Methods for converting carbon dioxide and electricity into fuels and chemicals

Abstract

The present invention describes methods, systems, and catalysts for the conversion of carbon dioxide, water, and electricity into low- or zero-carbon, high-quality fuels and chemicals. In one aspect, the present invention provides an integrated process for converting a feed stream comprising carbon dioxide into a product stream comprising hydrocarbons between 5 and 24 carbon atoms in length.

Description

[Technical field]

[0001] The present invention describes a catalytic process for the conversion of carbon dioxide, water and electricity (ideally renewable or low carbon electricity) into low or zero carbon, high quality fuels and chemicals. The conversion efficiency of the process is improved by incorporating several innovations that have not been described in the current technology. The first improvement is an autothermal reforming (ATR) process that converts tail gas (and potentially other hydrocarbon feedstocks) from the fuel / chemical production stage and oxygen from the electrolysis process into additional syngas. The second improvement is the use of heat energy from the ATR process for the (CO2)RWGS (hydrogenation) catalytic step. The third improvement is the separation and conversion of CO2 from the ATR process into additional syngas using a CO2 hydrogenation catalyst. Fourth, the use of a proprietary Reverse Water Gas Shift (RWGS) catalyst, reactor and method for converting CO2 and hydrogen into syngas, preferably operating the RWGS process at pressures approaching those of the fuel / chemical production process that converts the syngas into fuels or chemicals. Most preferably, these fuels or chemicals are predominantly C5-C 24 The hydrocarbon liquid is a paraffinic or olefinic liquid within the range of [Background technology]

[0002] Carbon dioxide is produced by many industrial and biological processes. It is usually emitted into the atmosphere. However, since carbon dioxide is recognized as a significant greenhouse gas, it is necessary to reduce the carbon dioxide emissions from these processes. This carbon dioxide can be used to enhance the recovery of oil and gas from oil wells in limited cases, but most of the captured carbon dioxide is released into the atmosphere. The preferred way to deal with carbon dioxide is to efficiently capture and utilize it, converting it into useful products such as fuels (e.g., diesel fuel, gasoline, gasoline blendstocks, jet fuel, kerosene, etc.) and chemicals (e.g., solvents, olefins, alcohols, aromatics, lubricants, waxes, ammonia, methanol, etc.) to replace fuels and resources produced from fossil resources such as petroleum and natural gas, thereby reducing the total net emissions of carbon dioxide into the atmosphere. This is what is meant by low-carbon, ultra-low-carbon or zero-carbon fuels and chemicals.

[0003] Carbon dioxide can be obtained from several sources. Industrial manufacturing plants that produce ammonia for fertilizers produce large amounts of carbon dioxide. Ethanol plants that convert corn or wheat into ethanol produce large amounts of carbon dioxide. Power plants that generate electricity from various natural resources (e.g., natural gas, coal, other natural resources) produce large amounts of carbon dioxide. For example, nylon production plants, ethylene production plants, other chemical plants, etc. produce large amounts of carbon dioxide. Some natural gas processing plants produce CO2 as part of the process of refining natural gas to meet pipeline specifications. CO2 capture for the uses described herein often requires separation of CO2 from the exhaust gas stream or another stream in which CO2 is not the predominant component. Some CO2 sources are already relatively pure and can be used in the processes described herein with only minor processing, which may include gas compression. Some processes may require alkylamines or other methods to be used to remove carbon dioxide from the exhaust gas steam. The alkylamines used in the methods may include monoethanolamine, diethanolamine, methyldiethanolamine, diisopropylamine, aminoethoxyethanol, or combinations thereof. Metal Organic Framework (MOF) materials have also been used as a means of capturing carbon dioxide from low-concentration streams, using chemisorption or physisorption to separate it. Other methods of obtaining high concentrations of carbon dioxide include chemical looping combustion, where a circulating metal oxide material captures the carbon dioxide produced during the combustion process. Carbon dioxide can also be captured from the atmosphere in so-called direct air capture (DAC).

[0004] Renewable sources of hydrogen (H2) can be produced from water by electrolysis.

[0005] [ka]

[0006] The reaction uses electricity to split water into hydrogen and oxygen. An electrolyser consists of an anode and a cathode separated by an electrolyte. Electrolysers function in slightly different ways, mainly due to the different electrolyte materials they contain.

[0007] However, each electrolysis technology has a theoretical minimum electrical energy input of 39.4 kWh / kgH2 (HHV of hydrogen) when water is fed to the system at normal pressure and temperature and all energy input is provided in the form of electricity. If adequate thermal energy is provided to the system, the required electrical energy input can be less than 39.4 kWh / kgH2. In addition to electrolysis, significant current research is investigating the use of light energy and photocatalysis to split water into hydrogen and oxygen. (Acar et al, Int. J. Energy Res. 2016; 40:1449-1473).

[0008] One reaction being considered for the utilization of carbon dioxide is the reverse water gas shift (RWGS) reaction.

[0009] [ka]

[0010] This reaction converts carbon dioxide and hydrogen to carbon monoxide and water. The reaction is endothermic at room temperature and requires heat to proceed, and requires elevated temperatures and good catalysts to convert carbon dioxide significantly. Many catalysts have been disclosed for the RWGS reaction. The main catalysts previously investigated were Cu or Pt or Rh dispersed on metal oxide supports. (Daza & Kuhn, RSC Adv. 2016, 6, 49675-49691).

[0011] With CO (carbon monoxide) from the reverse water gas shift reaction and hydrogen from the electrolysis of water, useful products can be obtained via catalytic hydrogenation of carbon monoxide to hydrocarbons. The mixture of H2 and CO is called synthesis gas or syngas. Syngas can be used as a feedstock to produce a wide range of chemical products, including liquid fuels, alcohols, acetic acid, dimethyl ether, methanol, ammonia, and many other chemical products.

[0012] Catalytic hydrogenation of carbon monoxide to produce heavy hydrocarbons (C 100 The production of light gases, liquids and waxes, plus oxygenated hydrocarbons (up to 10 ... 25 These FT waxes are then hydrocracked and / or further processed to produce diesel, naphtha and other fractions. Light hydrocarbons are also produced during the hydrocracking process and may require further upgrading to produce viable products. The catalysts commonly used for FT are either cobalt (Co) or iron (Fe) based catalysts, which are also active in the water gas shift (WGS) reaction, which converts the feed carbon monoxide to carbon dioxide. For more details on the current state of the art in Fischer-Tropsch see (SSAil, S.Dasappa / Renewable and Sustainable Energy Reviews 58(2016) 267-286). Summary of the Invention [Problem to be solved by the invention]

[0013] To date, efficient and economical methods, systems and catalysts for the conversion of carbon dioxide into useful fuels and chemicals have not been developed. Better methods, systems and catalysts are needed. [Means for solving the problem]

[0014] The present invention relates to a method for converting carbon dioxide, water and electricity into useful chemicals and fuels. The method involves converting water to hydrogen in an efficient electrolysis unit that uses electricity, ideally renewable electricity, as the energy source. Carbon dioxide and hydrogen are reacted to carbon monoxide and water in a reverse water gas shift (RWGS) reactor, with renewable electricity as the heat source for the reaction. The catalyst used in the reactor is a novel solid solution catalyst. The carbon monoxide and additional hydrogen produced are reacted to fuels and chemicals in a liquid fuel production reactor that uses a novel catalyst to directly produce fuels and chemicals. As described herein, various fuels or chemicals can be produced from the syngas. Preferably, the products produced are hydrocarbons with 4 to 24 carbon atoms in length. The incorporation of several innovative steps in the method improves the conversion efficiency of the method and reduces capital costs. The first improvement is an autothermal reforming (ATR) process that converts tail gas (and potentially other hydrocarbon feedstocks) from the fuel / chemical production process and oxygen from the electrolysis process into additional syngas. The second improvement is to utilize heat energy from the ATR process for a CO2 hydrogenation catalyst step. The third improvement is to convert CO2 from the ATR process into additional syngas using a CO2 hydrogenation catalyst. The fourth improvement is to use a unique reverse water gas shift (RWGS) catalyst and method to convert CO2 and hydrogen into syngas, preferably operating the RWGS step at pressures close to those of the fuel / chemical production process, and preferably operating the syngas at a pressure that is mostly C5-C. 24 to convert the hydrocarbons into liquids within the range of [Brief description of the drawings]

[0015] 1-3 show an integrated, highly efficient process for converting carbon dioxide, water, and renewable electricity into renewable fuels and chemicals.

[0016] [Figure 1] Figure 1 shows a portion of the overall process flow diagram for converting H2 and CO2 to fuels and chemicals. Specifically, Figure 1 shows a reverse water gas shift reactor system for producing CO from CO2.

[0017] [Diagram 2] A portion of the overall process flow diagram for the conversion of H2 and CO2 to fuels and chemicals is shown in Figure 2. Specifically, Figure 2 shows a liquid fuel production system that reacts CO with H2 to produce long chain hydrocarbons that can be used as fuels or chemicals, and an ATR for tail gas conversion.

[0018] [Diagram 3] Figure 3 shows a portion of an overall process flow diagram for converting H2 and CO2 into fuels and chemicals. Specifically, Figure 3 shows an electrolysis unit for producing hydrogen and oxygen from water and low carbon electricity. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0019] FIG. 1 shows several subsystems: 1) an electrolysis system that produces hydrogen from water; 2) a reverse water gas shift (RWGS) reactor system that produces CO from CO; 3) an auto thermal reformer (ATR) section; and 4) a syngas compression system.

[0020] Water is fed into an electrolysis system. Renewable electricity is used to power the electrolysis system. Hydrogen can be produced by electrolysis of water.

[0021] [ka]

[0022] Electrolysers consist of an anode and a cathode separated by an electrolyte. Slightly different processes result in different electrolysers functioning differently. A variety of electrolyser designs using different electrolysis techniques can be used, including alkaline, membrane and high temperature electrolysis. Alkaline electrolysis is preferred as large scale processes above 1 MW are commercially feasible. A variety of electrolytes can be used, including KOH or NaOH liquids with or without activating compounds. Activating compounds can be added to the electrolyte to improve electrolyte stability. Many of the ionic activators for the hydrogen evolution reaction are ethylenediamine(ene)-based metal chloride complexes ([M(en)3]Cl). x , M 1 / 4 The cathode is composed of a tungsten carbide (Co, Ni, etc.) and Na2MoO4 or Na2WO4. A variety of electrocatalysts are available for the electrodes, including different combinations of metals and oxides such as Raney-nickel-aluminum, which can be enhanced by adding cobalt or molybdenum to the alloy. Several combinations of transition metals, e.g. Pt2Mo, Hf2Fe, and TiPt, have been used as cathode materials and have shown significantly higher electrocatalytic activity than state-of-the-art electrodes.

