60°C. In another embodiment, the freezing point is between -48°C and -55°C. In some embodiments, the heavy hydroisomerization product is a synthetic paraffinic kerosene (SPK) for use as a component of jet fuel.

[0013] In some embodiments of the invention, at least a portion of the light LFP separation unit product stream is fed to an oligomerization reactor to produce an oligomerization reactor product comprising hydrocarbons having 9 to 15 carbon atoms.

[0014] In some embodiments of the invention, at least a portion of the oligomerization reactor product is fed to an LFP separation unit.

[0015] In some embodiments of the invention, at least a portion of the heavy LFP separation unit product is fed to a hydrocracking reactor to produce a hydrocracked product stream that is fed to a hydrocrackate separation unit to produce at least two hydrocracked product streams, including a light hydrocracked product stream and a heavy hydrocracked product stream, the heavy hydrocracked product stream comprising hydrocarbons having a carbon number of 9 to 15.

[0016] In some embodiments of the invention, the carbon intensity (CI) of the SAF produced is between 0% and 50%, preferably between 0% and 20%, and more preferably between 0% and 10%. If negative carbon hydrogen produced from biomass, renewable natural gas, or other renewable feedstocks is used in the production of the SAF, the CI of the sustainable aviation fuel produced will be negative. Effect of the Invention

[0017] According to the present invention, low carbon hydrogen and captured CO 2 A method for producing synthetic paraffinic kerosene (SPK) blendstock for use as a sustainable aviation fuel is provided. [Brief description of the drawings]

[0018] [Figure 1] FIG. 1 shows a process for producing synthetic paraffinic kerosene using a hydroisomerization reactor. [Diagram 2] FIG. 2 shows a process for producing synthetic paraffinic kerosene using an oligomerization reactor. [Diagram 3] FIG. 3 shows a process for producing synthetic paraffinic kerosene using a hydrocracking reactor. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0019] Figure 1 shows an integrated process for producing synthetic paraffinic kerosene. Feed stream 1 is low carbon electricity. Low carbon electricity includes but is not limited to wind power, solar power, nuclear power, electricity generated from biomass or renewable natural gas, hydroelectric power, etc. Feed stream 2 is water. These are fed to unit 1, an electrolyzer. In the electrolyzer, hydrogen and oxygen are produced using water and low carbon energy. Water is fed to the electrolyzer. The electrolyzer is powered by low carbon electricity. Hydrogen is produced by electrolysis of water.

[0020] H 2 O=H 2+1 / 2O 2

[0021] An electrolyzer comprises an anode and a cathode separated by an electrolyte. Different electrolyzers function in slightly different ways. Different electrolyzers are designed to be used with different electrolysis technologies including alkaline electrolysis, polymer electrolyte membrane (PEM) electrolysis, solid oxide electrolysis, high temperature electrolysis, and other emerging types of electrolysis. The different electrolytes used are liquid KOH and NaOH, with or without activating compounds. Activating compounds are added to the electrolyte to improve the stability of the electrolyte. Most ionic activators for the hydrogen production reaction are ethylenediamine-based metal chloride complexes ("M(en) 3 " Cl x ,M1 / 4Co,Ni, etc.), and Na 2 MoO 4 Or Na 2 WO 4 The different electrocatalysts used on the electrodes contain various combinations of metals and oxides, such as Raney-Nickel-Aluminum, which are enhanced by the addition of cobalt or molybdenum to the alloy.

[0022] The products from the electrolyzer are a hydrogen-containing stream (product stream 1) and an oxygen-containing stream (product stream 2). By using renewable energy sources, the electrolyzer produces green hydrogen. Depending on the carbon intensity of the energy used in unit 1, other low-carbon hydrogen streams are produced. Other hydrogen production methods using renewable or non-renewable energy sources can also be used, including methane cracking, steam reforming with carbon capture, biomass gasification, renewable natural gas (RNG) reforming, or sourcing hydrogen from geological sources. Purification of the streams may then be required to produce hydrogen.

[0023] In FIG. 1, feed stream 3 is a stream containing carbon dioxide. Carbon dioxide is obtained from several sources. Power plants that generate electricity from various carbon sources emit large amounts of carbon dioxide. Industrial manufacturing plants that produce ammonia for fertilizer generate large amounts of carbon dioxide. Ethanol plants that convert corn or wheat into ethanol generate large amounts of carbon dioxide through fermentation. Other industrial fermentation processes also generate large amounts of carbon dioxide. Municipal wastewater treatment systems that use aerobic and anaerobic digestion of sludge also generate large amounts of CO 2 Generates CO as described here. 2 The use or conversion of CO 2 CO from gas streams where CO is not the predominant component (e.g., exhaust gas) 2 The process typically involves the separation and purification of the carbon dioxide. Usually, alkylamines are used to remove carbon dioxide from gas streams. The alkylamines used in the process include monoethanolamine, diethanolamine, methyldiethanolamine, diisopropylamine, aminoethoxyethanol or combinations thereof. Metal-organic framework (MOF) materials are used as a means to capture carbon dioxide from dilute streams using chemisorption or physisorption to capture carbon dioxide from the stream. Other methods to obtain concentrated carbon dioxide include chemical looping combustion, where a circulating metal oxide material captures carbon dioxide produced during the combustion process. Carbon dioxide can also be captured directly from the atmosphere by direct air capture technology (DAC). The carbon dioxide capture process often includes regeneration of the capture material. The alkylamines are regenerated by heating, typically with low pressure steam.

[0024] The captured carbon dioxide can be converted into useful products, such as fuels (e.g., diesel fuel, gasoline blend stock, jet fuel, etc.), chemicals (e.g., solvents, olefins, alcohols, aromatics, etc.), and other products that can replace fuels and chemicals produced from fossil resources such as oil and natural gas, thereby reducing the total emissions of carbon dioxide into the atmosphere. These are referred to as low-carbon, very low-carbon, zero-carbon, or negative-carbon fuels or chemicals.

[0025] Carbon dioxide streams obtained from industrial or biological processes, or captured directly from the atmosphere, or obtained from commercial carbon dioxide pipelines are not pure carbon dioxide. Carbon dioxide streams obtained from industrial facilities or pipelines contain 0 ppm to 2000 ppm by weight of sulfur-containing compounds, and also 0% to 10% by volume of hydrocarbons. To avoid problems in downstream processing, purification of the carbon dioxide, including removal of sulfur-containing compounds and hydrocarbons, is required. After purification, the purified carbon dioxide is suitable for the production of low- or zero-carbon fuels and chemicals.

