Apparatus and method for producing synthetic fuels without using fresh water

Abstract

The invention relates to a plant for producing synthetic fuels, in particular aviation turbine fuel (kerosene), gasoline and / or diesel, comprising a) a device for separately taking carbon dioxide and water from ambient air, b) a synthesis gas production device for producing a raw synthesis gas comprising carbon monoxide, hydrogen, carbon dioxide and water, wherein the synthesis gas production device has a carbon dioxide supply line, an air supply line and a water supply line leading from the device for separately taking carbon dioxide and water from ambient air, c) a separation device for separating carbon dioxide and water from the raw synthesis gas produced in the synthesis gas production device, d) a Fischer-Tropsch device for producing hydrocarbons from the synthesis gas from which carbon dioxide and water are separated in the separation device by means of the Fischer-Tropsch process, e) a refining device for refining the hydrocarbons produced in the Fischer-Tropsch device to synthetic fuels, f) a desalination device for desalinating water, wherein the desalination device has a water supply line from the device for separately taking carbon dioxide and water from ambient air and a water discharge line leading to the Fischer-Tropsch device, and g) a water purification device comprising a water supply line leading from the Fischer-Tropsch device to purify the water produced therein, wherein the plant further comprises a pre-reformer for converting non-methane hydrocarbons into methane, carbon oxides, water and hydrogen and i) a water vapor supply line leading from the water purification device to the pre-reformer, ii) a process gas supply line leading from the refining device to the pre-reformer and / or a return gas line leading from the Fischer-Tropsch device to the pre-reformer and iii) a circulation line leading from the pre-reformer to the water supply line connected to the synthesis gas production device.

Description

[0001] This invention relates to apparatus and methods for producing synthetic fuels, particularly aviation turbine fuels, diesel fuel, and / or gasoline.

[0002] There are many different methods for producing fuels, such as aviation turbine fuel, diesel, and gasoline. These methods are primarily based on the processing of fossil fuels, such as crude oil refining, coal liquefaction, or the synthesis of fuels from natural gas, water, and oxygen. The synthesis of fuels from natural gas, water, and oxygen is also known as the "gas-to-oil" process. In this method, syngas containing hydrogen and carbon monoxide is first produced from natural gas, water, and oxygen, which is then converted into hydrocarbons in a Fischer-Tropsch synthesis process. These hydrocarbons are primarily composed of long-chain n-alkanes. These hydrocarbons are then converted into synthetic fuels through cracking and isomerization.

[0003] A similar method involves converting electrical energy into synthetic fuels, known as "power-to-liquids." This involves converting water and carbon dioxide into syngas, which is then further processed into synthetic fuels in a manner similar to "natural gas-to-liquids" (GTL). A significant drawback of both GTL and GTL is the requirement for substantial amounts of fresh water. However, water of the required purity is an expensive feedstock. Furthermore, known methods generate relatively large amounts of unused waste gas and wastewater, which is environmentally undesirable.

[0004] Therefore, the object of the present invention is to provide an apparatus and method for producing synthetic fuels that can operate with little or no fresh water supply and produce only a very small amount of unused exhaust gas and wastewater, thereby increasing the yield of synthetic fuels, while still being able to operate on electricity and preferably renewable energy.

[0005] According to the present invention, this objective is achieved by an apparatus for producing synthetic fuels, particularly aviation turbine fuel, diesel fuel, and / or gasoline, said apparatus comprising: a) Equipment used to separate and extract carbon dioxide and water from ambient air. b) A syngas production apparatus for producing crude syngas comprising carbon monoxide, hydrogen, carbon dioxide, and water, wherein the syngas production apparatus has a carbon dioxide supply line, an air supply line, and a water or water vapor supply line extending from equipment for separating carbon dioxide and water from ambient air. c) Separation equipment for separating carbon dioxide and water from crude syngas produced in syngas production facilities. d) Fischer-Tropsch equipment used to produce hydrocarbons from syngas from which carbon dioxide and water are separated in a separation unit via the Fischer-Tropsch process. e) Refining equipment used to refine hydrocarbons produced in Fischer-Tropsch plants into synthetic fuels. f) Desalination equipment for desalinizing water, wherein the desalination equipment has a water supply line from a device for separating and extracting carbon dioxide and water from ambient air and a water discharge line leading to the Fischer-Tropsch unit, and g) Water purification equipment, comprising a water supply line extending from the Fischer-Tropsch unit to purify the water produced therein. The apparatus further includes a pre-reformer for converting non-methane hydrocarbons into methane, carbon oxides, water, and hydrogen, and i) a steam supply line from a water purification unit to the pre-reformer, ii) a process gas supply line from a refining unit to the pre-reformer and / or a return gas line from a Fischer-Tropsch unit to the pre-reformer, and iii) a circulation line from the pre-reformer to a water or steam supply line connected to a syngas production unit.

[0006] Because in the apparatus and method according to the invention, the water required for fuel synthesis, particularly syngas production and Fischer-Tropsch synthesis, is partially obtained from ambient air, and the carbon dioxide required is entirely obtained from ambient air, and the (reaction) water generated in the water purification equipment during fuel synthesis, particularly Fischer-Tropsch synthesis, and preferably in the desalination equipment during syngas production, is purified to the extent necessary for recycling, processed in a pre-reformer, and recycled from there to the syngas production equipment, the apparatus and method according to the invention can operate using only water generated from ambient air and (reaction) water generated from the apparatus and optionally other parts of the apparatus in Fischer-Tropsch synthesis, such as the syngas production equipment, i.e., with no or at most a small supply of fresh water, and particularly in a carbon dioxide-neutral manner. Here, in order to operate with no or at most a small supply of fresh water, the use of (reaction) water generated in the Fischer-Tropsch synthesis carried out in the Fischer-Tropsch apparatus, particularly in the syngas production equipment, is important, because water obtained from the air in the equipment used to separate carbon dioxide and water from ambient air is usually insufficient for this purpose. Here, the use of (reaction) water generated in the Fischer-Tropsch synthesis process in the syngas production equipment can only be achieved by the following method: the (reaction) water is characterized by being reacted with approximately 2% by mass of hydrocarbons, particularly, for example, C42. 1-6The hydrocarbons, contaminated with alcohols, aldehydes, and acetone, have extremely high COD levels. They are purified in a water purification unit to at least separate the impurities causing the high COD, and then treated in a pre-reformer before being circulated through a water supply line to the syngas production unit. As explained below, water purification in the water purification unit is preferred so that at least a majority of the approximately 2% by mass hydrocarbon impurities are retained in the purified water from which the impurities causing the high COD have been separated. These hydrocarbons are then converted in the pre-reformer to methane, carbon oxides, water, and hydrogen, which can be reused in the syngas production unit. Therefore, in addition to the (reaction) water generated in the Fischer-Tropsch synthesis, hydrocarbon waste from the Fischer-Tropsch synthesis can also be reused in the syngas production unit. A further advantage of the apparatus according to the invention is that, by means of a process gas supply line from the refining unit to the pre-reformer or a return gas line from the Fischer-Tropsch unit to the pre-reformer, the hydrocarbons from the refining unit, particularly those containing C... 1-5 Process gases containing hydrocarbons or those from Fischer-Tropsch plants that specifically contain C 1-7 Process gases of hydrocarbons, carbon monoxide, and carbon dioxide are converted into methane, carbon oxides, water, and hydrogen in a pre-reformer, which are then reused in the syngas production unit—supplying it via a recirculation line. Thus, hydrocarbon byproducts are reused in the apparatus or method according to the invention, rather than being discharged and disposed of as waste, which not only reduces the amount of waste generated but also maximizes yield and thus increases the efficiency of the syngas production unit by at least 13%. Therefore, the equipment for separating carbon dioxide and water from ambient air, the desalination equipment, the water purification equipment, the pre-reformer, and the syngas production unit work together to utilize not only the (reaction) water produced in the Fischer-Tropsch synthesis but also the hydrocarbons produced in the Fischer-Tropsch synthesis and optionally in the refining unit, thereby maximizing the yield of synthetic fuels, minimizing hydrocarbon waste, and reducing the unit's freshwater requirement to zero or at least very low values. Furthermore, this significantly reduces the amount of wastewater discharged by the unit during its operation. Moreover, the apparatus and method according to the invention allow for a significant reduction in unused waste gas because the generated process gases are reused in individual sections of the unit. Finally, the device and method according to the invention can operate using only electrical energy and in a resource-saving manner, as they do not require natural and fossil raw materials such as crude oil and natural gas.