[0023] Water at the cathode combines with electrons from the external circuit to form hydrogen gas and negatively charged oxygen ions. The oxygen ions pass through a solid ceramic membrane and react at the anode to form oxygen gas and generate electrons for the external circuit. In this way, both hydrogen and oxygen gases are produced in the electrolyzer. In one embodiment, multiple electrolyzers are operated in parallel. No electrolyzer operates at 100% energy efficiency, and energy usage is important to the economic operation of the facility. Energy usage in the electrolyzer is desirably less than 200 megawatt hours (MWh) / metric ton (MT) of H2 produced, preferably less than 120 MWh / MT of H2 produced, and more preferably less than 60 MWh / MT of H2 produced. For alkaline electrolyzer embodiments, power usage will be greater than 39.4 MWh / MT of H2 produced. However, for high temperature electrolyzer embodiments, if waste heat is used to heat the electrolyzer above ambient temperature, power usage could potentially be less than 39.4 MWh / MT of H2 produced.

[0024] Carbon dioxide can come from many industrial and natural sources. Carbon dioxide is often found in natural gas deposits. Carbon dioxide is emitted from many biological processes, such as anaerobic digestion. Many other processes (e.g., power plants, cement plants, ethanol production, oil refineries, chemical plants, etc.) produce carbon dioxide that is normally emitted into the atmosphere. Carbon dioxide is also found in the atmosphere. Carbon dioxide can be captured from these biological, industrial and atmospheric processes by many known techniques and used as a feedstock for the present invention.

[0025] Zero carbon, low carbon or ultra low carbon fuels and chemicals require that no fossil fuels are burned in the fuel and chemical production process, which means that heating of the feed to the integrated process needs to be by indirect means (cross exchangers) or using electrical heating where the electricity comes from zero carbon or renewable sources such as wind, solar, geothermal or nuclear.

[0026] In Figure 1, hydrogen stream 1 and carbon dioxide stream 2 are combined to form stream 3. The H2 / CO2 ratio is between 2.0 mol / mol and 4.0 mol / mol, more preferably between 3.0 and 4.0 mol / mol. The combined reverse water gas shift (RWGS) feed is heated to 900°F by indirect heat exchange. (482℃) It is important that this initial temperature increase is done without using direct combustion of a carbon-containing gas to provide the heat, as using direct combustion of a carbon-containing gas would mean that carbon dioxide is being produced, which would negate the benefits of converting the carbon dioxide into useful fuels and chemicals.

[0027] The RWGS feed gas containing the mixed hydrogen and carbon dioxide is heated at least partially to 1,500° F. in a preheater outside the main reactor vessel. (816℃) Higher than 1,600°F (871℃) The preheater is shown in FIG. 1 as step 4. Step 4 of the preheater uses electrical heating and indirect heat exchange to increase the temperature of the feed gas to 1,500° F. (816℃) to temperatures above 1,600°F (871℃)The gas is heated to a temperature higher than 1000° C. There are many ways to electrically heat the feed gas. One way is by electrical heating in an electrically heated radiant furnace. In this embodiment, at least a portion of the feed gas passes through heating coils in the furnace. In the furnace, the gas is heated by some convective heat transfer, either by surrounding the heating coils with radiant electric heating elements or by passing the gas directly over the heating elements. The electric heating elements can be made from a number of materials. The heating elements can be nickel chromium alloys. These elements can be wound strips or wires, or cast in a zigzag shape. The elements are usually backed by an insulated steel shell, with ceramic fibers commonly used for insulation. The radiant elements can be divided into multiple sections to control the heating pattern. Multiple coils and multiple sections may be required to provide heat to the feed gas and produce a heated feed gas. Radiant furnaces require proper design of heating elements and fluid coils to ensure good view factors and good heat transfer. It is desirable to minimize the power usage of the radiant furnace. The power usage of the radiant furnace is less than 0.5 MWh (megawatt-hour) of power / metric ton (MT) of CO2 in the feed gas, more preferably less than 0.40 MWh / MT of CO2, and even more preferably less than 0.20 MWh / MT of CO2.

[0028] The heated RWGS feed gas stream 5 is then fed to the RWGS main reactor vessel step 6. There are two possible embodiments of the RWGS main reactor vessel. In the first embodiment, the RWGS main reactor vessel is adiabatic or nearly adiabatic and designed to minimize heat loss, but no heat is added to the main reactor vessel and the temperature in the main reactor vessel decreases from the inlet to the outlet of the reactor. In the second embodiment, the RWGS main reactor vessel is designed similarly, but additional heat is added to the vessel to maintain an isothermal or nearly isothermal temperature distribution in the vessel. The RWGS main reactor vessel is a reactor with a length that is longer than its diameter. The inlet to the main reactor vessel is smaller than the overall diameter of the vessel. The main reactor vessel is a steel vessel. The steel vessel is internally insulated to limit heat loss. Various insulation materials may be used to limit heat loss to the environment, including poured or castable refractory lining or insulating bricks.

[0029] Inside the RWGS main reactor vessel is a bed of catalyst. The catalyst can be in the form of granules, pellets, spheres, trilobes, quadra-lobes, monoliths or any other designed shape to minimize the pressure drop across the reactor. Ideally, the shape and size of the catalyst particles are controlled to ensure that the pressure drop across the reactor is less than 100 pounds per square inch (psi) [345 kPa], more preferably less than 20 psi (139 kPa). The size of the catalyst form can have a characteristic dimension between 1 mm and 10 mm. The catalyst particles can be as small as 40 m. 2 / g, more preferably 80 m 2 / g, preferably with an internal surface area of ​​100 m 2The structured material is a porous material with a preferred surface area of ​​10000000000000 / g. Several catalytic materials are expected to be able to catalyze the RWGS reaction. The main catalysts previously investigated for RWGS were Cu or Pt or Rh dispersed on metal oxide supports. (Daza & Kuhn, RSC Adv. 2016, 6, 49675-49691). The preferred catalysts have been found to be solid solution catalysts with transition metals on metal-alumina spinels.

[0030] The RWGS catalyst used in the present method is a versatile, high performance solid solution catalyst that can efficiently perform the RWGS reaction. This robust solid solution transition metal catalyst has high thermal stability up to 1,100°C, does not form carbon (coking), and has good tolerance to contaminants that may be present in the captured CO2 stream. The catalyst exhibits high activity at low transition metal concentrations (5-20 wt%) compared to other catalysts that require at least 30 wt% transition metal. Moreover, it does not require the use of expensive precious metals to improve the catalytic performance. The manufacturing process for the RWGS catalyst is also important in that it produces a catalyst that forms a unique solid solution phase, a bimetallic crystalline phase, that does not segregate the metallic phase. This unique chemical structure improves the resistance to coking compared to conventional metal supported catalysts. It also improves the tolerance to poisons such as sulfur and ammonia. In addition, the catalyst provides improved catalytic activity at a small surface area compared to monometallic atomically segregated catalytic phases such as Ni on alumina. The catalyst does not require alkali promotion to suppress carbon deposition.

[0031] Here, the pressure differential between the RWGS step and the hydrocarbon synthesis or liquid fuel production (LFP) step is within 200 psi of each other, more preferably within 100 psi of each other, or even more preferably within 50 psi of each other. By operating the two processes at pressures close to each other, the compression required for the syngas stream can be limited.

[0032] In the RWGS main reactor, the conversion of carbon dioxide to carbon monoxide per pass is typically between 60 and 90 mole percent, more preferably between 70 and 85 mole percent. When an adiabatic reactor embodiment is used, the temperature in the RWGS main reactor decreases from the inlet to the outlet. The RWGS main reactor outlet temperature is typically 100° F. lower than the main reactor inlet temperature. (56℃) to 200°F (111℃) and more preferably 105° C. lower than the inlet temperature of the main reactor. °F(58℃) to 160°F (89℃) The Weight Hourly Space Velocity (WHSV) for RWGS is the mass flow rate of RWGS reactants (H2+CO2) per hour divided by the mass of catalyst in the bed of the RWGS main reactor, and is expressed as WHSV in the range of 1,000 to 50,000 hr -1 Preferably, the operating time is between 5,000 and 30,000 hours. -1 It is between.

[0033] Gas exiting the RWGS main reactor is RWGS product gas stream 7. The RWGS product gas includes carbon monoxide (CO), hydrogen (H2), unreacted carbon dioxide (CO2), and water (H2O). In addition, the RWGS product gas may also include small amounts of methane (CH4) produced by side reactions in the main reactor.

[0034] At this point in the process, the RWGS product gas can be used in a variety of ways. As shown in Figure 2, the product gas can be cooled and compressed and used in downstream processes to produce fuels and chemicals. The RWGS product gas can also be cooled and compressed in step 8 and sent back to the preheater step 4 and fed back to the main reactor step 5. The RWGS product gas can also be reheated in a second electric preheater step 9 and sent to a second reactor step 10 for additional conversion of CO2 to CO.