[0026] At least a portion of the product stream 1 comprising hydrogen is mixed with a feed stream 3 comprising carbon dioxide to produce a reverse water gas shift (RWGS) reactor feed stream. The carbon dioxide and hydrogen react to carbon monoxide and water in the reverse water gas shift (RWGS) reactor, with the heat of reaction provided by a RWGS heater. The catalyst used in the RWGS reactor is a catalyst described in published U.S. patent application US17 / 300260.

[0027] At least a portion of product stream 4 (RWGS product stream) containing hydrogen and carbon monoxide becomes a liquid fuel production (LFP) reactor feed. The RWGS product containing carbon monoxide and optionally added hydrogen is reacted with fuels and chemicals in a liquid fuel production (LFP) reactor using a catalyst to produce long chain hydrocarbons for use as fuels and chemicals. The final product is a mixed hydrocarbon where the majority of the hydrocarbons in the mixture (e.g., 51% to 99% by volume) are hydrocarbons 24 carbon atoms or less in length.

[0028] The LFP hydrocarbon product stream (Product Stream 5) contains n-alkanes with carbon numbers between 5 and 24 and is fed to an LFP separation unit which produces at least three products. "Carbon number" refers to the number of carbon atoms in each alkane. LFP separation can be a variety of separation processes such as absorption, adsorption, filtration, distillation, etc. Preferably, the separation process is distillation. The LFP separation unit produces at least three products. The light LFP separation product contains n-alkanes with carbon numbers between 5 and 8. The heavy LFP separation product contains n-alkanes with carbon numbers between 16 and 24. The medium LFP separation product contains n-alkanes with carbon numbers between 9 and 15. The medium LFP separation product is within the boiling range of synthetic paraffinic kerosene or jet fuel. However, as shown in Example 1, the physical properties of the medium LFP separation product, which is rich in n-alkanes, do not meet the requirements of SPK jet fuel without additional processing.

[0029] In one embodiment of the present invention, at least a portion of the heavy LFP separation unit product is sold as premium low sulfur high cetane diesel fuel. "At least a portion" means a portion of the total. Non-limiting examples of "at least a portion" include 5%, 10%, 20%, 30%, 40%, 50%, 60%, 70%, 80%, 90% and 100%.

[0030] At least a portion of the medium LFP separation product is fed to Unit 5, or the hydroisomerization unit. Hydroisomerization improves the feed properties by converting normal alkane hydrocarbons to branched hydrocarbons of the same carbon number. This reaction improves the low temperature flow properties of the hydrocarbons. As shown in Example 1, the hydroisomerization reaction reduces the pour point or freeze point of the hydrocarbon stream.

[0031] The hydroisomerization reactor may be of any suitable design, preferably a cylindrical reactor with a liquid feed at the top of the reactor. The liquid feed containing the medium LFP separation product is mixed with a feed stream 5 containing hydrogen. The mixed feed is reacted in a catalyst bed in the reactor vessel. Typically, the reactor is a trickle bed reactor. At least a portion of the n-alkanes are passed through the catalyst and reacted to produce branched alkanes. The reactor comprises one or more catalyst beds. In some embodiments, additional hydrogen feed is injected between the various catalyst beds. The molar ratio of hydrogen to liquid hydrocarbon feed is 10-300, preferably 15-30, more preferably 19-25. The operating pressure of the hydroisomerization reactor is 10-100 bar, preferably 20-80 bar, more preferably 30-40 bar. The weight hourly space velocity (WHSV) is 0.1-10 kg (liquid feed) / hr·kg (catalyst), preferably 0.2-5 hr -1 More preferably, it is 0.5 to 2 hours. -1 The operating temperature of the reactor is 200℃ to 350℃.

[0032] The hydroisomerization catalyst is a solid shaped particle. The catalyst comprises a metal deposited on an acidic support. The catalytic metals are, in some embodiments, platinum and palladium, which provide hydrogenation and dehydrogenation activity. In some embodiments, the catalytic metal comprises nickel. In some embodiments, the catalytic metal comprises copper. In some embodiments, the catalytic metal comprises bimetallic metals, such as Ni-Cu, Ni-Mo, Pt-Fe, and Pt-Be. The acidic support is selected from any suitable support, such as ZSM-5, ZSM-22, ZSM-23, silica alumina, SiO 2 -Al 2 O 3 , beta zeolite, MCM-41, MCM-48, SBA-15 and supports including blends of these supports.

[0033] The conversion of n-alkanes to branched alkanes in the hydroisomerization reactor is preferably 50%-100%, more preferably 80%-100%. The reactor temperature, pressure, hydrogen to n-alkane ratio, and weight hourly space velocity (WHSV) are adjusted to maintain high conversion of n-alkanes to branched alkanes.

[0034] Figure 2 shows an alternative embodiment of the invention. In some embodiments of the invention, at least a portion of the light LFP separation unit product (product stream 9), which comprises a mixture of alkanes and alkenes, is fed to an oligomerization reactor (unit 7) to produce an oligomerization product (product stream 13). At least a portion of product stream 13 is sent back to the LFP separation unit (unit 4).

[0035] The light LFP separation unit product contains a mixture of n-alkanes and n-alkenes. The alkene / alkane ratio in the stream is controlled by varying the operating conditions of the LFP reactor. A low ratio of carbon monoxide to hydrogen in the LFP reactor feed and a high LFP reactor temperature favor the production of n-alkenes over n-alkanes. The alkenes react with each other to produce products within the boiling range of kerosene.

[0036] Oligomerization refers to one or more successive addition reactions between alkenes. An alkene addition is referred to as an oligomerization unless it is important to indicate a specific number of addition reactions. It is an umbrella term that includes dimerization (the addition reaction of two alkenes), trimerization, tetramerization, and higher number of addition reactions.

[0037] The oligomerization reactor (unit 7) is a fixed-bed reactor packed with catalyst. The reactor operates at temperatures between 100 °C and 300 °C and pressures between 8 and 70 bar. Different types of catalysts are used to oligomerize n-alkenes in the oligomerization reactor. These catalysts include SO 4 2- / ZrO 2 , H-ZSM-5, HY, Cr / H-ZSM-5, Cr / HY, Cr / H-MCM-41, solid phosphoric acid (SPA), metal promoted SPA catalyst, Fe / NiO / SPA, amorphous SiO 2 -Al 2 O 3 , H-ZSM-22, H-ZSM-57, Cr / SO 2 , H 3 PO 4 / SO 2 and other commercially available catalysts.

[0038] Due to the nature of the oligomerization reaction, linear alkenes produced in the LFP reactor are oligomerized to primarily branched alkenes. These branched oligomers are primarily dimers and trimers of the feed alkene. Although the branched products are primarily alkenes, with certain metal-promoted oligomerization catalysts, the alkenes produced by oligomerization can be hydrogenated to alkanes in the oligomerization reactor.