[0007] According to the invention, the apparatus for separately obtaining carbon dioxide and water from ambient air is an apparatus capable of obtaining carbon dioxide and water from ambient air and then supplying them separately from each other. The apparatus for separately obtaining carbon dioxide and water from ambient air can thus obtain carbon dioxide and water simultaneously from the air, but then separate the water from the carbon dioxide, so that the apparatus for separately obtaining carbon dioxide and water provides a water stream and a separate carbon dioxide stream.

[0008] According to the present invention, the separation unit is designed to separate carbon dioxide and water from crude syngas produced in the syngas production unit, the Fischer-Tropsch unit is designed to produce hydrocarbons from the syngas from which carbon dioxide and water have been separated in the separation unit via a Fischer-Tropsch process, and the refining unit is designed to refine the hydrocarbons produced in the Fischer-Tropsch unit into synthetic fuels. This means that the separation unit for separating carbon dioxide and water is connected to the syngas production unit via a crude syngas supply line, the Fischer-Tropsch unit for producing hydrocarbons via a Fischer-Tropsch process is connected to the separation unit via a syngas supply line, and the refining unit is connected to the Fischer-Tropsch unit via a hydrocarbon supply line.

[0009] As explained above, the device according to the invention can operate with little or no fresh water, and therefore preferably without a fresh water supply line. A fresh water supply line here refers to any line that introduces water from the outside into the device, except for lines that introduce ambient air containing a small percentage of water into the device.

[0010] According to the invention, the apparatus includes a pre-reformer for converting hydrocarbons of a higher grade than methane into methane, carbon oxides, water, and hydrogen, and a steam supply line from a water purification unit to the pre-reformer, through which steam is supplied from the water purification unit, the steam containing higher grade hydrocarbons from a Fischer-Tropsch synthesis carried out in a Fischer-Tropsch unit. Higher grade hydrocarbons herein are all hydrocarbon compounds having more than one carbon atom per molecule, particularly C... 2-7 Hydrocarbons. The pre-reformer allows the decomposition of hydrocarbons produced in Fischer-Tropsch and refining units into methane, carbon oxides, water, and hydrogen, and thus reuses them in the apparatus according to the invention, for example by supplying them to syngas production units. Due to the conversion of all hydrocarbon-containing waste gas streams generated in the pre-reformer, almost no hydrocarbon emissions occur in the apparatus according to the invention, and the efficiency of the apparatus is significantly improved by the reuse of gaseous hydrocarbon streams. Therefore, the pre-reformer increases the carbon yield in the process carried out in the apparatus according to the invention, and thus also increases the overall yield of the process. Furthermore, the pre-reformer protects downstream syngas production units from harmful sulfur compounds by reducing the harmful substance load to below 1 ppb, which is particularly advantageous if the syngas production unit includes one or more co-solid oxide electrolyzers. Finally, the pre-reformer protects downstream syngas production units from coking by removing higher hydrocarbons from the feed stream in the pre-reformer.

[0011] In detail, three sub-reactions occur in the pre-reformer, which can also be called an autothermal reformer or an adiabatic reformer: an endothermic reaction in thermodynamic equilibrium between carbon oxides (CO, CO2), methane, hydrogen, and water, followed by an exothermic methanation and an exothermic shift reaction. The pre-reforming reactor preferably contains nickel oxide as a catalyst. Good results are achieved, particularly when the catalyst contains nickel oxide applied to a support, such as alumina, preferably Al₂O₃. The catalyst also preferably contains chromium oxide (Cr₂O₃). Catalysts containing 20 to 30% by mass of nickel on an alumina support are very particularly preferred, and the catalyst may optionally contain chromium oxide. These catalysts maintain thermal stability up to at least 650°C. Furthermore, these catalysts exhibit extremely high resistance to coking.

[0012] The pre-reformer is preferably designed as a fixed-bed reactor, or more precisely, preferably in a manner in which the water flows through it from top to bottom during its operation.

[0013] In addition, the pre-reformer is preferably designed to operate at pressures of 5 to 30 bar and / or temperatures of 380 to 650°C.

[0014] According to the invention, the apparatus therefore includes a process gas supply line from the refining unit to the pre-reformer and / or a return gas line from the Fischer-Tropsch unit to the pre-reformer. Furthermore, the apparatus includes a circulation line from the pre-reformer to a water supply line connected to a syngas production unit, so as to thus reuse at least to a large extent the process gases generated in the refining unit and the Fischer-Tropsch unit and processed in the pre-reformer. Additionally, a steam circulation line is preferably also provided from the Fischer-Tropsch unit to the syngas production unit.

[0015] Nevertheless, it is preferable to discharge a portion of the process gases generated during the operation of the Fischer-Tropsch unit as flare gas from the unit to avoid enrichment of inert gases in the process gases, which are referred to below as flare gas to distinguish them from other process gases. Therefore, it is preferable that the Fischer-Tropsch unit also has a flare gas discharge line.