[0035] FIG. 2 shows the hydrocarbon synthesis step, also known as the Liquid Fuel Production (LFP) step. The LFP reactor converts CO and H2 into long chain hydrocarbons that can be used as liquid fuels and chemicals. The reactor uses a unique catalyst to produce liquid fuel range hydrocarbons from the syngas. Syngas stream 12 from syngas cooling and condensation step 22 in FIG. 2 (and compression step 11 in FIG. 1, if necessary) is combined with tail gas stream 13 to produce LFP reactor feed stream 14. The LFP reactor feed includes hydrogen and carbon monoxide. Ideally, the ratio of hydrogen to carbon monoxide in the stream is between 1.9 and 2.2 mol / mol. The LFP reactor step 15 is a multi-tubular fixed bed reactor system. Each tube in the LFP reactor can be between 13 mm and 26 mm in diameter. The length of the reactor tube is generally greater than 6 mm, more preferably greater than 10 mm. LFP reactors are generally oriented vertically, with the feed to the LFP reactor entering the top of the LFP reactor. However, in some circumstances the reactor can be oriented horizontally, and in situations where height is limited it may be advantageous to arrange the reactor at an incline. The majority of the length of the LFP reactor tube is filled with LFP catalyst. To aid in the distribution of the LFP reactor feed into the LFP reactor tube, the LFP catalyst may also be mixed with a diluent, e.g. silica or alumina. The chemical reactions occurring in the LFP reactor convert most hydrocarbons, with carbon numbers between 5 and 24 in length (C5-C 24LFP product gases are produced that include carbon dioxide (Hydrocarbon) products and water, although there are some hydrocarbons outside of this range. It is important that the LFP reactor does not generate significant amounts of carbon dioxide. It is desirable that less than 2% of the carbon monoxide in the LFP reactor feed is converted to carbon dioxide in the LFP reactor. It is also important that only a limited amount of carbon monoxide in the LFP reactor feed is converted to hydrocarbons having carbon numbers greater than 24. It is preferred that less than 25% by weight of the LFP product hydrocarbon fraction has a carbon number greater than 24. More preferably, it is preferred that less than 10% by weight of the LFP product hydrocarbon fraction has a carbon number greater than 24. Even more preferably, it is preferred that less than 4% by weight of the LFP product hydrocarbon fraction has a carbon number greater than 24. Even more preferably, it is preferred that less than 1% by weight of the LFP product hydrocarbon fraction has a carbon number greater than 24. As discussed above, the Fischer-Tropsch (FT) process generally produces hydrocarbon products having lengths between 1 and 125 carbon atoms. The LFP catalysts used do not produce heavy hydrocarbons in the same yield as other catalysts used in the FT process. In some embodiments of the invention, the LFP catalyst has only marginal activity for the conversion of carbon monoxide to carbon dioxide via the water gas shift reaction. In some embodiments of the invention, the water gas shift conversion of carbon monoxide to carbon dioxide is less than 5% of the carbon monoxide in the feed. In some embodiments, the LFP catalyst comprises cobalt as an active metal. In some embodiments, the LFP catalyst comprises iron as an active metal. In some embodiments, the LFP catalyst comprises a combination of iron and cobalt as active metals. The LFP catalyst is supported on a metal oxide support selected from the group of alumina, silica, titania, activated carbon, carbon nanotubes, zeolites, or other support materials, or mixtures thereof, of sufficient size, shape, pore size, surface area, crush strength, and effective pellet radius.The catalyst can have a variety of lobed supports with either three, four or five lobes, with two or more lobes longer than the other two shorter lobes, and both of the longer lobes being symmetrical. The distance from the mid-point of the support or from the mid-point of each lobe is called the effective pellet radius and is expressed as C5 to C6. 24 It is an important parameter for achieving the desired selectivity to hydrocarbons. Promoters for the LFP catalyst may include one of nickel, cerium, lanthanum, platinum, ruthenium, rhenium, gold or rhodium. The promoters for the LFP catalyst are less than 1 wt. % of the total catalyst, preferably less than 0.5 wt. %, and even more preferably less than 0.1 wt. %.

[0036] The LFP catalyst support has a pore size greater than 8 nanometers (nm), an average effective pellet radius less than 600 microns, a crush strength greater than 3 lbs / mm, and a surface area of ​​less than 100 m 2 / g. After metal impregnation, the catalyst has a metal dispersion of about 4%. 24 Several types of supports have been found to maximize the yield of hydrocarbons, including alumina / silica combinations, activated carbon, alumina, carbon nanotubes and / or zeolite-based supports.

[0037] LFP fixed bed reactors are classified into C5-C 24 The LFP reactor in one embodiment is operated at a pressure between 150 and 450 psi. °F(177℃) to 460°F (238℃) Operates in a temperature range of 410°F, more typically about (210℃)The reaction is exothermic. The reactor tube bundle is encased in a heat exchanger where the reactor temperature is maintained inside the LFP reactor tubes by boiling steam on the outside of the LFP reactor tubes. Since the steam temperature is lower than the LFP reactor temperature, heat flows from the LFP reactor tubes to the cooler steam. The steam temperature is maintained by maintaining the steam pressure. The steam is generally saturated steam. In alternative embodiments, the catalytic reactor can be a slurry reactor, a microchannel reactor, a fluidized bed reactor or other type of reactor known in the art.

[0038] The CO conversion in the LFP reactor is maintained at 30 to 80 mol% CO conversion per pass. The CO can be recycled for additional conversion or sent downstream to additional LFP reactors. Carbon selectivity to CO2 is minimized to less than 4% of the converted CO, more preferably less than 1%. C5-C 24 The carbon selectivity to hydrocarbons is between 60 and 90%. The LFP reactor product gas stream 16 contains the desired C5-C condensed as liquid fuel and water. 24 It contains hydrocarbons, as well as unreacted carbon monoxide, hydrogen, small amounts of C1-C4 hydrocarbons, and small amounts of C 24+ Included in the feed stream is a hydrocarbon stream 24. Desired products are separated from the stream by cooling, condensation and / or distillation of the products, or other acceptable means, step 17. Unreacted carbon monoxide, hydrogen, and C1-C4 hydrocarbons, stream 18, become part of the feed to the autothermal reformer, step 19.

[0039] FIG. 2 also shows the autothermal reformer (ATR) step 20 portion of the method. In the autothermal reformer (ATR), the ATR's hydrocarbon feed includes carbon monoxide, hydrogen, and C1-C4 hydrocarbons. Autothermal reforming of methane (C1)-based natural gas to carbon monoxide and hydrogen has been practiced commercially for many years. See K. Aasberg-Petersen et al., Journal of Natural Gas Science and Engineering 3 (2011) 423-459.

[0040] In one embodiment of the invention, the ATR hydrocarbon feed includes natural gas steam 20 and a stream of unreacted carbon monoxide, hydrogen, and C1-C4 hydrocarbons 18. Natural gas includes methane and may include light hydrocarbons and carbon dioxide. In this embodiment, the fuels and chemicals produced may not be zero carbon fuels, but still have improved carbon intensity over conventional fuels and chemicals. The natural gas in the ATR feed is converted to syngas (containing a large percentage of hydrogen). This reduces the amount of water that needs to be electrolyzed to produce hydrogen, and can reduce the size of the electrolyzer. This embodiment may be more economically viable for producing low carbon fuels and chemicals. The ratio of natural gas to LFP unreacted carbon monoxide, hydrogen, and C1-C4 hydrocarbons in the ATR hydrocarbon feed is preferably less than 2.0 kg / kg. More preferably, the ratio is less than 1.25 kg / kg.

[0041] The ATR used in the present invention produces products rich in carbon monoxide and less than 10 mol% carbon dioxide in the product gas. The ATR oxidant feed contains steam and oxygen, which is produced by electrolysis of water. The ATR oxidant feed and the ATR hydrocarbon feed are preheated and then reacted in the ATR burner, where the oxidant and hydrocarbons are partially oxidized at temperatures above 2,000°C. The ATR reactor can be divided into three sections. In the combustion section (or burner), at least a portion of the ATR hydrocarbon feedstock is completely combusted to water and carbon dioxide. In the thermal section, thermal reactions take place. In the thermal section, further conversion takes place by homogeneous gas phase reactions. These reactions are slower than combustion reactions such as the oxidation of CO and pyrolysis reactions involving higher hydrocarbons. The main overall reactions in the thermal section are homogeneous gas phase steam reforming and shift reactions of hydrocarbons. In the catalytic zone, the final conversion of the hydrocarbons takes place by heterogeneous catalytic reactions, including steam reforming of methane and water gas shift reaction. As a result, the ATR product gas has a composition close to the predicted thermodynamic equilibrium composition. The actual ATR product gas composition is the same as the thermodynamic equilibrium composition with a difference of less than 70°C. This is the so-called equilibrium approach temperature. To minimize the amount of CO2 produced in the ATR, the amount of steam in the ATR oxidant feed should be as low as possible while still obtaining an ATR product gas close to the predicted equilibrium composition and with low soot. Typically, the ratio of the total steam to carbon (mol / mol) in the ATR feed combination (oxidant + hydrocarbon) is desired to be between 0.4 and 1.0, and optimally about 0.6.

[0042] The ATR product leaves the catalytic section of the ATR at a temperature above 800° C. The ATR product step 21 is cooled to a lower temperature through a waste heat boiler step 22 where heat is transferred to generate steam that can be used to generate electricity, similar to the low pressure steam produced by the LFP reactor.

[0043] ATR catalysts suitable for the reaction in the catalytic zone are typically nickel-based. The novel solid solution catalysts described above can be used as ATR catalysts. Other suitable ATR catalysts are nickel on alpha-alumina or magnesium alumina spinels (MgAl2O4) with or without precious metal promoters, including gold, platinum, rhenium, or ruthenium. Spinels have higher melting points, higher thermal strength, and stability than alumina-based catalysts.

[0044] The ATR product stream 23 can be combined with the RWGS product and used as the feed for the LFP reactor, resulting in the conversion of C5-C 24 It can be converted to hydrocarbon products at high utilization rates.

[0045] In some embodiments, the LFP product gas is not suitable as a direct feed to the ATR and must be pre-reformed. In those cases, the LFP product gas containing unreacted carbon monoxide, hydrogen, C1-C4 hydrocarbons and CO2 constitutes the hydrocarbon feed gas of the pre-reformer. The higher the amount of higher hydrocarbons and carbon oxides in this stream, the more likely it is that a pre-reformer should be used instead of using it directly as the hydrocarbon feed to the ATR. The pre-reformer is generally an adiabatic reactor. The adiabatic pre-reformer converts the higher hydrocarbons in the pre-reformer feed to a mixture of methane, steam, carbon oxides and hydrogen, which in turn makes it suitable as the hydrocarbon feed to the ATR. One advantage of using a pre-reformer is that the ATR hydrocarbon feed can be preheated at a higher temperature, which allows less oxygen to be used in the ATR. As a result, such an integrated process converts carbon dioxide into C5-C suitable for use as fuels or chemicals. 24It gives high conversion to hydrocarbon products.

[0046] Specific Method Embodiments

[0047] Below are specific embodiments of processes for converting carbon dioxide, water and electricity into low or zero carbon, high quality fuels and chemicals.