[0039] Kerosene and diesel range materials are produced by oligomerization. The properties of the fractions depend on the catalyst technology used. When ZSM-5 catalyzed oligomerization is employed, branching of the fractions is limited and the hydrogenated fractions have high cetane numbers and good cold flow properties.

[0040] There are currently commercial oligomerization technologies available that are used to convert alkenes in the light LFP separation unit products to hydrocarbons within the boiling range of kerosene. These commercial technologies include UOP Cat Poly, which uses a solid phosphoric acid (SPA) catalyst, Axens Polynaphtha, which uses amorphous silica-alumina, PetroSA COD technology, which uses H-ZSM-5 zeolite, ExxonMobil MOGD technology, or Emogas technology, which uses H-ZSM-5 zeolite, H-ZSM-22 zeolite, or H-ZSM-57.

[0041] At least a portion of the oligomerization reactor product (Stream 13) is recycled to the LFP separation unit (Unit 4). The oligomerized portion of the stream, which has a boiling range where the oligomers are primarily contained in the medium LFP separation unit product, is then sent to the hydroisomerization reactor (Unit 5). The alkenes from the oligomerization reactor (Unit 7) are hydrogenated to alkanes in the hydroisomerization reactor.

[0042] Figure 3 shows another optional embodiment of the invention. In this embodiment, instead of being sold as diesel fuel, the heavy hydroisomerization product (Stream 12) is sent to a hydrocracking reactor to increase the yield of kerosene or jet fuel. Hydrogen (Feed Stream 6) is also added to the hydrocracking reactor. Unlike standard petroleum refinery hydrocrackers, hydrocrackers are typically operated at lower severity (temperature and pressure) than petroleum refineries used to convert vacuum gas oil to diesel fuel. This is because the heteroatom levels (S, N) in the hydrocracked feed are very low and the carbon number distribution of the feed is lower than the C typical for petroleum vacuum gas oil. 44 C, not + 16 -C 24 This is because the operating pressure of the hydrocracker is in the range of 10 to 70 bar, preferably 25 to 35 bar. The operating temperature of the reactor is in the range of 250 to 380°C.

[0043] Hydrocracking catalysts require metals and acid sites. Many different catalysts have been investigated for n-alkane hydrocracking in general, and Fischer-Tropsch hydrocracking in particular. Based on the properties of the metals, there are two main catalyst classes relevant for the hydrocracking of these materials:

[0044] 1. Sulfided base metals on acidic support materials. These are typical crude oil hydrocracking catalysts, which require the addition of a sulfiding agent to keep the metals in the sulfided state. Such catalysts are used industrially with Syncrude in some Fischer-Tropsch units. The most commonly used catalysts of this type are NiMo and NiW on amorphous silica-alumina (ASA).

[0045] 2. Non-sulfided precious metal catalyst. Pt / SiO 2 -Al 2 O 3 Pt-based hydrocracking catalysts have proven to be very suitable for this application, providing higher cut selectivity at high conversions than sulfided base metal catalysts, but the use of Pt makes these catalysts more expensive.

[0046] The hydrocracking reactor is 16 -C 24 Material C 9 -C 15 The hydrocracked product stream (Product Stream 14) is sent to a hydrocracked product separation unit (Unit 9) to separate light gases (H 2 , C 1 ~C 4 ) is superficially dried. The heavy hydrocracked product separation unit (stream 16) contains hydrocarbons with carbon numbers between 5 and 15. At least a portion of the heavy hydrocracked product separation stream is sent back to the LFP separation unit (unit 4).

[0047] The SPK jet fuel of the present invention is carbon neutral and has no well-to-wheel CO emissions. 2 Emissions of 0-10gCO 2The emission factor is known as carbon intensity. Well-to-wheel emissions include all emissions associated with the production, processing, distribution and use of the fuel. Tools such as CA-GREET 3.0 (Reference 4) are used to calculate the overall carbon intensity.

[0048] Example 1: Hydroisomerization The LFP reactor produces an LFP hydrocarbon product stream comprising 50.7 volume percent of the hydrocarbon product stream comprising n-alkanes having carbon numbers between 9 and 15. The LFP separation unit produces a medium LFP separation unit product stream comprising n-alkanes having carbon numbers between 9 and 15.

[0049] According to ASTM D7566, the specifications of FT-derived SPK have some important properties. The main parameters are flash point (FLP) and freezing point (FP). The minimum flash point (FLP) is 38°C and the maximum freezing point (FP) is -40°C. However, the usual Jet A fuel used at US airports has a freezing point ranging from -42°C to -45°C.

[0050] Table 1 shows the C 9 From C 15 The data show the composition of the LFP hydrocarbon products ranging from C 9 -C 15 The results show that the n-alkane fraction of the LFP hydrocarbon product comprises 50.7% by volume of the total LFP hydrocarbon product. Without additional processing, the medium LFP separation product does not meet the SPK freezing point specification of a freezing point greater than -17.8°C. The medium LFP separation product meets the flash point specification of a flash point greater than 54.4°C.

[0051] [Table 1]

[0052] To meet SPK specifications, additional hydroisomerization of the medium LFP separation unit product is required. Table 1 shows the carbon number C 9 ~C 15shows the characteristics of methyl-branched n-alkanes.

[0053] After hydroisomerization, the freezing point (FP) is significantly reduced to below -48°C, which meets the SPK specification. The flash point (FLP) is slightly reduced, but still meets the SPK specification.

[0054] The overall composition and properties of Infinium jet fuel are shown in Table 2.

[0055] [Table 2]

[0056] Various overall properties of the Infinium synthetic jet fuel of the present invention are compared to standard jet fuel specifications in Table 3.

[0057] [Table 3]

[0058] In some embodiments, the D86 final boiling point of the Infinium synthetic jet fuel is in the range of 299°C to 250°C. In certain cases, the D86 final boiling point of the Infinium synthetic jet fuel is in the range of 290°C to 225°C. In certain cases, the D86 final boiling point of the Infinium synthetic jet fuel is in the range of 285°C to 235°C. In certain cases, the D86 final boiling point of the Infinium synthetic jet fuel is in the range of 275°C to 245°C.

[0059] In some embodiments, the density of the Infinium synthetic jet fuel at 15° C. ranges from 0.75 to 0.84 g / cc. In particular cases, the density of the Infinium synthetic jet fuel at 15° C. ranges from 0.75 to 0.82 g / cc. In particular cases, the density of the Infinium synthetic jet fuel at 15° C. ranges from 0.75 to 0.80 g / cc. In particular cases, the density of the Infinium synthetic jet fuel at 15° C. ranges from 0.75 to 0.77 g / cc.