[0016] According to another preferred embodiment of the invention, the apparatus for separating carbon dioxide and water from ambient air is a direct air capture device having multiple adsorption / desorption modules connected in parallel, such that the adsorption / desorption modules switch from adsorption mode to desorption mode after reaching their equilibrium load. During operation of the direct air capture device, carbon dioxide and water are separated from ambient air in a discontinuous process by adsorption onto an adsorbent, preferably an amine-functionalized porous solid. Once the adsorbent is saturated with carbon dioxide and water, the carbon dioxide and water or water vapor adsorbed in this manner are then separated from the adsorbent by desorption. To make the method at least quasi-continuous, as explained above, it is preferable to connect multiple adsorption / desorption modules in parallel. Adsorption is carried out at low temperatures, preferably at ambient temperature (-20 to 40°C) and atmospheric pressure, while desorption is carried out under a vacuum, for example, at an absolute pressure of 0.1 to 0.3 bar, and preferably at an elevated temperature of 120 to 150°C. Once the adsorbent is saturated with carbon dioxide and water, the air supply and exhaust to the device are cut off to initiate desorption, and the desorption phase is initiated by pumping a heating medium through the adsorbent to heat it. Simultaneously, a water ring pump is activated to draw out the mixture of carbon dioxide and water vapor; this pump, in addition to generating a high desorption temperature of 150 to 200°C, also creates a vacuum for optimal desorption. The gas flow from the adsorption / desorption module is cooled with cooling water upstream of the water ring pump, and the liquid ring of the pump is also water-cooled. The water ring pump generates such low pressure that the mixture of high-purity carbon dioxide and water can be separated in the downstream separator. Although the impurities in the air can be considered relatively low in principle, due to the discontinuous adsorption method, many impurities, particularly numerous anions and cations (such as ammonia, calcium, magnesium, iron, copper, manganese, chloride, sulfate, nitrogen, nitrate, and sulfate ions), accumulate in the water separated from the ambient air. These impurities must be separated downstream before syngas production. To produce syngas using the preferred co-solid oxide electrolyzer according to the invention, a conductivity of at most 2 µS / cm and preferably less than 2 µS / cm is required. Therefore, the carbon dioxide and water obtained in the apparatus for separating carbon dioxide and water from ambient air are not supplied to the syngas production apparatus together. Instead, the water is first separated from the carbon dioxide by condensation, with the separated water supplied to a desalination unit and the dehydrated carbon dioxide supplied to the syngas production apparatus. Once desorption is complete, the adsorption / desorption module is first cooled to a temperature of approximately 25°C before resuming the adsorption of carbon dioxide and water from the air. For this purpose, the air inlet and outlet of the apparatus are reopened.

[0017] Water of the required purity for syngas production is supplied to the syngas production equipment via the aforementioned water supply lines, preferably in the form of steam. This steam preferably also contains methane, carbon oxides, and hydrogen from the pre-reformer, and may also be supplied with steam originating from the Fischer-Tropsch unit. Here, steam refers to evaporated water, i.e., gaseous water. Even when water for syngas production is preferably supplied in the form of steam, in this context, water is sometimes generally referred to as such without specifying its condensed state. Nevertheless, applicable to all the above and subsequent embodiments, water is preferably supplied to the syngas production equipment in the form of steam.

[0018] Especially when the syngas production plant includes one or more co-solid oxide electrolyzers, good results are achieved in syngas production. Water vapor and carbon dioxide, supplied separately to the syngas production plant, are converted in the co-solid oxide electrolyzer into a gaseous mixture containing carbon monoxide, hydrogen, water vapor, and carbon dioxide. This electrolyzer is preferably operated at 800 to 1000°C, without pressure, and preferably 1.29 V per plane, with a maximum of 1.6 V and 0.6 A / cm². 2 It operates under DC voltage. The crude synthesis gas produced thus contains, for example, 50 to 60% by mass of carbon monoxide, 5 to 10% by mass of hydrogen, 10 to 12% by mass of water vapor and 20 to 30% by mass of carbon dioxide. Hot air is blown into the secondary side of the ceramic membrane to exhaust the oxygen stream formed. The exhaust gas at this time consists of air and a considerable proportion of oxygen. In a co-solid oxide electrolysis cell, water vapor electrolysis (reaction (1): 2*H2O = 2*H2 + O2) is connected with reverse water gas shift reaction (RWGS = reverse water gas shift) (reaction (2): CO2 + H2 = H2O + CO). In this case, 1 mole of H2 from reaction (1) is consumed in reaction (2) and 1 mole of water formed in reaction (2) is consumed in reaction (1) to obtain the overall reaction equation CO2 + 2*H2O = 2*H2 + CO + 1.5*O2, which, under pure chemical stoichiometry, produces an H2 / CO ratio of 2. Oxygen is again transported through the membrane to the air chamber of the co-solid oxide electrolyzer. The H2 / CO ratio can be set to 1.5 to 5 using the feedstock, with a slightly greater than 2.0 preferred for subsequent Fischer-Tropsch synthesis. In summary, a gas mixture containing carbon monoxide, hydrogen, water vapor, and carbon dioxide is produced in the syngas production unit. The water condensed after cooling the gas mixture has a relatively high ion accumulation, therefore it is preferably supplied from the syngas production unit to the desalination unit via a water supply line. Crude syngas in the H2 / CO molar ratio range of 1.5 to 5 can be produced, with an H2 / CO ratio greater than 2.0 being the target for Fischer-Tropsch synthesis. Because the co-solid oxide electrolyzer is sensitive to C... 2+Hydrocarbons are very sensitive—because the co-solid oxide electrolyzer is in C 2+ Coking occurs during operation in the presence of hydrocarbons—process gases and recycle gases are recycled to the syngas production unit, and hydrocarbon-containing process water from the Fischer-Tropsch unit and refining unit is treated in a pre-reformer according to the invention, where non-methane hydrocarbons are converted into methane, carbon oxides, water, and hydrogen. The methane is then converted into carbon oxides and water vapor with oxygen in the syngas production unit, which are then processed again to produce syngas. The methane introduced into the syngas production unit via the pre-reformer thus significantly contributes to reducing the process endothermia to maintain a reaction temperature of approximately 1000°C.