[0048] 1. Water is fed to an electrolysis system powered by renewable electricity. Carbon dioxide is captured from a source. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is typically heated and then fed into a RWGS reactor vessel containing a solid solution catalyst. The RWGS reactor converts the feedstock to RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide and water. The RWGS product gas is cooled, compressed and fed to a Liquid Fuel Production (LFP) system or what is otherwise called the hydrocarbon synthesis step. The LFP system converts the RWGS product gas (either refined or raw) into hydrocarbon products, with more than 50% of the products being C5 to C6. 24 wherein the pressure differential between the RWGS step and the hydrocarbon synthesis step is within 200 psi of each other, more preferably within 100 psi of each other, or even more preferably within 50 psi of each other.

[0049] 2. Water is fed to an electrolysis system powered by renewable electricity. Carbon dioxide is recovered from a source. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is typically heated and then fed into a RWGS reactor vessel containing a nickel-based solid solution catalyst. The RWGS reactor converts the feedstock to RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide and water. One or more of C1-C4 hydrocarbons, carbon monoxide and hydrogen are fed into an autothermal reformer (ATR) to provide an ATR product stream. The RWGS product gas (either refined or unrefined) is combined with the ATR product stream and fed into a liquid fuel production (LFP) system. The LFP system converts the combined RWGS and ATR products into hydrocarbon products, with more than 50% of the products being C5 to C6 hydrocarbons. 24 It is a hydrocarbon.

[0050] 3. Water is fed to an electrolysis system powered by renewable electricity. Carbon dioxide is captured from a source. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is typically heated and then fed into a RWGS reactor vessel containing a nickel-based solid solution catalyst. The RWGS reactor converts the feedstock into a RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide and water. One or more of the C1-C4 hydrocarbons, carbon monoxide and hydrogen are fed into an autothermal reformer (ATR) containing a nickel solid solution catalyst to provide an ATR product stream. The RWGS product gas (either refined or raw) is combined with the ATR product stream (either refined or raw) and fed into a liquid fuel production (LFP) system containing a Fischer-Tropsch catalyst or other catalyst or catalysts to produce hydrocarbon products from the syngas. The LFP system converts the combined RWGS and ATR products into hydrocarbon products, with more than 50% of the products being C5 to C6. 24 It is a hydrocarbon.

[0051] 4. The water is fed to an electrolysis system powered by renewable electricity. Carbon dioxide is captured from a source, which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or rice or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion, or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is typically heated and then fed into a RWGS reactor vessel containing a nickel solid solution catalyst. The RWGS reactor converts the feedstock to RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide and water. The RWGS product gas is cooled, compressed, and fed to a Liquid Fuel Production (LFP) system containing a catalyst or other catalyst that produces hydrocarbons from syngas. The LFP system converts the RWGS product gas (either refined or unrefined) to hydrocarbon products, with more than 50% of the products being C5 to C6. 24 It is a hydrocarbon.

[0052] 5. Water is fed to an electrolysis system powered by renewable electricity. Carbon dioxide is captured from a source, which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or rice or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion, or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (reverse water gas shift feedstock or "RWGS" feedstock) which is typically heated and then fed into a RWGS reactor containing a nickel solid solution catalyst. C1-C 4+ One or more of a hydrocarbon (e.g., methane), carbon monoxide, and hydrogen are fed into an autothermal reformer (ATR) containing a nickel solid solution catalyst to provide an ATR product stream. A product gas (either purified or raw) of the RWGS is combined with a product stream (either purified or raw) of the ATR and fed into a catalyst system to produce methanol.

[0053] 6. Water is fed to an electrolysis system powered by renewable electricity. Carbon dioxide is captured from a source, which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion, or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is typically heated and then fed into a RWGS reactor vessel containing a nickel solid solution catalyst. The RWGS reactor converts the feedstock to a RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide, and water. C1-C 4+ One or more of a hydrocarbon (e.g., methane), carbon monoxide, and hydrogen are fed into an autothermal reformer (ATR) containing a nickel solid solution catalyst to provide an ATR product stream. The RWGS product gas (either purified or raw) is combined with the ATR product stream (either purified or raw) and fed to a process to produce ammonia from syngas.

[0054] 7. The water is fed to an electrolysis system powered by renewable electricity, the electrolyser of which operates using alkaline, membrane or high temperature electrolysis, with the renewable electricity coming from wind, solar, geothermal or nuclear sources of renewable energy. Carbon dioxide is captured from a source, which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (reverse water gas shift feedstock or "RWGS" feedstock), which is typically heated and then fed into a RWGS reactor containing a nickel solid solution catalyst. The RWGS reactor converts the feedstock to a RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide and water. The RWGS product gas is cooled, compressed and fed into a liquid fuel production (LFP) system, which may contain a Fischer-Tropsch catalyst, to produce C5-C 100+The resulting mixture produces primarily waxes with hydrocarbons in the range of

[0055] 8. Water is fed to an electrolysis system powered by renewable electricity, whose electrolysers operate using alkaline, membrane or high temperature electrolysis, with the renewable electricity coming from wind, solar, geothermal or nuclear sources of renewable energy. Carbon dioxide is captured from a source that can be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (reverse water gas shift feedstock or "RWGS" feedstock) that is typically heated and then fed into a RWGS reactor containing a nickel solid solution catalyst. The RWGS reactor converts the feedstock to a RWGS product gas that contains carbon monoxide, hydrogen, unreacted carbon dioxide and water. One or more of C1-C4 hydrocarbons (e.g., methane), carbon monoxide, and hydrogen are fed into an autothermal reformer (ATR) containing a nickel solid solution catalyst to provide an ATR product stream. RWGS product gas (either purified or raw) is combined with the ATR product stream (either purified or raw) and fed to a process to produce ammonia from syngas.

[0056] 9. Water is fed to an electrolysis system powered by renewable electricity, whose electrolysers operate using alkaline, membrane or high temperature electrolysis, with the renewable electricity coming from wind, solar, geothermal or nuclear sources of renewable energy. Carbon dioxide is captured from a source that can be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (reverse water gas shift feedstock or "RWGS" feedstock), which is typically heated and then fed into a RWGS reactor vessel containing a solid solution catalyst containing transition metals. The RWGS reactor converts the feedstock into a RWGS product gas that contains carbon monoxide, hydrogen, unreacted carbon dioxide and water. One or more of C1-C4 hydrocarbons (e.g., methane), carbon monoxide, and hydrogen are fed into an autothermal reformer (ATR) containing a solid solution catalyst to provide an ATR product stream. The RWGS product gas (either refined or unrefined) is combined with the ATR product stream (either refined or unrefined) and fed into a liquid fuel production (LFP) system containing a catalyst to produce hydrocarbons from the syngas. The LFP system converts the combined RWGS and ATR products into hydrocarbon products, with more than 70% of the products being C5 to C6. 24 It is a hydrocarbon.

[0057] 10. Water is fed to a renewable electricity-powered electrolysis system, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear power as renewable or low carbon energy sources. Carbon dioxide is captured from a source, which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (reverse water gas shift feedstock or "RWGS" feedstock) which is heated to 1,400°F. (760℃) The feedstock is heated to an inlet temperature above 1000° C., which is not provided by direct combustion of a carbon-containing gas, and then fed into a RWGS reactor vessel containing a nickel solid solution catalyst. The RWGS reactor converts the feedstock into a RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide and water. The RWGS product gas is cooled and compressed to produce ammonia, methanol or liquid hydrocarbons.

[0058] 11. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear power as renewable or low carbon energy sources. Carbon dioxide is captured from a source, which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,000°F. (538℃)The feedstock is heated to an inlet temperature above 100° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into a RWGS reactor vessel containing a nickel solid solution catalyst. The RWGS reactor converts the feedstock into a RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide and water. One or more of the C1-C4 hydrocarbons (e.g., methane), carbon monoxide and hydrogen are fed into an autothermal reformer (ATR) containing a nickel solid solution catalyst to provide an ATR product stream. The RWGS product gas (either refined or raw) is combined with the ATR product stream (either refined or raw) and fed into a liquid fuel production (LFP) system containing a fuel production catalyst using a combination of nickel and cobalt. The LFP system converts the combined RWGS and ATR products into hydrocarbon products, of which more than 50% are C5 to C6 hydrocarbons. 24 It is a hydrocarbon.

[0059] 12. Water is fed to a renewable electricity-powered electrolysis system, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear power as a renewable or low carbon energy source. Carbon dioxide is captured from a source, which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃)The feedstock is heated to an inlet temperature above 1000° C., which is not provided by direct combustion of a carbon-containing gas, and then fed into a RWGS reactor vessel containing a transition metal based solid solution catalyst. The RWGS reactor converts the feedstock into a RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide and water. The RWGS product gas is cooled, compressed and fed into a chemical production facility.

[0060] 13. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear as a renewable energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃) The feedstock is heated to an inlet temperature above 100° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into a RWGS reactor vessel containing a nickel solid solution catalyst. The RWGS reactor converts the feedstock into a RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide, and water. One or more of the C1-C4 hydrocarbons (e.g., methane), carbon monoxide, and hydrogen are fed into an autothermal reformer (ATR) containing a nickel solid solution catalyst to provide an ATR product stream. The RWGS product gas (either refined or unrefined) is combined with the ATR product stream (either refined or unrefined) and fed into a system using a Fischer-Tropsch catalyst to produce higher hydrocarbon waxes as a primary product.

[0061] 14. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear as a renewable energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,200°F using any type of electric heating element that results in power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (649℃) The feedstock is heated to an inlet temperature above 100° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor vessel containing a nickel solid solution catalyst. The RWGS reactor converts the feedstock into a RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide and water. The RWGS product gas is cooled, compressed and fed into a Liquid Fuel Production (LFP) system containing a Fischer-Tropsch catalyst or other catalyst that produces hydrocarbons from the syngas. The LFP system converts the RWGS product gas (either refined or unrefined) into hydrocarbon products, of which more than 50% are C4 to C6. 24 It is a hydrocarbon.