[0060] In some embodiments, the smoke point of the Infinium synthetic jet fuel ranges from 40mm to 80mm. In some embodiments, the smoke point of the Infinium synthetic jet fuel ranges from 40mm to 75mm. In some embodiments, the smoke point of the Infinium synthetic jet fuel ranges from 40mm to 65mm.

[0061] In some embodiments, the aromatics content of the Infinium synthetic jet fuel ranges from 0.1 to 8% by volume. In some embodiments, the aromatics content of the Infinium synthetic jet fuel ranges from 0.1 to 4% by volume. In some embodiments, the aromatics content of the Infinium synthetic jet fuel ranges from 0.1 to 2% by volume. In some embodiments, the aromatics content of the Infinium synthetic jet fuel ranges from 0.1 to 1% by volume.

[0062] Example 2: Oligomerization The light LFP separation unit product is C 5 ~C 8 The composition in this example is 81.1 wt% C 5 -C 8 n-alkanes and 18.9 wt% C 5 -C 8 Alkenes. Oligomerization unit: 100°C, 8 bar, LHSV 1.2h -1 The catalyst used is sulfated zirconia (SO 4 2- / ZrO 2 The oligomerization reactor product was 81.1 wt.% C5-C8 n-alkanes, 10.4 wt.% C 9 ~C 15 Alkene, 7.6 wt% C 16 ~C 21 Alkenes, and 0.9 wt% C 22+ Alkenes. A portion of the oligomerization reactor product is recycled to the LFP separation unit.

[0063] There are numerous embodiments of the present invention, including, but not limited to, the following.

[0064] 1. A method for producing synthetic paraffinic kerosene includes using low carbon power in an electrolyzer to convert an electrolyzer feed comprising water into a first electrolyzer product stream comprising hydrogen and a second electrolyzer product stream comprising oxygen; mixing at least a portion of the first electrolyzer product stream comprising hydrogen with a stream comprising carbon dioxide to produce a RWGS reactor feed stream; feeding the RWGS reactor feed stream to a RWGS reactor to produce a RWGS product stream comprising hydrogen and carbon monoxide; using at least a portion of the RWGS product stream as an LFP reactor feed stream; feeding the LFP reactor feed stream to a liquid fuel production reactor to produce an LFP hydrocarbon product stream comprising n-alkanes having carbon numbers between 9 and 15; 9 -C 15 the n-alkane fraction is between 40% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit to produce at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; feeding at least a portion of the medium LFP separation unit product stream to a catalytic hydroisomerization unit to produce a hydroisomerization product stream, and feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products, the heavy hydroisomerization product comprising branched chain alkanes having 9 to 15 carbon atoms, and the heavy hydroisomerization product stream having a freezing point of -40°C or less.

[0065] 2. A method for producing synthetic paraffinic kerosene includes using low carbon power in an electrolyzer to convert an electrolyzer feed comprising water into a first electrolyzer product stream comprising hydrogen and a second electrolyzer product stream comprising oxygen; mixing at least a portion of the first electrolyzer product stream comprising hydrogen with a stream comprising carbon dioxide to produce a RWGS reactor feed stream; feeding the RWGS reactor feed stream to a RWGS reactor to produce a RWGS product stream comprising hydrogen and carbon monoxide; using at least a portion of the RWGS product stream as an LFP reactor feed stream; feeding the LFP reactor feed stream to a liquid fuel production reactor to produce an LFP hydrocarbon product stream comprising n-alkanes having carbon numbers between 9 and 15; 9 -C 15 the n-alkane fraction is between 40% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; and feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit, whereby the LFP separation unit produces at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; feeding at least a portion of the LFP separation unit product stream to a catalytic hydroisomerization unit to produce a hydroisomerization product stream; feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products, the heavy hydroisomerization product comprising branched alkanes having 9 to 15 carbon atoms, the freezing point of the heavy hydroisomerization product stream being below -40°C; and feeding at least a portion of the light LFP separation unit product stream to an oligomerization reactor to produce an oligomerization reactor product comprising hydrocarbons having 9 to 15 carbon atoms.

[0066] 3. A method for producing synthetic paraffinic kerosene includes using low carbon power in an electrolyzer to convert an electrolyzer feed comprising water into a first electrolyzer product stream comprising hydrogen and a second electrolyzer product stream comprising oxygen; combining at least a portion of the first electrolyzer product stream comprising hydrogen with a stream comprising carbon dioxide to produce a RWGS reactor feed stream; feeding the RWGS reactor feed stream to a RWGS reactor to produce a RWGS product stream comprising hydrogen and carbon monoxide; using at least a portion of the RWGS product stream as an LFP reactor feed stream; feeding the LFP reactor feed stream to a liquid fuel production reactor to produce an LFP hydrocarbon product stream comprising n-alkanes having carbon numbers between 9 and 15; 9 -C 15 the n-alkane fraction is between 40% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; and feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit, whereby the LFP separation unit produces at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; feeding at least a portion of the LFP separation unit product stream to a catalytic hydroisomerization unit to produce a hydroisomerization product stream; feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products, the heavy hydroisomerization product comprising branched alkanes having 9 to 15 carbon atoms, the freezing point of the heavy hydroisomerization product stream being below -40°C; and feeding at least a portion of the light LFP separation unit product stream to an oligomerization reactor to produce an oligomerization reactor product comprising hydrocarbons having 9 to 15 carbon atoms.

[0067] 4. A method for producing synthetic paraffinic kerosene includes using low carbon power in an electrolyzer to convert an electrolyzer feed comprising water into a first electrolyzer product stream comprising hydrogen and a second electrolyzer product stream comprising oxygen; combining at least a portion of the first electrolyzer product stream comprising hydrogen with a stream comprising carbon dioxide to produce a RWGS reactor feed stream; feeding the RWGS reactor feed stream to a RWGS reactor to produce a RWGS product stream comprising hydrogen and carbon monoxide; using at least a portion of the RWGS product stream as an LFP reactor feed stream; feeding the LFP reactor feed stream to a liquid fuel production reactor to produce an LFP hydrocarbon product stream comprising n-alkanes having carbon numbers between 9 and 15; 9 -C 15the n-alkane fraction is between 40% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit to produce at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; feeding at least a portion of the medium LFP separation unit product stream to a catalytic hydroisomerization unit to produce a hydroisomerization product stream, and feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least three product streams. and feeding at least a portion of the light LFP separation unit product stream to an oligomerization reactor to produce an oligomerization reactor product comprising hydrocarbons having 9 to 15 carbon atoms; feeding at least a portion of the heavy LFP separation unit product stream to a hydrocracking reactor to produce a hydrocracked product stream; and feeding the hydrocracked product stream to a hydrocracked product separation unit to produce at least two hydrocracked product streams, the light hydrocracked product stream comprising hydrogen and the heavy hydrocracked product stream comprising hydrocarbons having 9 to 15 carbon atoms.