[0019] The crude syngas produced in one or more co-solid oxide electrolyzers still contains a significant proportion of carbon dioxide and a small amount of water vapor, which are separated in downstream separation units to optimize Fischer-Tropsch synthesis. Preferably, the separation units include an amine scrubber for separating carbon dioxide from the crude syngas by absorption, a compressor for condensing water and compressing the syngas to the pressure required for Fischer-Tropsch synthesis, a carbon dioxide recirculation line leading to the syngas production unit or to a carbon dioxide line leading from a device for separately obtaining carbon dioxide and water to the syngas production unit, and a syngas supply line leading to the Fischer-Tropsch unit. In the amine scrubber, carbon dioxide is separated from the crude syngas by absorption with at least one absorbent and recirculated to the syngas production unit via the carbon dioxide recirculation line, said absorbent preferably consisting of an amine compound such as monoethanolamine and / or diethylene glycolamine and water. In the downstream compressor, the remaining syngas is compressed to the pressure required for Fischer-Tropsch synthesis, wherein water is simultaneously condensed and separated from the syngas. The separated water is supplied from the separation unit to the desalination unit via a water supply line, while the remaining (purified) syngas is supplied to the Fischer-Tropsch unit. The syngas supplied to the Fischer-Tropsch unit preferably contains 80 to 90% by mass carbon monoxide and 10 to 15% by mass hydrogen. Separating carbon dioxide from the crude syngas is advantageous because otherwise carbon dioxide would be recycled and enriched, as it is produced in the Fischer-Tropsch synthesis and is not converted. Therefore, by separating carbon dioxide from the crude syngas, the concentration of carbon dioxide does not increase, and the subsequent parts of the unit are thus protected from excessive carbon dioxide loading.

[0020] In the desalination equipment, wastewater streams from at least the equipment used to separately obtain carbon dioxide and water, preferably also from the syngas production equipment and / or from the separation equipment and / or from the compressor used to condense water and compress syngas, are particularly preferably processed so that they can be directly used in other parts of the unit, particularly for example, for the syngas production equipment, for Fischer-Tropsch synthesis, and, if applicable, for hydrogen production. For example, the wastewater stream from the equipment used to separately obtain carbon dioxide and water contains significant amounts of ammonium ions and significant amounts of calcium ions, magnesium ions, chloride ions, and sulfate ions. It also contains other ions such as nitrate ions, nitrogen ions, sulfide ions, iron, and manganese. Furthermore, the wastewater streams from the syngas production equipment, from the separation equipment, and from the compressor used to condense water and compress syngas contain silicon, sodium, calcium, boron, magnesium, iron, lithium, nickel, and lead ions. To this end, in a further extension of the concept of the invention, a desalination device is designed to desalinate and degas water to a conductivity of less than 20 μS / cm, preferably less than 10 μS / cm, particularly preferably less than 5 μS / cm, and most preferably at most 2 μS / cm. In this invention, desalinated water with a conductivity of at most 2 μS / cm is also referred to as completely desalinated water, and the desalination device designed for this purpose is referred to as a completely desalinated device. For this purpose, the desalination device and preferably the completely desalinated device preferably have one or more anion and cation exchangers and membrane devices for degassing. During the degassing process, carbon dioxide, carbon monoxide, nitrogen, and oxygen are reliably separated from the water. The anion and cation exchangers are preferably unloaded using a sodium hydroxide solution or hydrochloric acid. The resulting wastewater has an ion concentration approximately six times that of the water supplied to the desalination device, and due to the simultaneous unloading of the anion and cation exchangers, it can be discharged as neutral wastewater to a municipal wastewater treatment plant.

[0021] The syngas is then converted into hydrocarbons in a Fischer-Tropsch unit. The Fischer-Tropsch synthesis is preferably carried out in a reactor with a catalyst at a temperature of 170 to 270°C, preferably 190 to 250°C, most preferably 210 to 230°C, such as 220°C. Suitable catalysts are particularly selected from cobalt catalysts, such as those preferably Co / MMT (montmorillonite) or Co / SiO2. The Fischer-Tropsch synthesis is preferably carried out in one or more tube bundle units, wherein the catalyst is located in the tubes, while the cooling medium, preferably boiler feedwater, is conducted in the shell space. The Fischer-Tropsch unit preferably includes one or two reactors so that the Fischer-Tropsch synthesis can be carried out in one or two stages. For cost reasons, the Fischer-Tropsch synthesis is preferably carried out in one stage. For example, the Fischer-Tropsch synthesis is carried out at a pressure of 25 to 35 bar, or preferably also at a higher pressure, such as 45 bar. The higher the pressure, the smaller the reactor can be constructed. The Fischer-Tropsch synthesis is preferably carried out to achieve a carbon monoxide conversion rate of 92% or greater. In the Fischer-Tropsch synthesis, condensate and wax are obtained as liquid products, which are supplied to downstream refining units. The highly exothermic process of Fischer-Tropsch synthesis is cooled by boiler feedwater, which is supplied from the desalination unit to the Fischer-Tropsch unit via appropriate pipelines and evaporates to cool the reactor. The steam generated in the Fischer-Tropsch synthesis is preferably supplied, at least in majority, to the syngas production unit via the aforementioned preferred steam recirculation pipelines. The remaining steam from the Fischer-Tropsch unit is preferably used for heating other unit components, so that no external steam is required.

[0022] In the refining unit, the products of Fischer-Tropsch synthesis are refined into synthetic fuels, particularly aviation turbine fuels (kerosene), diesel, and / or gasoline. To produce industrially useful kerosene, diesel, and gasoline, the Fischer-Tropsch alkane products must be converted through hydroisomerization and cracking (isomerization cracking) to produce high-quality aviation turbine fuels with the desired low-temperature properties (preferably with a filterability temperature limit corresponding to a maximum of -40°C "cold filter plugging point"). The heavy products are recycled in the isomerization cracking reactor so that only kerosene and gasoline remain as products. The light gases produced here are supplied as process gases from the refining unit to the pre-reformer via the preferred process gas supply lines described above.

[0023] Therefore, the refining equipment preferably includes one or more isomerization cracking reactors. Preferably, the one or more isomerization cracking reactors contain catalysts that do not require sulfidation, thereby avoiding contamination of the reaction products by sulfur-containing components. This also allows the process gases and water vapor generated during isomerization cracking to be recycled to a syngas production facility, preferably including one or more co-solid oxide electrolyzers. The co-solid oxide electrolyzers tolerate extremely low sulfur concentrations of only 1 pbp or less without damage. Good results are obtained particularly when the catalyst of the one or more isomerization cracking reactors is an element selected from ruthenium, rhodium, palladium, silver, rhenium, osmium, iridium, platinum, gold, copper, rhenium, mercury, and any combination of two or more of the above elements. The one or more isomerization cracking reactors particularly preferably contain a platinum / palladium catalyst. Isomerization cracking is a catalytic reaction in which, in particular, long-chain alkanes are converted into shorter-chain isomers with improved low-temperature properties for kerosene production. This catalytic reaction is preferably carried out in a bed reactor cooled with hydrogen to ensure maximum bed temperature. For example, the bed reactor operates at a pressure of at least 70 bar.