[0062] 15. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear power as a renewable or low carbon energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃) The feedstock is heated to an inlet temperature above 100° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor vessel containing a solid solution catalyst. The RWGS reactor converts the feedstock into a RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide and water. One or more of C1-C3 hydrocarbons (e.g., methane), carbon monoxide and hydrogen are fed into an autothermal reformer (ATR). The RWGS product gas (either purified or raw) is combined with the ATR product stream (either purified or raw) and fed into a methanol production system.

[0063] 16. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear power as a renewable or low carbon energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃) The feedstock is heated to an inlet temperature above 100° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor vessel containing a nickel solid solution catalyst. The catalyst particles are controlled in shape and size to provide a pressure drop across the reactor of less than 50 pounds per square inch or less than 20 pounds per square inch. The RWGS reactor converts the feedstock into a RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide and water. The RWGS product gas is cooled, compressed and fed into a Liquid Fuel Production (LFP) system containing a catalyst that produces hydrocarbons from the syngas. The LFP system converts the RWGS product gas (either refined or unrefined) into hydrocarbon products of which greater than 50% is C5 to C6. 24 It is a hydrocarbon.

[0064] 17. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear power as a renewable or low carbon energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃) The feedstock is heated to an inlet temperature above 100° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor vessel containing a solid solution catalyst. The catalyst particles are controlled in shape and size to provide a pressure drop across the reactor of less than 50 pounds per square inch or less than 20 pounds per square inch. The RWGS reactor converts the feedstock into a RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide, and water. One or more of C1-C3 hydrocarbons (e.g., methane), carbon monoxide, and hydrogen are fed into an autothermal reformer (ATR) containing a nickel solid solution catalyst to provide an ATR product stream. The RWGS product gas (either refined or unrefined) is combined with the ATR product stream (either refined or unrefined) and fed into a syngas conversion system including either a methanol synthesis process, an ammonia production process, a Fischer-Tropsch process for the production of wax and other hydrocarbons, or the production of other chemicals or fuels.

[0065] 18. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear power as a renewable or low carbon energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃) The feedstock is heated to an inlet temperature above 100° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor vessel containing a nickel solid solution catalyst. The catalyst particles are controlled in shape and size to provide a pressure drop across the reactor of less than 100 pounds per square inch, or less than 50 pounds per square inch. The RWGS reactor converts the feedstock into a RWGS product gas that includes carbon monoxide, hydrogen, unreacted carbon dioxide, and water. The conversion of carbon dioxide to carbon monoxide per pass in the RWGS reactor vessel is between 30 and 90 mole %, or between 50 and 70 mole %, and the weight hourly space velocity for the RWGS is between 1,000 and 50,000 hr -1 Between 5,000 and 30,000 hours -1 The RWGS product gas is cooled, compressed and fed into a Liquid Fuel Production (LFP) system that contains a catalyst to produce hydrocarbons from the syngas. The LFP system converts the RWGS product gas (either refined or unrefined) into hydrocarbon products, with greater than 50% of the products being C5 to C6. 24 It is a hydrocarbon.

[0066] 19. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear power as a renewable or low carbon energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,000°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (538℃) The feedstock is heated to an inlet temperature above 1000° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor vessel containing a transition metal based solid solution catalyst. The catalyst particles are controlled in shape and size to provide a pressure drop across the reactor of less than 50 pounds per square inch, or less than 20 pounds per square inch. The RWGS reactor converts the feedstock into a RWGS product gas that includes carbon monoxide, hydrogen, unreacted carbon dioxide, and water. The conversion of carbon dioxide to carbon monoxide per pass in the RWGS reactor vessel is between 15 and 75 mole %, or between 30 and 70 mole %, and the weight hourly space velocity for the RWGS is between 1,000 and 50,000 hr -1 and more preferably between 5,000 and 30,000 hours -1One or more of the C1 to C4 hydrocarbons (e.g., methane), carbon monoxide, and hydrogen are fed into an autothermal reformer (ATR) containing a nickel solid solution catalyst to provide an ATR product stream. The RWGS product gas (either refined or raw) is combined with the ATR product stream (either refined or raw) and fed into a liquid fuel production (LFP) system containing a Fischer-Tropsch catalyst or other catalyst to produce hydrocarbons from the syngas. The LFP system converts the combined RWGS and ATR products into a hydrocarbon product, with more than 50% of the product being C4 to C6. 24 It is a hydrocarbon.

[0067] 20. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear power as a renewable or low carbon energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃)The feedstock is heated to an inlet temperature above 1000° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor containing a nickel solid solution catalyst. The catalyst particles are controlled in shape and size to provide a pressure drop across the reactor of less than 50 pounds per square inch, or less than 20 pounds per square inch. The RWGS reactor converts the feedstock into a RWGS product gas that includes carbon monoxide, hydrogen, unreacted carbon dioxide, and water. The conversion of carbon dioxide to carbon monoxide per pass in the RWGS reactor is between 15 and 75 mole %, or between 30 and 70 mole %, and the weight hourly space velocity for the RWGS is between 1,000 and 50,000 hr -1 and more preferably between 5,000 and 30,000 hours -1 The RWGS product gas is cooled and compressed and fed, along with the recycled syngas, into a Liquid Fuel Production (LFP) system containing a catalyst for producing hydrocarbons from the syngas. The reactor is a fixed bed reactor system having multiple tubes, each reactor tube having an I diameter between 13 mm and 26 mm and greater than 6 meters in length or greater than 10 meters in length.

[0068] 21. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear as a renewable energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃) The feedstock is heated to an inlet temperature greater than 100° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor containing a transition metal based solid solution catalyst. The RWGS reactor converts the feedstock into a RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide and water. The conversion of carbon dioxide to carbon monoxide per pass in the RWGS reactor is between 15 and 90 mole %, or between 30 and 70 mole %, and the weight hourly space velocity for the RWGS is between 1,000 and 50,000 hr -1 and more preferably between 5,000 and 30,000 hours -1One or more of C1-C4 hydrocarbons (e.g., methane), carbon monoxide, and hydrogen are fed into an autothermal reformer (ATR) containing a nickel solid solution catalyst to provide an ATR product stream. The RWGS product gas (either refined or raw) is combined with the ATR product stream (either refined or raw) and fed, along with recycled syngas, into a liquid fuel production (LFP) system containing a Fischer-Tropsch catalyst or other catalyst to produce hydrocarbons from the syngas. The reactor is a fixed bed reactor system having a plurality of tubes, each reactor tube having an I diameter between 13 mm and 26 mm and greater than 6 meters in length or greater than 10 meters in length. The LFP system converts the combined RWGS and ATR products into hydrocarbon products, greater than 50% of which are C5 to C6 hydrocarbons. 24 It is a hydrocarbon.

[0069] 23. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear as a renewable energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃)The feedstock is heated to an inlet temperature above 1000° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor containing a nickel solid solution catalyst. The catalyst particles are controlled in shape and size to provide a pressure drop across the reactor of less than 50 pounds per square inch, or less than 20 pounds per square inch. The RWGS reactor converts the feedstock into a RWGS product gas that includes carbon monoxide, hydrogen, unreacted carbon dioxide, and water. The conversion of carbon dioxide to carbon monoxide per pass in the RWGS reactor is between 15 and 90 mole %, or between 40 and 80 mole %, and the weight hourly space velocity for the RWGS is between 1,000 and 50,000 hr -1 and more preferably between 5,000 and 30,000 hours -1 The RWGS product gas is cooled, compressed and fed, along with the recycled syngas, into a Liquid Fuel Production (LFP) system containing a catalyst that produces hydrocarbons from the syngas. The reactor is a fixed bed reactor system having multiple tubes, each reactor tube having an I diameter between 13 mm and 26 mm and greater than 6 meters or greater than 10 meters in length. The LFP system converts the RWGS product gas (either refined or raw) into hydrocarbon products, with greater than 50% of the products being C4 to C6. 24 Less than 2% of the carbon monoxide in the LFP reactor feed is converted to carbon monoxide in the LFP reactor, and less than 10% or less than 4% by weight of the hydrocarbon fraction of the LFP product has a carbon number greater than 24.

[0070] 24. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear as a renewable energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃) The feedstock is heated to an inlet temperature above 1000° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor containing a nickel solid solution catalyst. The catalyst particles are controlled in shape and size to provide a pressure drop across the reactor of less than 50 pounds per square inch, or less than 20 pounds per square inch. The RWGS reactor converts the feedstock into a RWGS product gas that includes carbon monoxide, hydrogen, unreacted carbon dioxide, and water. The conversion of carbon dioxide to carbon monoxide per pass in the RWGS reactor is between 15 and 75 mole %, or between 30 and 70 mole %, and the weight hourly space velocity for the RWGS is between 1,000 and 50,000 hr -1 and more preferably between 5,000 and 30,000 hours -1One or more of C1-C4 hydrocarbons (e.g., methane), carbon monoxide, and hydrogen are fed into an autothermal reformer (ATR) containing a nickel solid solution catalyst to provide an ATR product stream. The RWGS product gas (either refined or raw) is combined with the ATR product stream (either refined or raw) and fed, along with recycled syngas, into a liquid fuel production (LFP) system containing a catalyst for producing hydrocarbons from the syngas. The reactor is a fixed bed reactor system having a plurality of tubes, each reactor tube having an I diameter between 13 mm and 26 mm and greater than 6 meters in length or greater than 10 meters in length. The LFP system converts the combined RWGS and ATR products into hydrocarbon products, with greater than 50% of the products being C4 to C6. 24 Less than 2% of the carbon monoxide in the LFP reactor feed is converted to carbon monoxide in the LFP reactor, and less than 10% or less than 4% by weight of the hydrocarbon fraction of the LFP product has a carbon number greater than 24.