[0068] 5. A method for producing synthetic paraffinic kerosene includes using low carbon power in an electrolyzer to convert an electrolyzer feed comprising water into a first electrolyzer product stream comprising hydrogen and a second electrolyzer product stream comprising oxygen; combining at least a portion of the first electrolyzer product stream comprising hydrogen with a stream comprising carbon dioxide to produce a RWGS reactor feed stream; feeding the RWGS reactor feed stream to a RWGS reactor to produce a RWGS product stream comprising hydrogen and carbon monoxide; using at least a portion of the RWGS product stream as an LFP reactor feed stream; feeding the LFP reactor feed stream to a liquid fuel production reactor to produce an LFP hydrocarbon product stream comprising n-alkanes having carbon numbers of 9 to 15; 9 -C 15 the n-alkane fraction is between 40% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit, whereby the LFP separation unit produces at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; feeding at least a portion of the medium LFP separation unit product stream to a catalytic hydroisomerization unit to produce a hydroisomerization product stream; feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products; the heavy hydroisomerization product comprises branched alkanes having 9 to 15 carbon atoms, the heavy hydroisomerization product stream having a freezing point of -40°C or less; and feeding at least a portion of the light LFP separation unit product stream to an oligomerization reactor to produce at least two hydroisomerization products. producing an oligomerization reactor product comprising hydrocarbons having a carbon number of 9 to 15; feeding at least a portion of the heavy LFP separation unit product to a hydrocracking reactor to produce a hydrocracked product stream; feeding the hydrocracked product stream to a hydrocracked product separation unit to produce at least two hydrocracked product streams, the light hydrocracked product stream comprising hydrogen and the heavy hydrocracked product stream comprising hydrocarbons having a carbon number of 9 to 15; and feeding the heavy hydrocracked product stream to the LFP separation unit.

[0069] 6. A method for producing synthetic paraffinic kerosene includes feeding an LFP reactor feed stream containing hydrogen and carbon monoxide to a liquid fuel production reactor to produce an LFP hydrocarbon product stream containing n-alkanes having carbon numbers between 9 and 15, 9 -C 15the n-alkane fraction is 50% to 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit to produce at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; feeding at least a portion of the medium LFP separation unit product stream to a catalytic hydroisomerization unit to produce a hydroisomerization product stream, and feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products, the heavy hydroisomerization product comprising branched chain alkanes having 9 to 15 carbon atoms, and the heavy hydroisomerization product stream having a freezing point of -40°C or less.

[0070] 7. A method for producing synthetic paraffinic kerosene includes feeding an LFP reactor feed stream containing hydrogen and carbon monoxide to a liquid fuel production reactor to produce an LFP hydrocarbon product stream containing n-alkanes having carbon numbers between 9 and 15, 9 -C 15the n-alkane fraction is between 50% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; and feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit, whereby the LFP separation unit produces at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; and feeding at least a portion of the LFP separation unit product stream to a catalytic hydroisomerization unit to produce a hydroisomerization product stream; feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products, the heavy hydroisomerization product comprising branched alkanes having 9 to 15 carbon atoms, the freezing point of the heavy hydroisomerization product stream being below -40°C; and feeding at least a portion of the light LFP separation unit product stream to an oligomerization reactor to produce an oligomerization reactor product comprising hydrocarbons having 9 to 15 carbon atoms.

[0071] 8. A method for producing synthetic paraffinic kerosene includes feeding an LFP reactor feed stream containing hydrogen and carbon monoxide to a liquid fuel production reactor to produce an LFP hydrocarbon product stream containing n-alkanes having carbon numbers between 9 and 15, 9 -C 15the n-alkane fraction is between 50% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit, where the LFP separation unit produces at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; and subjecting at least a portion of the medium LFP separation unit product stream to catalytic hydroisomerization. supplying the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products, the heavy hydroisomerization product comprising branched alkanes having 9 to 15 carbon atoms, the heavy hydroisomerization product stream having a freezing point of -40°C or less; supplying at least a portion of the light LFP separation unit product stream to an oligomerization reactor to produce an oligomerization reactor product comprising hydrocarbons having 9 to 15 carbon atoms, and supplying at least a portion of the oligomerization reactor product to the LFP separation unit.

[0072] 9. A method for producing synthetic paraffinic kerosene includes feeding an LFP reactor feed stream containing hydrogen and carbon monoxide to a liquid fuel production reactor to produce an LFP hydrocarbon product stream containing n-alkanes having carbon numbers between 9 and 15, 9 -C 15the n-alkane fraction is between 50% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit to produce at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; feeding at least a portion of the medium LFP separation unit product stream to a catalytic hydroisomerization unit to produce a hydroisomerization product stream, and feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least three product streams. and feeding at least a portion of the light LFP separation unit product stream to an oligomerization reactor to produce an oligomerization reactor product comprising hydrocarbons having 9 to 15 carbon atoms; feeding at least a portion of the heavy LFP separation unit product stream to a hydrocracking reactor to produce a hydrocracked product stream; and feeding the hydrocracked product stream to a hydrocracked product separation unit to produce at least two hydrocracked product streams, the light hydrocracked product stream comprising hydrogen and the heavy hydrocracked product stream comprising hydrocarbons having 9 to 15 carbon atoms.

[0073] 10. A method for producing synthetic paraffinic kerosene includes feeding an LFP reactor feed stream containing hydrogen and carbon monoxide to a liquid fuel production reactor to produce an LFP hydrocarbon product stream containing n-alkanes having carbon numbers between 9 and 15, 9 -C 15the n-alkane fraction is between 50% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit to produce at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; feeding at least a portion of the medium LFP separation unit product stream to a catalytic hydroisomerization unit to produce a hydroisomerization product stream; and feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products. the heavy hydroisomerization product comprises branched alkanes having a carbon number of 9 to 15, and the freezing point of the heavy hydroisomerization product stream is below -40°C; feeding at least a portion of the light LFP separation unit product stream to an oligomerization reactor to produce an oligomerization reactor product comprising hydrocarbons having a carbon number of 9 to 15; feeding at least a portion of the heavy LFP separation unit product stream to a hydrocracking reactor to produce a hydrocracked product stream; feeding the hydrocracked product stream to a hydrocracked product separation unit to produce at least two hydrocracked product streams; the light hydrocracked product stream comprises hydrogen, the heavy hydrocracked product stream comprises hydrocarbons having a carbon number of 9 to 15, and feeding the heavy hydrocracked product stream to the LFP separation unit.