[0024] Furthermore, preferably, the refining equipment includes one or more hydrogen stripping towers for separating light hydrocarbons (i.e., C1 to C4 hydrocarbons). Compared to steam, which is conventionally used for this purpose, the advantage of using hydrogen as the stripping medium is that hydrogen provides significantly better stripping performance due to its lower molecular weight compared to steam, and it can be resupplyed throughout the process via the hydrocarbon return stream leading to the syngas production unit. This also reliably ensures adherence to the preferred maximum sulfur content in the wastewater from the isocracker to the water purification unit.

[0025] Finally, the refining equipment preferably includes one or more distillation columns for separating synthetic fuels into individual fractions, such as aviation turbine fuel and diesel, aviation turbine fuel and gasoline, aviation turbine fuel, gasoline and diesel, etc.

[0026] The isomeric cracking reactor and hydrogen stripping tower require hydrogen. Therefore, in a further extension of the inventive concept, the apparatus is proposed to further include a hydrogen production unit, and preferably also a hydrogen compression unit. Preferably, hydrogen production is carried out by alkaline low-temperature high-pressure water electrolysis. Furthermore, it is preferred that the apparatus includes a hydrogen compression unit to bring the hydrogen produced in the hydrogen production unit to a pressure of 60 to 80 bar, for example, 70 bar, required for refining in the isomeric cracking reactor and hydrogen stripping tower. Preferably, the apparatus further includes a water supply line from the desalination unit to the hydrogen production unit, an air supply line to the hydrogen production unit, a hydrogen line from the hydrogen production unit to the hydrogen compression unit, a water line from the hydrogen compression unit to the desalination unit, and a hydrogen line from the hydrogen compression unit to the refining unit.

[0027] Wastewater generated during Fischer-Tropsch synthesis—which contains a high proportion of hydrocarbons, particularly alcohols, aldehydes, and carboxylic acids, with a chemical oxygen demand (COD) of approximately 40,000 mg / L—cannot be directly supplied to municipal biological wastewater treatment plants. Furthermore, the wastewater contains approximately 2% by mass of hydrocarbons that, according to the invention, should preferably be used for fuel synthesis. Typically, wastewater generated from Fischer-Tropsch synthesis contains significant amounts of methanol and ethanol, and additionally small amounts of propanol, butanol, 2-pentanol, n-hexane, acetaldehyde, propionaldehyde, and acetone. Therefore, Fischer-Tropsch process wastewater is supplied via corresponding pipelines to water purification equipment. Additionally, water formed during the refining process is preferably supplied via corresponding pipelines to water purification equipment. The water purification equipment preferably has one or more partial evaporation units, wherein at least 70% of the wastewater is preferably separated by partial evaporation, and thus at least 75%, preferably at least 95%, of all hydrocarbons contained therein. As an alternative to or supplement to one or more partial evaporation units, all other types of water purification equipment that separates water vapor and at least 75%, preferably at least 95%, of all hydrocarbons contained therein from the wastewater may also preferably be used. According to the invention, the separated water vapor and preferably at least a portion of the separated hydrocarbons are conducted to the pre-reformer via a water supply line or a water vapor supply line.

[0028] It is particularly preferred to use one or more partial evaporation units as water purification equipment, one or more co-solid oxide electrolyzers as syngas production equipment, and refining equipment containing one or more isomerization cracking reactors with catalysts that do not require sulfidation. This reliably ensures that only compounds that will not adversely affect the co-solid oxide electrolyzers (even over long operating times), such as those that damage them and / or cause them to coke, are supplied to the syngas production equipment via the pre-reformer.

[0029] Another subject of the invention is a method for producing synthetic fuels, particularly aviation turbine fuels, gasoline and / or diesel, which is carried out in the apparatus described above.

[0030] As explained above, the method according to the invention can operate without fresh water or with at most a small amount of fresh water. Therefore, it is preferred that less than 20%, more preferably less than 10%, particularly preferably less than 5%, of fresh water be supplied to the method according to the invention, and most preferably no fresh water is supplied at all. Fresh water supply here refers to the supply of various external water sources, not those obtained in the apparatus used to separate carbon dioxide and water from ambient air, to the apparatus.

[0031] According to another preferred embodiment of the invention, carbon dioxide is separated from syngas in a separation device by absorption with at least one amine compound, preferably monoethanolamine and / or diethylene glycolamine and water.

[0032] Furthermore, it is preferred that the water is purified in the desalination equipment to a conductivity of less than 20 µS / cm, more preferably less than 10 µS / cm, particularly preferably less than 5 µS / cm, and most preferably at most 2 µS / cm.

[0033] A further extension of the concept of the invention proposes that flare gas be discharged from the Fischer-Tropsch unit, wherein the flow rate of the flare gas is greater than the quotient of the flow rate of nitrogen and argon contained in the feed stream discharged from the equipment used to separate carbon dioxide and water from ambient air and the total concentration of nitrogen and argon set in the return gas stream from the Fischer-Tropsch unit to the pre-reformer, wherein the total concentration of nitrogen and argon in the return gas stream from the Fischer-Tropsch unit to the pre-reformer is preferably set to 1.5 to 10% by mass. This reliably prevents the accumulation of inert gases, such as nitrogen and argon, in the syngas production equipment and the Fischer-Tropsch unit.

[0034] According to the present invention, the process gas generated in the refining equipment (which preferably contains hydrogen and C) 1-5 Hydrocarbons) and / or return gases generated in the Fischer-Tropsch unit (which preferably contain hydrogen, carbon monoxide, carbon dioxide, water, nitrogen, and C) 1-7 Hydrocarbons are supplied to the pre-reformer, where they are converted into methane, carbon oxides, water, and hydrogen. The gas produced in this way is then fed into the syngas production unit. Process gases produced in the refining unit and return gases produced in the Fischer-Tropsch unit are preferably supplied to the pre-reformer.

[0035] Good results are also achieved, particularly when the apparatus includes a hydrogen production unit and a hydrogen compression unit, and the refining unit comprises one or more isomerization cracking reactors, a hydrogen stripping tower, and one or more distillation towers, wherein the hydrogen produced in the hydrogen production unit is supplied to the hydrogen compression unit and compressed therein, and the compressed hydrogen is supplied to the isomerization cracking reactor and the hydrogen stripping tower of the refining unit. The water required for hydrogen production is preferably supplied from the desalination unit to the hydrogen production unit.