[0071] 25. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear as a renewable energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃)The feedstock is heated to an inlet temperature above 100° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor containing a nickel solid solution catalyst. The catalyst particles are controlled in shape and size to provide a pressure drop across the reactor of less than 100 pounds per square inch or less. The RWGS reactor converts the feedstock into a RWGS product gas that contains carbon monoxide, hydrogen, unreacted carbon dioxide, and water. The conversion of carbon dioxide to carbon monoxide per pass in the RWGS reactor is between 15 and 75 mole %, or between 30 and 70 mole %, and the weight hourly space velocity for the RWGS is between 1,000 and 50,000 hr -1 and more preferably between 5,000 and 30,000 hours -1 The RWGS product gas is cooled, compressed and fed, along with recycled syngas, into a Liquid Fuel Production (LFP) system containing a catalyst for producing hydrocarbons from the syngas. The LFP catalyst support has a pore size greater than 8 nanometers, an average effective pellet radius less than 60 micrometers, a crush strength greater than 3 lb / mm, and a pore size greater than 80 m. 2 / g, wider than 90m 2 / g, wider than 100m 2 / g, wider than 125m 2 / g or wider than 150m 2 The catalyst has a BET surface area of ​​greater than 100 nm / g and a metal dispersion of the catalyst on the support of between 2% and 4%, or 3%. The reactor is a fixed bed reactor system having multiple tubes, each reactor tube having an I diameter of between 13 mm and 26 mm and greater than 6 meters in length, or greater than 10 meters in length. The LFP system converts the RWGS product gas (either refined or raw) into hydrocarbon products, with greater than 50% of the products being C4 to C6. 24 Less than 2% of the carbon monoxide in the LFP reactor feed is converted to carbon monoxide in the LFP reactor, and less than 10% or less than 4% by weight of the hydrocarbon fraction of the LFP product has a carbon number greater than 24.

[0072] 26. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear as a renewable energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃) The feedstock is heated to an inlet temperature above 1000° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor containing a nickel solid solution catalyst. The catalyst particles are controlled in shape and size to provide a pressure drop across the reactor of less than 50 pounds per square inch, or less than 20 pounds per square inch. The RWGS reactor converts the feedstock to a RWGS product gas that includes carbon monoxide, hydrogen, unreacted carbon dioxide, and water. The conversion of carbon dioxide to carbon monoxide per pass in the RWGS reactor is between 15 and 90 mole %, or between 50 and 85 mole %, and the weight hourly space velocity for the RWGS is between 1,000 and 50,000 hr -1 and more preferably between 5,000 and 30,000 hours -1One or more of C1-C4 hydrocarbons (e.g., methane), carbon monoxide, and hydrogen are fed into an autothermal reformer (ATR) containing a nickel solid solution catalyst to provide an ATR product stream. The RWGS product gas (either refined or raw) is combined with the ATR product stream (either refined or raw) and fed into a liquid fuel production (LFP) system along with a catalyst to produce hydrocarbons from the syngas. The LFP catalyst support has a pore size greater than 8 nanometers, an average effective pellet radius less than 60 micrometers, a crush strength greater than 3 lbs / mm, and a thermal conductivity greater than 80 m. 2 / g, wider than 90m 2 / g, wider than 100m 2 / g, wider than 125m 2 / g or wider than 150m 2 The catalyst has a BET surface area of ​​greater than 100 / g and a metal dispersion of between 2% and 4%, or 3%, on the support. The reactor is a fixed bed reactor system having multiple tubes, each reactor tube having an I diameter of between 13 mm and 26 mm and greater than 6 meters in length, or greater than 10 meters in length. The LFP system converts the combined RWGS and ATR products into a hydrocarbon product, with greater than 50% of the product being C4 to C6. 24 Less than 2% of the carbon monoxide in the LFP reactor feed is converted to carbon monoxide in the LFP reactor, and less than 10% or less than 4% by weight of the hydrocarbon fraction of the LFP product has a carbon number greater than 24.

[0073] 27. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear as a renewable energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃) The feedstock is heated to an inlet temperature above 1000° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor containing a nickel solid solution catalyst. The catalyst particles are controlled in shape and size to provide a pressure drop across the reactor of less than 50 pounds per square inch, or less than 20 pounds per square inch. The RWGS reactor converts the feedstock into a RWGS product gas that includes carbon monoxide, hydrogen, unreacted carbon dioxide, and water. The conversion of carbon dioxide to carbon monoxide per pass in the RWGS reactor is between 15 and 75 mole %, or between 30 and 70 mole %, and the weight hourly space velocity for the RWGS is between 1,000 and 50,000 hr -1 and more preferably between 5,000 and 30,000 hours -1 The RWGS product gas is cooled, compressed and fed, along with recycled syngas, into a Liquid Fuel Production (LFP) system containing a catalyst for producing hydrocarbons from the syngas. The LFP catalyst support has a pore size greater than 8 nanometers, an average effective pellet radius less than 60 micrometers, a crush strength greater than 3 lb / mm, and a pore size greater than 80 m. 2 / g, wider than 90m 2 / g, wider than 100m2 / g, wider than 125m 2 / g or wider than 150m 2 The catalyst has a BET surface area of ​​greater than 100 nm / g and a metal dispersion of the catalyst on the support of between 2% and 4%, or 3%. The reactor is a fixed bed reactor system having multiple tubes, each reactor tube having an I diameter of between 13 mm and 26 mm and greater than 6 meters in length, or greater than 10 meters in length. The LFP system converts the RWGS product gas (either refined or raw) into hydrocarbon products, with greater than 50% of the products being C4 to C6. 24 Less than 2% of the carbon monoxide in the LFP reactor feed is converted to carbon monoxide in the LFP reactor, and less than 10% or less than 4% by weight of the hydrocarbon fraction of the LFP product has a carbon number greater than 24. The conversion of CO in the LFP reactor maintains between 30 and 80 mol% CO conversion per pass, and carbon selectivity to CO2 is minimized to less than 4% or less than 1% for the converted CO.

[0074] 28. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear as a renewable energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃)The feedstock is heated to an inlet temperature above 1000° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor containing a nickel solid solution catalyst. The catalyst particles are controlled in shape and size to provide a pressure drop across the reactor of less than 50 pounds per square inch, or less than 20 pounds per square inch. The RWGS reactor converts the feedstock to a RWGS product gas that includes carbon monoxide, hydrogen, unreacted carbon dioxide, and water. The conversion of carbon dioxide to carbon monoxide per pass in the RWGS reactor is between 15 and 90 mole %, or between 60 and 90 mole %, and the weight hourly space velocity for the RWGS is between 1,000 and 50,000 hr -1 and more preferably between 5,000 and 30,000 hours -1 One or more of C1-C3 hydrocarbons (e.g., methane), carbon monoxide, and hydrogen are fed into an autothermal reformer (ATR) containing a nickel solid solution catalyst to provide an ATR product stream. The RWGS product gas (either refined or raw) is combined with the ATR product stream (either refined or raw) and fed, along with recycled syngas, into a liquid fuel production (LFP) system containing a catalyst to produce hydrocarbons from the syngas. The LFP catalyst support has a pore size greater than 8 nanometers, an average effective pellet radius less than 60 micrometers, a crush strength greater than 3 lbs / mm, and a thermal conductivity greater than 80 m. 2 / g, wider than 90m 2 / g, wider than 100m 2 / g, wider than 125m 2 / g or wider than 150m 2 The catalyst has a BET surface area of ​​greater than 100 / g and a metal dispersion of between 2% and 4%, or 3%, on the support. The reactor is a fixed bed reactor system having multiple tubes, each reactor tube having an I diameter of between 13 mm and 26 mm and greater than 6 meters in length, or greater than 10 meters in length. The LFP system converts the combined RWGS and ATR products into a hydrocarbon product, with greater than 50% of the product being C4 to C6.24 Less than 2% of the carbon monoxide in the LFP reactor feed is converted to carbon monoxide in the LFP reactor, and less than 10% or less than 4% by weight of the hydrocarbon fraction of the LFP product has a carbon number greater than 24. The conversion of CO in the LFP reactor maintains between 30 and 80 mol% CO conversion per pass, and carbon selectivity to CO2 is minimized to less than 4% or less than 1% for the converted CO.

[0075] 29. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear as a renewable energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃) The feedstock is heated to an inlet temperature above 1000° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor containing a nickel solid solution catalyst. The catalyst particles are controlled in shape and size to provide a pressure drop across the reactor of less than 50 pounds per square inch, or less than 20 pounds per square inch. The RWGS reactor converts the feedstock into a RWGS product gas that includes carbon monoxide, hydrogen, unreacted carbon dioxide, and water. The conversion of carbon dioxide to carbon monoxide in the RWGS reactor per pass is between 15 and 90 mole %, or between 30 and 70 mole %, and the weight hourly space velocity for the RWGS is between 1 and 1,000 to 50,000 hr -1and more preferably between 5,000 and 30,000 hours -1 The RWGS product gas is cooled, compressed and fed together with the recirculated syngas into a Liquid Fuel Production (LFP) system containing another catalyst to produce hydrocarbons from the syngas. The hydrocarbons produced in this process, or a portion thereof, are used as fuel. This fuel has a percent reduction in life cycle greenhouse gas emissions of at least 10%, at least 20%, at least 30%, at least 40%, at least 50%, at least 60%, at least 70%, at least 80%, or at least 90% compared to the average life cycle greenhouse gas emissions of petroleum diesel (produced by fractional distillation of crude oil between 200° C. and 350° C. at atmospheric pressure, typically resulting in a mixture of carbon chains containing 9 to 25 carbon atoms per molecule).

[0076] 30. Water is fed to an electrolysis system powered by renewable electricity, the electrolyzers of which operate using alkaline, membrane or high temperature electrolysis, and the renewable electricity is derived from wind, solar, geothermal or nuclear as a renewable energy source. Carbon dioxide is captured from a source which may be an industrial manufacturing plant producing ammonia for fertilizer, a cement plant, an ethanol plant converting corn or wheat to ethanol, an oil refinery, a chemical plant, a power plant producing electricity, anaerobic digestion or the atmosphere. Hydrogen and carbon dioxide are mixed to form a stream (Reverse Water Gas Shift Feedstock or "RWGS" Feedstock) which is heated to 1,400°F using radiant electric heating elements with power usage of less than 0.5 MWh / metric ton of power, less than 0.40 MWh / metric ton of power or less than 0.20 MWh / metric ton of power for CO2 in the feed gas. (760℃)The feedstock is heated to an inlet temperature greater than 100° C., which heating is not provided by direct combustion of a carbon-containing gas, and then fed into an adiabatic or isothermal RWGS reactor containing a nickel solid solution catalyst. The RWGS reactor converts the feedstock into a RWGS product gas containing carbon monoxide, hydrogen, unreacted carbon dioxide, and water. The conversion of carbon dioxide to carbon monoxide per pass in the RWGS reactor is between 15 and 75 mole %, or between 30 and 70 mole %, and the weight hourly space velocity for the RWGS is between 1,000 and 50,000 hr -1 and more preferably between 5,000 and 30,000 hours -1 One or more of the C1-C4 hydrocarbons (e.g., methane), carbon monoxide, and hydrogen are fed into an autothermal reformer (ATR) to provide an ATR product stream. The RWGS product gas (either refined or raw) is combined with the ATR product stream (either refined or raw) and fed into a fuel or chemical production system that has a life cycle greenhouse gas emission percent reduction of at least 10%, at least 20%, at least 30%, at least 40%, at least 50%, at least 60%, at least 70%, at least 80%, or at least 90% compared to the average life cycle greenhouse gas emissions for a petroleum-derived product. EXAMPLES

[0077] 1-2 show an integrated process for converting carbon dioxide, water and electricity into renewable fuels and chemicals.