[0074] 11. A method for producing synthetic paraffinic kerosene includes using low carbon power in an electrolyzer to convert an electrolyzer feed comprising water into a first electrolyzer product stream comprising hydrogen and a second electrolyzer product stream comprising oxygen; mixing at least a portion of the first electrolyzer product stream comprising hydrogen with a stream comprising carbon dioxide to produce a RWGS reactor feed stream; feeding the RWGS reactor feed stream to a RWGS reactor to produce a RWGS product stream comprising hydrogen and carbon monoxide; using at least a portion of the RWGS product stream as an LFP reactor feed stream; feeding the LFP reactor feed stream to a liquid fuel production reactor to produce an LFP hydrocarbon product stream comprising n-alkanes having carbon numbers of 9 to 15; 9 -C 15 the n-alkane fraction is between 40% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit, whereby the LFP separation unit produces at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; and feeding at least a portion of the P separation unit product stream to a catalytic hydroisomerization unit, the hydroisomerization unit being a catalytic reactor, the catalyst comprising a precious metal selected from the group consisting of platinum and palladium, the catalytic hydroisomerization unit producing a hydroisomerization product stream, and feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products, the heavy hydroisomerization product comprising branched alkanes having 9 to 15 carbon atoms, and the freezing point of the deuterium isomerization product stream being equal to or lower than -40°C.

[0075] 12. A method for producing synthetic paraffinic kerosene includes using low carbon power in an electrolyzer to convert an electrolyzer feed comprising water into a first electrolyzer product stream comprising hydrogen and a second electrolyzer product stream comprising oxygen; mixing at least a portion of the first electrolyzer product stream comprising hydrogen with a stream comprising carbon dioxide to produce a RWGS reactor feed stream; feeding the RWGS reactor feed stream to a RWGS reactor to produce a RWGS product stream comprising hydrogen and carbon monoxide; using at least a portion of the RWGS product stream as an LFP reactor feed stream; feeding the LFP reactor feed stream to a liquid fuel production reactor to produce an LFP hydrocarbon product stream comprising n-alkanes having carbon numbers of 9 to 15; 9 -C 15 and wherein the n-alkane fraction is between 40% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; and wherein at least a portion of the LFP hydrocarbon product stream is fed to an LFP separation unit, whereby the LFP separation unit produces at least three product streams, the light LFP separation unit product comprising n-alkanes having a carbon number of 5 to 8, the medium LFP separation unit product stream comprising n-alkanes having a carbon number of 9 to 15, and the heavy LFP separation unit product comprising n-alkanes having a carbon number of 16 to 24. providing at least a portion of the medium LFP separation unit product stream to a catalytic hydroisomerization unit, the hydroisomerization unit being a catalytic reactor, the catalyst comprising nickel, the catalytic hydroisomerization unit producing a hydroisomerization product stream, and providing the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products, the heavy hydroisomerization product comprising branched alkanes having 9 to 15 carbon atoms, and the deuterium isomerization product stream having a freezing point of -40°C or less.

[0076] 13. A method for producing synthetic paraffinic kerosene includes using low carbon power in an electrolyzer to convert an electrolyzer feed comprising water into a first electrolyzer product stream comprising hydrogen and a second electrolyzer product stream comprising oxygen; mixing at least a portion of the first electrolyzer product stream comprising hydrogen with a stream comprising carbon dioxide to produce a RWGS reactor feed stream; feeding the RWGS reactor feed stream to a RWGS reactor to produce a RWGS product stream comprising hydrogen and carbon monoxide; using at least a portion of the RWGS product stream as an LFP reactor feed stream; feeding the LFP reactor feed stream to a liquid fuel production reactor to produce an LFP hydrocarbon product stream comprising n-alkanes having carbon numbers of 9 to 15; 9 -C 15 and wherein the n-alkane fraction is between 40% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; and wherein at least a portion of the LFP hydrocarbon product stream is fed to an LFP separation unit, whereby the LFP separation unit produces at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms. -alkanes; feeding at least a portion of the medium LFP separation unit product stream to a catalytic hydroisomerization unit, the hydroisomerization unit being a catalytic reactor, the catalyst comprising copper, the catalytic hydroisomerization unit producing a hydroisomerization product stream, and feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products, the heavy hydroisomerization product comprising branched chain alkanes having 9 to 15 carbon atoms, and the deuterium isomerization product stream having a freezing point of -40°C or less.

[0077] 14. A method for producing synthetic paraffinic kerosene includes using low carbon power in an electrolyzer to convert an electrolyzer feed comprising water into a first electrolyzer product stream comprising hydrogen and a second electrolyzer product stream comprising oxygen; mixing at least a portion of the first electrolyzer product stream comprising hydrogen with a stream comprising carbon dioxide to produce a RWGS reactor feed stream; feeding the RWGS reactor feed stream to a RWGS reactor to produce a RWGS product stream comprising hydrogen and carbon monoxide; using at least a portion of the RWGS product stream as an LFP reactor feed stream; feeding the LFP reactor feed stream to a liquid fuel production reactor to produce an LFP hydrocarbon product stream comprising n-alkanes having carbon numbers of 9 to 15; 9 -C 15 the n-alkane fraction is between 40% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit, where the LFP separation unit produces at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; and subjecting at least a portion of the medium LFP separation unit product stream to a catalytic hydroisomerization unit. feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products, the heavy hydroisomerization product comprising branched alkanes having 9 to 15 carbon atoms, the deuterium isomerization product stream having a freezing point of -40°C or less; feeding at least a portion of the light LFP separation unit product stream to an oligomerization reactor, the oligomerization reactor being a catalytic reactor, the catalyst comprising solid phosphoric acid, and the oligomerization reactor producing an oligomerization reactor product comprising hydrocarbons having 9 to 15 carbon atoms.

[0078] 15. A method for producing synthetic paraffinic kerosene includes using low carbon power in an electrolyzer to convert an electrolyzer feed comprising water into a first electrolyzer product stream comprising hydrogen and a second electrolyzer product stream comprising oxygen; combining at least a portion of the first electrolyzer product stream comprising hydrogen with a stream comprising carbon dioxide to produce a RWGS reactor feed stream; feeding the RWGS reactor feed stream to a RWGS reactor to produce a RWGS product stream comprising hydrogen and carbon monoxide; using at least a portion of the RWGS product stream as an LFP reactor feed stream; feeding the LFP reactor feed stream to a liquid fuel production reactor to produce an LFP hydrocarbon product stream comprising n-alkanes having carbon numbers of 9 to 15; 9 -C 15 the n-alkane fraction is between 40% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit, where the LFP separation unit produces at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; and subjecting at least a portion of the medium LFP separation unit product stream to catalytic hydroisomerization. and feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products, the heavy hydroisomerization product comprising branched alkanes having 9 to 15 carbon atoms, the deuterium isomerization product stream having a freezing point of -40°C or less, and feeding at least a portion of the light LFP separation unit product stream to an oligomerization reactor, the oligomerization reactor being a catalytic reactor, the catalyst comprising chromium, and the oligomerization reactor producing an oligomerization reactor product comprising hydrocarbons having 9 to 15 carbon atoms.