[0036] According to another preferred embodiment of the invention, the refining apparatus includes an isomerization cracking reactor containing a catalyst that does not require sulfidation. Preferably, the catalyst contains an element selected from ruthenium, rhodium, palladium, silver, rhenium, osmium, iridium, platinum, gold, copper, rhenium, mercury, and any combination of two or more of the above elements. The catalyst is particularly preferably composed of platinum / palladium. Particularly preferably, the apparatus is completely free of catalysts that require sulfidation.

[0037] A further extension of the concept of the invention proposes supplying water from a Fischer-Tropsch unit and water from a refining unit to a water purification device, where the water is purified by partial evaporation, such that at least 70% of the wastewater is separated by partial evaporation, and thus at least 75%, preferably at least 95%, of all hydrocarbons are separated. The water vapor and hydrocarbons separated in this manner are then supplied to a pre-reformer, and the unevaporated water having a COD of less than 2000 mg / L is supplied to a municipal wastewater treatment plant.

[0038] Preferably, at least 80%, more preferably at least 90%, particularly preferably at least 95%, and most preferably 100% of the water produced in the equipment for separating carbon dioxide and water from ambient air, the syngas production equipment, the separation equipment, and the optional hydrogen compression equipment is supplied to the desalination equipment.

[0039] Furthermore, it is preferable that carbon dioxide is completely separated from the syngas in the separation device, such that the return gas produced from the syngas in the Fischer-Tropsch unit contains less than 5% by weight of carbon dioxide.

[0040] Finally, it is preferred that aviation turbine fuel, gasoline and / or diesel be produced in a refining unit, with aviation turbine fuel and gasoline being more preferred.

[0041] The invention will now be described in more detail with reference to the accompanying drawings, in which: Figure 1 This is a schematic diagram of an apparatus used to produce synthetic fuels.

[0042] Figure 1 The apparatus 10 shown for producing synthetic fuels includes: a) A device 12 for separating and extracting carbon dioxide and water from ambient air, having an air supply line 14 and an exhaust line 16. b) A syngas production apparatus 18 for producing crude syngas comprising carbon monoxide, hydrogen, carbon dioxide, and water, wherein the syngas production apparatus 18 has a carbon dioxide supply line 20, an air supply line 22, and a water or water vapor supply line 24, and a crude syngas discharge line 25, extending from apparatus 12 for separating carbon dioxide and water from ambient air. c) A separation device 26 for separating carbon dioxide and water from crude syngas produced in the syngas production apparatus 18, having a carbon dioxide circulation line 27 leading from the separation device 26 to a carbon dioxide supply line 20 leading from the apparatus 16 for separating carbon dioxide and water from ambient air to the syngas production apparatus 18. d) A Fischer-Tropsch unit 28 for producing hydrocarbons from syngas from which carbon dioxide and water have been separated in a separation unit 26 via a Fischer-Tropsch process, wherein the syngas is supplied to the Fischer-Tropsch unit 28 via a syngas supply line 29 leading from the separation unit 26 to the Fischer-Tropsch unit 28. e) A refining apparatus 30 for refining hydrocarbons produced in the Fischer-Tropsch unit 28 into synthetic fuels, said refining apparatus being connected to the Fischer-Tropsch unit via a hydrocarbon supply line 31. f) A desalination apparatus 32 for desalinizing water, wherein the desalination apparatus 32 has a water supply line 34 from a device 12 for separating carbon dioxide and water from ambient air, a water supply line 36 from a syngas production device 18, and a water supply line 38 from a separation device 26, and a water discharge line 40 leading to a Fischer-Tropsch unit 28. g) A water purification device 42, which includes a water supply line 44 extending from the refining unit 30 and a water supply line 46 extending from the Fischer-Tropsch unit 28 to purify the water produced therein in each case.

[0043] The apparatus 10 further includes a pre-reformer 48 for converting higher hydrocarbons into methane, carbon oxides, water, and hydrogen. A steam supply line 50 from the water purification unit 42 leads into the pre-reformer 48. Additionally, a supply line 52 for process gas and return gas supplied by a process gas discharge line 54 from the refining unit 30 and a gas discharge line 56 from the Fischer-Tropsch unit 28 leads into the pre-reformer 48. A portion of the gas discharged from the Fischer-Tropsch unit 28 is directed into the supply line 52, while the remainder is discharged from the apparatus 10 via a flare gas line 58. A recirculation line 62 leads from the pre-reformer 48 to a water or steam supply line 24 and from there to the syngas production unit 18 to supply the methane, carbon oxides, water, and hydrogen compounds formed in the pre-reformer 48 to the syngas production unit 18. A steam circulation line 63, connected to a steam exhaust line 64 leading from the Fischer-Tropsch unit 28, also leads to a supply line 24. The steam exhaust line 64 branches into the steam circulation line 63 and an excess steam line 65 extending from the steam exhaust line 64.

[0044] Finally, the apparatus 10 also includes a hydrogen production unit 66 and a hydrogen compression unit 68 to produce the hydrogen required for the refining unit 30. A water supply line 70 and an air supply line 72 from the desalination unit 32 lead into the hydrogen production unit 66. Furthermore, the hydrogen production unit 66 has an exhaust gas line 74 and a hydrogen line 76 leading to the hydrogen compression unit 68. From the hydrogen compression unit 68, the hydrogen line 78 leads into the refining unit 30, and the water line 80 leads into the desalination unit 32.

[0045] The refining unit 30 includes one or more isomerization cracking reactors (not shown), a hydrogen stripping tower (not shown), and one or more distillation towers (not shown). Additionally, the refining unit 30 includes a kerosene line 82 and a gasoline line 84.

[0046] In addition, wastewater pipelines 86, 86', and 86'' are routed from the desalination unit 32, the Fischer-Tropsch unit 28, and the water purification unit 42. Finally, the syngas production unit 18 also has an exhaust gas pipeline 74'.