[0078] The inlets to the process are 1) 1,919 metric tonnes per day (MT / D) of carbon dioxide, 1,214 MT / D of fresh water, and 3) 721.5 MW of renewable electricity.

[0079] In Figure 3, fresh water (stream 25) is combined with 1,497 MT / D of process water (or recycle water) (stream 26) from the process. The fresh and recycle water feed for the electrolyzer is 2,711 MT / D in total. The alkaline electrolyzer step 27 is maintained at 60 psig and 70°F. (21℃) The electrolyser operates at 1000 MW. The products of the electrolyser are 303 MT / D of hydrogen (Stream 28) and 2,408 MT / D of oxygen (Stream 29). For the electrolyser energy usage of 51.3 MWh / MT of hydrogen produced, the electrolyser uses 648.1 MW of electricity. Hydrogen (Stream 1 in Figure 1, 302 MT / D) is mixed with carbon dioxide (Stream 2) to provide the RWGS feed (Stream 3). Carbon dioxide (Stream 2) is a mix of fresh carbon dioxide (Stream 2, 1,919 MT / D) and recycled carbon dioxide (734 MT / D). In the RWGS feed, the molar ratio of H2 to CO2 is (H 2 (mol) / CO 2 (mol) is 2.5, which is within the desired range. The initial feed to the RWGS (Stream 3) is at a pressure of 60 psig and a temperature of 66° F. (19℃) In step 4, two independent heat exchangers, stream 3 is heated by indirect heat exchange to a temperature of 984°C. ° F (529℃) (Stream 5) gas to 1,600°F (871℃) An electric radiant furnace is used to heat the CO2 to 100° C. The electric radiant furnace uses 30.7 MW of electricity resulting in a power usage of 0.278 MWh / CO2 MT for CO2 in the product stream or final feed stream of the RWGS (Stream 5). The RWGS reactor (Step 6) is a refractory lined vessel or a collection of parallel reactors. The RWGS reactor is loaded with catalyst. The RWGS catalyst used in this example is a solid solution catalyst with only transition metals. The RWGS reactor outlet pressure is 10 psi lower than the inlet pressure of 55 psig. The RWGS outlet temperature is 1,600° F. (871℃) 152°F higher than the inlet temperature (84℃)Low. CO2 conversion is 70 mol%. 92 mol% of the converted CO2 is converted to CO (selectivity to CO 92%), and 8% of the converted CO2 is converted to methane via side reactions.

[0080] In this example, the RWGS reactor product gas (Stream 7) is optionally heated to 1,600° F. in a second heater and RWGS bed (Steps 9 and 10, respectively). (871℃) The reheated gas is then fed back to the second RWGS reactor (step 10), which for this example has a pressure drop of 10 psi and a temperature of 108° F. (60℃) The conversion of CO2 is 7 mol%.

[0081] The outlet of the second RWGS reactor was 1492°F. (811℃) The syngas mixture has an approximate bulk composition of 49 mol% H2, 20 mol% CO, 1 mol% methane, 8 mol% CO2, and 22 mol% water at a temperature of 1,256°F. This steam is then pumped through indirect heat exchange to a (680℃) (step 11) and combined with the syngas produced by the autothermal reformer (ATR) to provide a combined feed to the syngas cooling and syngas compression portions of the process.

[0082] Figure 2 shows the ATR portion of the process. The ATR has a flow rate of 855 MT / D and an ATR hydrocarbon feed (stream 18) that includes tail gas from the LFP portion of the facility with a molar composition of 21% hydrogen, 12% CO, 42% methane, 1% ethane, 2% propane, 1% butane, 1% pentane, 1% hexane, and 18% carbon dioxide. The ATR oxidant feed (stream 29) is 335 MT / D of oxygen produced in the electrolyzer. The ATR hydrocarbon feed is mixed with 255 MT / D of superheated steam. The oxidant is mixed with the ATR hydrocarbon feed prior to the ATR burner, simultaneously with the steam. This stream is heated by cross heat exchange with the ATR product, and this stream and oxygen are combusted in the ATR burner, and the combustion products pass through the ATR catalyst bed to produce 1832 MT / D of oxygen. ° F (1,000℃) The ATR exits (Stream 21) at or near the predicted equilibrium composition with an outlet temperature of 1,251° F. The ATR operates with a feed steam to carbon ratio of 0.53, which is the ratio of moles of steam to moles of carbon from all sources in the feed (including CO2 and CO). Soot and carbon formation is minimized by using a gold promoter and Ni on Mg spinel catalyst with a low operating pressure of 58 psig. The molar composition for the ATR product stream (Stream 21) is 46% hydrogen, 7% CO2, 7% carbon dioxide, and 20% water. The hydrogen to carbon monoxide ratio of the syngas is 1.7. The ATR product stream is pumped via cross exchange to a temperature of 1,251° F. (677℃) Cool to .

[0083] The product stream from the ATR is combined with the syngas from the RWGS reactor system and fed to the syngas cooling and compression portion of the plant. The combined syngas is cooled by a steam boiler. A portion of the water vapor from the steam system is used to combine with the ATR hydrocarbon feed. This stream is also cooled by an air-cooled fan. Water is removed from this stream as syngas condensate. Three stages of compression are used to reduce the pressure of the syngas to 340 psig and the temperature to 338°F. (170℃) This syngas is discharged as syngas to LFP at a rate of 3,093 MT / D with a molar composition of approximately 61% hydrogen, 28% carbon monoxide, 10% carbon dioxide, and 1% water. Electricity is required to compress the syngas. The power consumption of the syngas compressor is 34.0 MW.

[0084] FIG. 2 shows the LFP portion of the process where feed syngas stream 23 (3,093 MT / D) is blended with a recycle stream of LFP (stream 13) of 19,185 MT / D. The molar composition of this recycle gas is approximately 13% hydrogen, 7% carbon monoxide, 26% methane, 48% carbon dioxide, 1% water, 1% ethane, 2% propane, 1% butane, and 1% pentane. The composition of this recycle gas is controlled so that the blended feed gas has the correct composition ideal for a liquid combustion production process using the preferred LFP catalyst. The LFP reactor feed (stream 14) has a molar composition of approximately 26% hydrogen, 13% CO, 19% methane, 1% propane, 1% butane, 1% pentane, 38% carbon dioxide, and 1% water, and has a flow rate of approximately 22,277 MT / D. The H2 / CO ratio for the LFP feed is 2.0. Indirect heat exchange keeps the LFP feed temperature at 380°F at 330 psig pressure. (193℃)In a specific case, the LFP reactor is 10 reactors operating in parallel, the reactors are 30 meters tall from tangent to tangent, and each reactor contains a shell with 5,000 tubes inside, the tubes having an outer diameter of about 19 mm.

[0085] The reaction to produce hydrocarbons from syngas is exothermic. Steam is used outside the tubes of the LFP reactor to control the temperature. Thus, the LFP reactor raises steam, which can be used to generate electricity. The LFP steam is used to generate 8.7 MW of electricity.

[0086] For LFP reactors, the preferred operating temperature is 410°F. (210℃) It is.

[0087] In a particular case, the LFP catalyst has an average particle size of 50 micrometers, a pore size of 9 nm, and a pore size of 140 nm. 2 / g surface area, and the active metal is cobalt with a platinum or palladium promoter.

[0088] The catalyst particle size, catalyst loading, and velocity of the LFP feed to the LFP reactor tube are all controlled to minimize pressure drop within the LFP reactor tube and across the reactor, which in this example is maintained at 20 psig.

[0089] The CO conversion in the LFP reactor is 55 mol%. 24 The carbon selectivity to 1,2-dichloro-1,2-triazol-2,3-tetraazol-2,4-diazol-2,5-triazol-2,6-tetraazol-2,7-diazol-2,8-diazol-2,9 ...10-diazol-2,11-diazol-2,12-diazol-2,13-diazol-2,14-diazol-2,15-diazol-2,16-diazol-2,17-diazol-2,18-diazol-2,19-diazol-2,20-diazol-2,21-diazol-2,22-diazol-2,23-diazol-2,30-diazol-2,31-diazol-2,

[0090]

number

[0091] where n CO Converted is the molar flow rate of CO converted in the LFP reactor, and ni is the molar flow rate of hydrocarbons with carbon number i produced in the LFP reactor. The carbon selectivity to carbon dioxide is low at 0.38%, indicating that only a small amount of the CO converted in the LFP reactor is converted to carbon dioxide.

[0092]

number

[0093] where n CO2 is the molar flow rate of CO produced in the LFP reactor. This is highly favorable for zero-carbon fuel and chemical production processes that start with carbon dioxide as a feedstock.

[0094] The product emerges from the bottom of the reactor. Heavy hydrocarbons (C 24+ ) may be produced and these products can be withdrawn at the reactor outlet. If the LFP reactor is operated under the right conditions with a catalyst, there will be very few heavy products. The main LFP product is stream 16. The LFP product is further cooled to 333F in step 17 and is stream numbered 24 exiting Figure 2.

[0095] The LFP product stream is cooled to condense the products, and then in step 17 the LFP product is passed through a separator to separate into three streams. Product water (stream 26) is generated from the LFP process and is recycled to the electrolyzer and may require purification or prior treatment. The light gaseous products of the LFP reactor end up in streams 13 and 18, which are recycled to the LFP reactor feed and to the ATR. Before recycling this stream, it may be further separated into two streams via a CO2 separation system, if desired. The CO2-rich stream may be recycled back to the RWGS reactor feed. The remaining CO, H2 and light hydrocarbons in this stream are recycled back to the ATR.