[0079] 16. A method for producing synthetic paraffinic kerosene includes using low carbon power in an electrolyzer to convert an electrolyzer feed comprising water into a first electrolyzer product stream comprising hydrogen and a second electrolyzer product stream comprising oxygen; mixing at least a portion of the first electrolyzer product stream comprising hydrogen with a stream comprising carbon dioxide to produce a RWGS reactor feed stream; feeding the RWGS reactor feed stream to a RWGS reactor to produce a RWGS product stream comprising hydrogen and carbon monoxide; using at least a portion of the RWGS product stream as an LFP reactor feed stream; feeding the LFP reactor feed stream to a liquid fuel production reactor to produce an LFP hydrocarbon product stream comprising n-alkanes having carbon numbers of 9 to 15; 9 -C 15 the n-alkane fraction is between 40% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit, whereby the LFP separation unit produces at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; feeding at least a portion of the light LFP separation unit product stream to a catalytic hydroisomerization unit to produce a hydroisomerization product stream; feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products; the heavy hydroisomerization product comprises branched alkanes having 9 to 15 carbon atoms, the deuterium isomerization product stream having a freezing point of −40° C. or less; feeding at least a portion of the light LFP separation unit product stream to an oligomerization reactor, the oligomerization reactor being a catalytic reactor, the catalyst being SO 4 2- / ZrO 2 and the oligomerization reactor produces an oligomerization reactor product comprising hydrocarbons having 9 to 15 carbon atoms.

[0080] 17. A method for producing synthetic paraffinic kerosene includes feeding an LFP reactor feed stream containing hydrogen and carbon monoxide to a liquid fuel production reactor to produce an LFP hydrocarbon product stream containing n-alkanes having carbon numbers between 9 and 15, 9 -C 15 the n-alkane fraction is 50% to 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit to produce at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; feeding at least a portion of the medium LFP separation unit product stream to a catalytic hydroisomerization unit to produce a hydroisomerization product stream, and feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products, the heavy hydroisomerization product stream being a hydrogen peroxide fraction. the isomerization product comprises branched alkanes having 9 to 15 carbon atoms, the freezing point of the heavy hydroisomerization product stream is below -40°C; feeding at least a portion of the light LFP separation unit product stream to an oligomerization reactor to produce an oligomerization reactor product comprising hydrocarbons having 9 to 15 carbon atoms; feeding at least a portion of the heavy LFP separation unit product to a hydrocracking reactor, the hydrocracker being a catalytic reactor, the catalyst comprising a sulfide base metal on an acidic support material, the hydrocracking reactor producing a hydrocracked product stream; and feeding the hydrocracked product stream to a hydrocracked product separation unit to produce at least two hydrocracked product streams, the light hydrocracked product stream comprising hydrogen, and the heavy hydrocracked product stream comprising hydrocarbons having 9 to 15 carbon atoms.

[0081] 18. A method for producing synthetic paraffinic kerosene includes feeding an LFP reactor feed stream containing hydrogen and carbon monoxide to a liquid fuel production reactor to produce an LFP hydrocarbon product stream containing n-alkanes having carbon numbers between 9 and 15, 9 -C 15 the n-alkane fraction is between 50% and 100% by volume of the total hydrocarbon products in the LFP hydrocarbon product stream; feeding at least a portion of the LFP hydrocarbon product stream to an LFP separation unit to produce at least three product streams, the light LFP separation unit product comprising n-alkanes having 5 to 8 carbon atoms, the medium LFP separation unit product stream comprising n-alkanes having 9 to 15 carbon atoms, and the heavy LFP separation unit product comprising n-alkanes having 16 to 24 carbon atoms; feeding at least a portion of the medium LFP separation unit product stream to a catalytic hydroisomerization unit to produce a hydroisomerization product stream; and feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two hydroisomerization products. the heavy hydroisomerization product comprises branched alkanes having 9 to 15 carbon atoms, the heavy hydroisomerization product stream having a freezing point of -40°C or less; feeding at least a portion of the light LFP separation unit product stream to an oligomerization reactor to produce an oligomerization reactor product comprising hydrocarbons having 9 to 15 carbon atoms; feeding at least a portion of the heavy LFP separation unit product to a hydrocracking reactor, the hydrocracker being a catalytic reactor, the catalyst comprising a non-sulfided precious metal, the hydrocracking reactor producing a hydrocracked product stream; feeding the hydrocracked product stream to a hydrocracked product separation unit to produce at least two hydrocracked product streams, the light hydrocracked product stream comprising hydrogen, and the heavy hydrocracked product stream comprising hydrocarbons having 9 to 15 carbon atoms.

[0082] References

[0083] 1.ASTM D7566-21 is the relevant standard for jet fuel, "Standard Specification for Aviation Turbine Fuel Containing Synthesized Hydrocarbons," and Appendix 1 covers the specifications for synthetic paraffinic kerosene (SPK) produced by the Fischer-Tropsch reaction. The specification was published on July 1, 2021.

[0084] 2.Arno de Klerk, “Aviation Turbine Fuels Through the Fischer-Tropsch Process”, Chapter 10 in Biofuels for Aviation. 2016 Elsevier Inc. DOI:http: / / dx.doi.org / 10.1016 / B978-0-12-804568-8.00010-X

[0085] 3. Andreas Meurer and Jurgen Kern, “Fischer-Tropsch Synthesis as the Key for Decentralized Sustainable Kerosene Production”, Energies 2021, 14, 1836. https: / / doi.org / 10.3390 / en14071836, https: / / www.mdpi.com / journal / energies

Claims

1. 1. A hydrocarbon suitable for use as a jet fuel component, comprising: Carbon intensity (CI) is 0 to 10 gCO ２ eq / MJ, The freezing point is −48 to −55° C. The final boiling point according to D86 is 250 to 299°C; The density is 0.75 to 0.84 g / cc; The smoke point is 40 to 60 mm. The content of aromatic compounds is 0.01 to 7% by volume. Hydrocarbons.