[0047] During the operation of device 10, air is supplied via air supply line 16 to equipment 12 for separating carbon dioxide and water from ambient air, where carbon dioxide and water are separated from the air. Remaining waste gas is discharged from equipment 12 via waste gas line 16, where water and carbon dioxide are separated by condensation. The separated carbon dioxide is supplied to syngas production equipment 18 via supply line 20, and is also supplied to it via supply lines 24 and 22 with water vapor containing methane, carbon oxides, and hydrogen, as well as air. In syngas production equipment 18, crude syngas containing carbon monoxide, hydrogen, water vapor, and carbon dioxide is produced, and most of the water is separated from it by condensation. The separated water is supplied to desalination equipment 32 via water supply line 38, while the crude syngas is supplied to separation equipment 26 via line 25. Here, carbon dioxide is separated from the crude syngas by absorption, and this carbon dioxide is supplied via line 27 to line 20 and then to syngas production equipment 18. In addition, water is separated from the crude syngas by condensation in separation unit 26, and this water is supplied to desalination unit 32 via line 38. Water separated in unit 12 is also supplied to desalination unit 32 via water supply line 34. Finally, the purified syngas is fed to Fischer-Tropsch unit 28 via line 29, where it is converted into hydrocarbons, primarily n-alkanes. These hydrocarbons are supplied to refining unit 30 via line 31, where they are converted into crude synthetic fuels by hydroisomerization and cracking (isomerization cracking). The crude synthetic fuels are then separated in a hydrogen stripping tower and in one or more distillation towers in refining unit 30 into kerosene and gasoline fractions, which are discharged from unit 10 via lines 82 and 84. Water produced in Fischer-Tropsch unit 28 and refining unit 30 is supplied to water purification unit 42 via lines 46 and 44, where the wastewater is purified by partial evaporation. The reaction in Fischer-Tropsch unit 28 is a highly exothermic reaction requiring cooling. For this purpose, fully desalinated water from desalination unit 32 is supplied to Fischer-Tropsch unit 28 via water discharge line 40, where the heat of reaction of Fischer-Tropsch synthesis is discharged via steam discharge line 64 by generating steam. Most of the steam is supplied to syngas production unit 18 via steam recirculation line 63 and supply line 24, while excess steam is discharged from Fischer-Tropsch unit 28 via excess steam line 65 and used, for example, to evaporate wastewater flowing from Fischer-Tropsch unit 28 to water purification unit 42 via water supply line 46. The steam stream discharged via steam supply line 50 to pre-reformer 48 contains approximately 2% hydrocarbons, which are converted into methane, carbon oxides, water, and hydrogen in pre-reformer 48. The remaining purified wastewater is supplied to municipal wastewater treatment via line 86''. In addition, the return gas generated in the Fischer-Tropsch unit 28 and the process gas generated in the refining process are supplied to the pre-reformer 48 via lines 54, 56, and 52, where higher hydrocarbons are converted into methane, carbon oxides, water, and hydrogen.The feed stream containing methane, carbon oxides, water and hydrogen produced in the pre-reformer 48 is fed into the supply line 24 via the circulation line 62 together with the steam stream from the steam return line 63, and from there into the syngas production unit 18.

[0048] In hydrogen production unit 66, hydrogen is produced from air supplied via line 72 and water supplied via line 70. This hydrogen, as a mixture with water vapor, is supplied via line 76 to hydrogen compression unit 68, where it is compressed to the required pressure and the contained water is simultaneously separated by condensation. The compressed hydrogen is supplied via line 78 to refining unit 30, while the separated water is supplied via line 80 to desalination unit 32.

[0049] The present invention is described below using examples, which are exemplary and not limiting of the invention. Example

[0050] exist Figure 1 The apparatus shown and described above uses PRO / II (AVEVA) process simulation software to simulate the method according to the invention for producing 15,000 liters of kerosene per day. Here, the following product streams are obtained for each pipeline: serial number name kg / h Nm³ / h 14 air supply lines 9576623 20 Carbon dioxide supply pipeline to syngas production equipment 3941 22 Air supply lines to syngas production equipment 7093 24 Water or steam supply lines to syngas production equipment 4137 25 crude syngas discharge line leading to the separation unit 4407 27 Carbon dioxide circulation line from the separation unit 1216 29 Syngas supply pipeline from the separation unit to the Fischer-Tropsch unit 2794 31 hydrocarbon supply pipeline 834 34 From equipment used to separate carbon dioxide and water from ambient air to water supply pipelines for desalination equipment 4501 36 Water supply pipelines from syngas production equipment to desalination equipment 552 38 Water supply pipelines from the separation equipment to the desalination equipment 397 40 Water discharge pipeline from the desalination unit to the Fischer-Tropsch unit 4415 44 Water supply pipelines from refining equipment to water purification equipment 3.2 46 Water supply pipelines from Fischer-Tropsch equipment to water purification equipment 1413 50 Steam supply lines to the pre-reformer 999 52 Supply lines for fuel gas and return gas to the pre-reformer 576 54 fuel gas exhaust pipeline 65 56 Gas exhaust pipeline 547 58 Flare gas exhaust pipeline 37 62 Circulation line from the pre-reformer 1575 63 Steam circulation line from Fischer-Tropsch equipment 2562 64 Water vapor exhaust line from Fischer-Tropsch equipment 4349 65 Excess steam line from Fischer-Tropsch facility 1786 70 Water supply pipeline to the hydrogen production unit 172 72 air supply lines 21130 76 Hydrogen pipeline leading to hydrogen compression equipment 20.7 78 Hydrogen pipeline leading to refining equipment 18.9 80 Water discharge pipeline leading to the desalination equipment 1.8 82 kerosene pipeline 484 84 Gasoline line 300 86 wastewater pipeline 865 86' wastewater pipeline 66 86'' wastewater pipeline 418

[0051] List of reference numerals 10. Equipment for producing synthetic fuels 12. Equipment for separating and removing carbon dioxide and water from ambient air. 14. Air supply lines 16. Exhaust gas pipeline 18 Syngas Production Equipment 20 Carbon dioxide supply lines to the syngas production equipment 22 Air supply lines to the syngas production equipment 24. Water or steam supply lines to syngas production equipment 25. Crude syngas discharge line leading to the separation unit 26. Separation equipment for separating carbon dioxide and water from crude syngas 27. Carbon dioxide recirculation line from the separation unit 28 Fischer-Tropsch equipment 29 Syngas supply lines from the separation unit to the Fischer-Tropsch unit 30 Refining Equipment 31 Hydrocarbon supply pipeline 32 Desalination Equipment 34 Water supply lines from equipment used to separate carbon dioxide and water from ambient air to desalination equipment 36. Water supply pipelines from syngas production equipment to desalination equipment 38. Water supply lines from the separation unit to the desalination unit 40 Water discharge lines from the desalination unit to the Fischer-Tropsch unit 42 Water purification equipment 44 Water supply pipelines from refining equipment to water purification equipment 46 Water supply lines from the Fischer-Tropsch plant to the water purification plant 48 Pre-reformer 50 Steam supply lines to the pre-reformer 52. Supply lines for process gas and return gas to the pre-reformer 54 Process gas exhaust pipeline 56 Gas exhaust pipeline 58 Flare gas exhaust pipeline 62. Circulation line from the pre-reformer 63. Steam circulation lines from the Fischer-Tropsch plant 64. Steam exhaust line from Fischer-Tropsch plant 65. Excess steam line from Fischer-Tropsch facility 66 Hydrogen production equipment 68 Hydrogen compression equipment 70 Water supply lines leading to the hydrogen production unit 72 Air supply lines 74, 74' Exhaust Gas Pipeline 76. Hydrogen pipeline leading to the hydrogen compression equipment 78. Hydrogen pipeline leading to the refining equipment 80 Water discharge lines leading to the desalination equipment 82 Kerosene Pipeline 84 Gasoline Line 86, 86', 86'' Wastewater pipelines.