[0096] C4~C 24 The LFP hydrocarbon product stream is separated into two streams: gasoline blending stock and diesel fuel, which may also be further processed.

[0097] An example process produces 1,669 barrels per day (BPD) of naphtha / gasoline blendstock and 3,387 BPD of diesel fuel. The LFP products may be further fractionated and processed to produce specialty chemicals including solvents, n-paraffins, and olefins.

[0098] Table 1 summarizes the inputs for this example. MT C / day is the metric tons of carbon per day for this input. MT H / day is the metric tons of hydrogen for this input. These are important for calculating the carbon and hydrogen yields.

[0099] [Table 1]

[0100] Table 2 summarizes the outputs for this example.

[0101] [Table 2]

[0102] Table 3 shows some useful indices calculated for the example process.

[0103] [Table 3]

[0104] In the example process and all processes of the present invention, the carbon yield will be greater than 70%, and preferably greater than 85%. To obtain such high carbon yields, overall process integration is required, as is the use of the disclosed RWGS catalysts and the use of the disclosed LFP catalysts.

[0105] The present disclosure includes the following. (1) 1. An integrated process for converting a feed stream comprising carbon dioxide to a product stream comprising a hydrocarbon, comprising: a. an electrolysis step to convert an electrolyzer feed stream comprising water into an electrolyzer product stream comprising hydrogen and oxygen, wherein at least a portion of the electricity used in the electrolysis step is from a renewable or low carbon source; b. a reverse water gas shift step of reacting at least a portion of the hydrogen from the electrolyzer product stream with a stream comprising carbon dioxide to produce a reverse water gas shift product stream comprising carbon monoxide; c. reacting at least a portion of the hydrogen from the electrolyzer product stream with a stream comprising at least a portion of the reverse water gas shift product stream to produce a hydrocarbon synthesis product stream comprising hydrocarbons; d. an autothermal reforming step in which at least a portion of the oxygen produced by electrolysis is reacted with one or more streams comprising a) unreacted reactants from the hydrocarbon synthesis step, and b) products from the hydrocarbon synthesis step that are not hydrocarbons between 5 and 24 carbon atoms in length; The method includes: (2) The method according to (1) above, wherein the pressure of the reverse water gas shift step and the pressure of the hydrocarbon synthesis step are operated at a pressure difference of within 50 psi of each other. (3) The process of claim 1, wherein the reverse water gas shift reactor feed is heated to at least 1,500°F (816°C) using an electric radiant furnace, the reactor vessel is an adiabatic reactor, and the reactor outlet temperature is at least 100°F (56°C) lower than the inlet temperature. (4) The feed to the reverse water gas shift reactor has a hydrogen to carbon dioxide molar ratio (H 2 (mol) / CO 2 The method described in (3) above, having a composition such that (mol)) is 2.5 to 3.5. (5) The feedstock for the hydrocarbon synthesis has a molar ratio of hydrogen to carbon monoxide (H 2 (mol) / CO(mol)) is between 1.90 and 2.20, the hydrocarbon synthesis catalyst contains cobalt, and C 4 ~C 24 The selectivity of C is higher than 70%. 24 2. The process of claim 1, wherein the amount of carbon monoxide converted to heavier products is less than 10%. (6) The method according to (1) above, wherein the autothermal reforming step includes steam as a feed, and the steam to carbon ratio is between 0.40 and 1.00. (7) The method according to (6) above, wherein the autothermal reforming (ATR) catalyst is a solid solution catalyst. (8) The method of (1) above, wherein one of the feeds to the autothermal reforming step comprises natural gas. (9) The power consumption of the radiant furnace is 0.5 MWh (megawatt hour) of electricity / CO in the supply gas. 2 The method described in (1) above, wherein the amount is less than metric ton (MT). (10) The method of (1) above, wherein the radiant element may be divided into multiple zones to provide a controlled pattern of heating for the reverse water gas shift (RWGS) reactor. (11) 1. An integrated process for converting a feed stream comprising carbon dioxide to a product stream comprising a hydrocarbon, comprising: a. an electrolysis step for converting an electrolyzer feed stream comprising water into an electrolyzer product stream comprising hydrogen and oxygen, wherein at least a portion of the electricity used in the electrolysis step is from a renewable resource; b. a reverse water gas shift step of reacting at least a portion of the hydrogen from said electrolyser feed stream with a stream comprising carbon dioxide to produce a reverse water gas shift product stream comprising carbon monoxide; c. reacting at least a portion of the hydrogen from the electrolyzer product stream with a stream comprising at least a portion of the reverse water gas shift product stream to produce a chemical synthesis step; d. an autothermal reforming step in which at least a portion of the oxygen produced by electrolysis is reacted with one or more streams containing a) unreacted reactants from the chemical synthesis step; The method includes: (12) 12. The method of claim 11, wherein the chemicals produced as part of the method include methanol. (13) 12. The method of claim 11, wherein the chemicals produced as part of the method include a solvent. (14) 12. The process of claim 11, wherein the chemicals produced as part of the process include olefins. (15) The method of claim 11, wherein the chemicals produced as part of the method include n-paraffins. (16) The method according to (12) above, wherein fuel is produced in addition to the chemicals. (17) The method according to (13) above, wherein fuel is produced in addition to the chemicals. (18) The method according to (14) above, wherein fuel is produced in addition to the chemicals. (19) The method according to (15) above, wherein fuel is produced in addition to the chemicals.

Claims

1. 1. An integrated process for converting a feed stream comprising carbon dioxide to a product stream comprising a hydrocarbon, comprising: a. an electrolysis step to convert an electrolyzer feed stream comprising water into an electrolyzer product stream comprising hydrogen and oxygen, wherein at least a portion of the electricity used in the electrolysis step is from a renewable or low carbon source; b. a reverse water gas shift step of reacting at least a portion of the hydrogen from the electrolyzer product stream with a stream comprising carbon dioxide in a reverse water gas shift reactor to produce a reverse water gas shift product stream comprising carbon monoxide; c) reacting at least a portion of the hydrogen from the electrolyzer product stream with a stream comprising at least a portion of the reverse water gas shift product stream to produce a hydrocarbon synthesis product stream comprising hydrocarbons; d. an autothermal reforming step in which at least a portion of the oxygen produced by electrolysis is reacted with one or more streams comprising a) unreacted reactants from the hydrocarbon synthesis step, and b) products from the hydrocarbon synthesis step that are not hydrocarbons between 5 and 24 carbon atoms in length; The method of claim 1, wherein the feed to the reverse water gas shift reactor is a stream having a composition with a hydrogen to carbon dioxide molar ratio (H2(mol) / CO2(mol)) of 2.0 to 4.0 and heated to a temperature greater than 1,400°F (760°C).

2. 2. The method of claim 1, wherein the reverse water gas shift step pressure and the hydrocarbon synthesis step pressure are operated at within 50 psi of each other.

3. 2. The method of claim 1, wherein the reverse water gas shift reactor feed is heated to at least 1,500°F (816°C) using an electric radiant furnace to feed the reactor, the reactor being an adiabatic reaction vessel, and the reactor outlet temperature is at least 100°F (56°C) lower than the inlet temperature.

4. 2. The process of claim 1, wherein the feed to the reverse water gas shift reactor has a composition such that the molar ratio of hydrogen to carbon dioxide (H2(mol) / CO2(mol)) is from 2.5 to 3.

5.

5. The hydrocarbon synthesis feedstock has a hydrogen to carbon monoxide molar ratio between 1.90 and 2.20, the hydrocarbon synthesis catalyst comprises cobalt, and ４ ~C ２４ The selectivity of C is higher than 70%. ２４ 2. The process of claim 1, wherein the amount of carbon monoxide converted to heavier products is less than 10%.

6. 10. The method of claim 1, wherein the autothermal reforming step includes steam as a feed, and the steam to carbon ratio is between 0.40 and 1.

00.

7. 7. The method of claim 6, wherein the catalyst for the autothermal reforming step is a solid solution catalyst.

8. The method of claim 1 , wherein one of the feeds to the autothermal reforming step comprises natural gas.

9. The power consumption of the radiant furnace is 0.5 MWh (megawatt hour) of power / CO in the supply gas. ２ 4. The method of claim 3, wherein the amount of the raw material is less than a metric ton (MT).

10. 4. The method of claim 3, wherein the radiant elements in the radiant furnace are divided into a plurality of zones to provide a controlled pattern of heating for the reverse water gas shift reactor.

11. 1. An integrated process for converting a feed stream comprising carbon dioxide to a product stream comprising a hydrocarbon, comprising: a. an electrolysis step for converting an electrolyzer feed stream comprising water into an electrolyzer product stream comprising hydrogen and oxygen, wherein at least a portion of the electricity used in said electrolysis step is from a renewable resource; b. a reverse water gas shift step in which at least a portion of the hydrogen from the electrolyser feed stream is reacted with a stream comprising carbon dioxide in a reverse water gas shift reactor to produce a reverse water gas shift product stream comprising carbon monoxide; c. reacting at least a portion of the hydrogen from the electrolyzer product stream with a stream comprising at least a portion of the reverse water gas shift product stream to produce a chemical synthesis step; d. an autothermal reforming step in which at least a portion of the oxygen produced by electrolysis is reacted with a) one or more streams containing unreacted reactants from the chemical synthesis step; The method of claim 1, wherein the feed to the reverse water gas shift reactor is a stream having a composition with a hydrogen to carbon dioxide molar ratio (H2(mol) / CO2(mol)) of 2.0 to 4.0 and heated to a temperature greater than 1,400°F (760°C).

12. 12. The method of claim 11, wherein the chemicals produced as part of the method include methanol.

13. 12. The method of claim 11, wherein the chemicals produced as part of the method include a solvent.

14. 12. The method of claim 11, wherein the chemicals produced as part of the method include olefins.

15. 12. The method of claim 11, wherein the chemicals produced as part of the method include n-paraffins.

16. 13. The method of claim 12, wherein fuel is produced in addition to the chemical.

17. 14. The method of claim 13, wherein fuel is produced in addition to the chemical.

18. 15. The method of claim 14, wherein fuel is produced in addition to the chemicals.

19. 16. The method of claim 15, wherein fuel is produced in addition to the chemical.

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