2. The amount of particulate contaminants is 0.001 to 0.2 mg / l; The hydrocarbon of claim 1.

3. The flash point is 40 to 50°C. The hydrocarbon of claim 1.

4. The viscosity at -20°C is 1.0 to 5.

0. The hydrocarbon of claim 1.

5. The specific energy is 18,500 to 21,000 Btu / lb. The hydrocarbon of claim 1.

6. The hydrogen content is 14.0 to 17.5 wt.%. The hydrocarbon of claim 1.

7. The sulfur content is 0.1 to 4 ppm. The hydrocarbon of claim 1.

8. The flash point is 40 to 50°C. The viscosity at -20°C is 1.0 to 5.

0. The hydrocarbon of claim 2.

9. The specific energy is 18,500 to 21,000 Btu / lb; The hydrogen content is 14.0 to 17.5 wt. %; The sulfur content is 0.1 to 4 ppm. The hydrocarbon of claim 2.

10. The flash point is 40 to 50°C. The viscosity at -20°C is 1.0 to 5.

0. The hydrocarbon of claim 9.

11. a. low carbon electricity is used in an electrolyzer to convert an electrolyzer feed comprising water into a first electrolyzer product stream comprising hydrogen and a second electrolyzer product stream comprising oxygen; b. mixing at least a portion of the first electrolyzer product stream with carbon dioxide to produce a RWGS reactor feed stream; c. feeding the RWGS reactor feed stream to a RWGS reactor to produce a RWGS product stream comprising hydrogen and carbon monoxide; d. feeding at least a portion of the RWGS product stream to an LFP reactor to produce C ９ ~C １５ producing an LFP hydrocarbon product stream comprising n-alkanes and alkenes of The C in the LFP hydrocarbon product stream ９ ~C １５ % to 99 vol. % of n-alkanes and alkenes; f.C ９ ~C １５ feeding at least a portion of said n-alkane stream to a catalytic hydroisomerization unit to produce a hydroisomerization product stream; the hydroisomerization product stream is fed to a hydroisomerization separation unit to produce at least two hydroisomerization products; At least one of the hydroisomerization product streams meets ASTM D7566-21. A method for producing synthetic paraffinic kerosene.

12. a. low carbon electricity is used in an electrolyzer to convert an electrolyzer feed comprising water into a first electrolyzer product stream comprising hydrogen and a second electrolyzer product stream comprising oxygen; b. mixing at least a portion of the first electrolyzer product stream with carbon dioxide to produce a RWGS reactor feed stream; c. feeding the RWGS reactor feed stream to a RWGS reactor to produce a RWGS product stream comprising hydrogen and carbon monoxide; d. feeding at least a portion of the RWGS product stream to an LFP reactor to produce C ５ ~C ２４ producing an LFP hydrocarbon product stream comprising n-alkanes and alkenes of The C in the LFP hydrocarbon product stream ５ ~C ２４ % to 99 vol. % of n-alkanes and alkenes; e. feeding at least a portion of said LFP hydrocarbon product stream to an LFP separation unit; The LFP hydrocarbon product stream comprises at least three LFP separation products, namely: ５ ~C ８ A light LFP separation product containing n-alkanes of C ９ ~C １５ a medium LFP separation product containing n-alkanes of C １６ ~C ２４ a heavy LFP separation product comprising n-alkanes of f. feeding at least a portion of the medium LFP separation product to a hydroisomerization reactor and combining with a hydrogen stream to produce a hydroisomerization product stream; the hydroisomerization reactor comprises a hydroisomerization catalyst; g. feeding the hydroisomerization product stream to a hydroisomerization separation unit to produce at least two separated hydroisomerization products, a light hydroisomerization product and a heavy hydroisomerization product; The heavy hydroisomerization product is ９ ~C １５ and the freezing point of the heavy hydroisomerization product is −55 to −48° C., thereby producing a synthetic paraffinic kerosene. A method for producing synthetic paraffinic kerosene.

13. The light LFP separation product is fed to an oligomerization reactor; the oligomerization reactor comprises a catalyst; the oligomerization reactor converts the alkene into an oligomer stream; At least a portion of the oligomer stream is recycled to the LFP separation unit. A method for producing the synthetic paraffinic kerosene according to claim 12.

14. feeding at least a portion of the heavy LFP separation product to a hydrocracking reactor to produce a hydrocracked product stream; the hydrocracking reactor comprises a catalyst; feeding the hydrocracked product stream to a hydrocracked product separation unit to produce at least two hydrocracked product streams, a light hydrocracked product stream and a heavy hydrocracked product stream; the light hydrocracked product stream comprises hydrogen; The heavy hydrocracked product stream is ９ ~C １５ containing hydrocarbons of A method for producing the synthetic paraffinic kerosene according to claim 12.

15. the hydroisomerization catalyst is a three-dimensionally shaped particle comprising a metal deposited on an acidic support; A method for producing the synthetic paraffinic kerosene according to claim 12.

16. Said C ９ ~C １５ The branched alkanes are Carbon intensity (CI) is 0 to 10 gCO ２ eq / MJ, The final boiling point according to D86 is 250 to 299°C; The density is 0.75 to 0.84 g / cc; The smoke point is 40 to 60 mm. The content of aromatic compounds is 0.01 to 7% by volume. A method for producing the synthetic paraffinic kerosene according to claim 12.

17. The catalyst in the oligomerization reactor is SO ４ ２－ / ZrO ２ , H-ZSM-5, H-Y, Cr / H-ZSM-5, Cr / H-Y, Cr / H-MCM-41, solid phosphoric acid (SPA), metal-promoted solid phosphoric acid, Fe / NiO / SPA, amorphous SiO ２ -Al ２ O ３ , H-ZSM-22, H-ZSM-57, Cr / SO ２ , H ３ P.O. ４ / SO ２ A catalyst selected from the group consisting of A method for producing the synthetic paraffinic kerosene according to claim 13.

18. the hydrocracking reactor catalyst is selected from the group of catalysts consisting of sulfided base metal and non-sulfided precious metal catalysts on acidic support materials; A method for producing the synthetic paraffinic kerosene according to claim 14.

19. At least a portion of the heavy hydrocracked product stream is recycled to the LFP separation unit. A method for producing the synthetic paraffinic kerosene according to claim 14.

20. the metal of the hydroisomerization catalyst is selected from the group of metals consisting of platinum, palladium, nickel, copper, Ni-Cu, Ni-Mo, Pt-Fe and Pt-Be; A method for producing the synthetic paraffinic kerosene according to claim 15.

21. The acidic carrier is ZSM-5, ZSM-22, ZSM-23, silica, alumina, SiO ２ -Al ２ O ３ , beta zeolite, MCM-41, MCM-48, SBA-15, and combinations of these supports; A method for producing the synthetic paraffinic kerosene according to claim 20.

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