Claims

1. An apparatus (10) for producing synthetic fuels, comprising: a) Equipment for separating and extracting carbon dioxide and water from ambient air (12), b) A syngas production apparatus (18) for producing crude syngas containing carbon monoxide, hydrogen, carbon dioxide and water, wherein the syngas production apparatus (18) has an air supply line (22), a water supply line (24) and a carbon dioxide supply line (20) extending from a device (12) for separating carbon dioxide and water from ambient air. c) Separation equipment (26) for separating carbon dioxide and water from crude syngas produced in the syngas production equipment (18), d) A Fischer-Tropsch unit (28) for producing hydrocarbons from syngas from which carbon dioxide and water are separated in a separation unit (26) via a Fischer-Tropsch process. e) Refining equipment (30) for refining hydrocarbons produced in the Fischer-Tropsch plant (28) into synthetic fuels. f) A desalination apparatus (32) for desalinizing water, wherein the desalination apparatus (32) has a water supply line (34) from a device (12) for separating carbon dioxide and water from ambient air and a water discharge line (40) leading to a Fischer-Tropsch unit (28), and g) A water purification device (42) comprising a water supply line (44) extending from a refining unit (30) and a water supply line (46) extending from a Fischer-Tropsch unit (28) for purifying water generated therein, wherein the water purification device (42) is configured to extract at least 75% of water vapor and all hydrocarbons contained therein from the water, and to transfer the extracted water vapor and extracted hydrocarbons via a water vapor supply line (50) to a pre-reforming unit (48); The apparatus further includes a pre-reformer (48) for converting non-methane hydrocarbons into methane, carbon oxides, water, and hydrogen, and i) a steam supply line (50) from a water purification unit (42) to the pre-reformer (48), ii) process gas supply lines (54, 52) from a refining unit (30) to the pre-reformer (48), return gas lines (56, 52) from a Fischer-Tropsch unit (28) to the pre-reformer (48), and iii) a circulation line (62) from the pre-reformer (48) to a water supply line (24) connected to a syngas production unit (18), wherein the pre-reformer (48) contains nickel oxide as a catalyst.

2. The apparatus (10) according to claim 1, characterized in that... The device has no fresh water supply pipeline.

3. The apparatus (10) according to claim 1 or 2, characterized in that... The water purification device (42) is designed as a partial evaporator, in which not only water is partially evaporated, but also the hydrocarbons contained therein are partially evaporated.

4. The apparatus (10) according to claim 1 or 2, characterized in that... The refining equipment (30) includes at least one isomerization cracking reactor, wherein the at least one isomerization cracking reactor has a catalyst that does not require sulfidation.

5. The apparatus (10) according to claim 1 or 2, characterized in that... The desalination equipment (32) for desalinating water also has a water supply line (36) from the syngas production equipment (18) and a water supply line (38) from the separation equipment (26).

6. The apparatus (10) according to claim 1 or 2, characterized in that... The syngas production equipment (18) includes one or more co-solid oxide electrolyzers.

7. The apparatus (10) according to claim 1 or 2, characterized in that... The separation equipment (26) includes an amine scrubber for separating carbon dioxide from the syngas by absorption, a compressor for condensing water and for compressing the gas to the pressure required for Fischer-Tropsch synthesis, a carbon dioxide recirculation line (27) leading to the syngas production equipment (18) or to the carbon dioxide line (20) leading from the equipment (12) for separately obtaining carbon dioxide and water to the syngas production equipment (18), and a syngas supply line (29) leading to the Fischer-Tropsch equipment (28).

8. The apparatus (10) according to claim 1 or 2, characterized in that... The desalination equipment (32) includes one or more anion and cation exchangers and a membrane device for degassing, which is designed to desalinate and degas water to a conductivity of less than 20 μS / cm.

9. The apparatus (10) according to claim 1 or 2, characterized in that... The refining equipment (30) includes a hydrogen stripping tower and one or more distillation towers.

10. The apparatus (10) according to claim 1 or 2, characterized in that... The apparatus further includes a hydrogen production unit (66) and a hydrogen compression unit (68), wherein the apparatus (10) further includes a water line (70) leading from the water desalination unit (32) to the hydrogen production unit (66), a water line (80) leading from the hydrogen compression unit (68) to the desalination unit (32), a hydrogen line (76) leading from the hydrogen production unit (66) to the hydrogen compression unit (68), and a hydrogen line (78) leading from the hydrogen compression unit (68) to the refining unit (30).

11. The apparatus (10) according to claim 1, characterized in that... The synthetic fuel is aviation turbine fuel, gasoline, and / or diesel.

12. A method for producing synthetic fuels, carried out in an apparatus (10) according to claim 1, wherein water vapor and at least 75% of all hydrocarbons contained therein are obtained from the water in the water purification device (42), and the obtained water vapor and the obtained hydrocarbons are transferred to a pre-reformer (48) via a water vapor supply line (50).

13. The method according to claim 12, characterized in that... The method supplies less than 20% fresh water, wherein the fresh water supply refers to supplying various external water sources, not those obtained in the equipment used to separate carbon dioxide and water from ambient air, into the device.

14. The method according to claim 12 or 13, characterized in that... In the desalination device (32), water is purified to a conductivity of less than 20 µS / cm.

15. The method according to claim 12 or 13, characterized in that... Flare gas is discharged from the Fischer-Tropsch unit (28), wherein the flow rate of the flare gas is greater than the quotient of the flow rates of nitrogen and argon contained in the feed stream discharged from the device (12) for separating carbon dioxide and water from ambient air and the total concentration of nitrogen and argon set in the return stream from the Fischer-Tropsch unit (28) to the pre-reformer (48).

16. The method according to claim 12 or 13, characterized in that... The apparatus (10) has a hydrogen production unit (66) and a hydrogen compression unit (68), and the refining unit (30) includes one or more isomerization cracking reactors, a hydrogen stripping tower and one or more distillation towers, wherein hydrogen produced in the hydrogen production unit (66) is supplied to the hydrogen compression unit (68) and compressed therein, and the compressed hydrogen is supplied to the hydrogen stripping tower of the refining unit (30).

17. The method according to claim 12 or 13, characterized in that... The refining unit (30) includes one or more isomerization cracking reactors, in which a catalyst that does not require sulfidation is used, and water from the Fischer-Tropsch unit (28) and water from the refining unit (30) are supplied to the water purification unit (42), in which the water is purified by partial evaporation, wherein at least 70% of the partially evaporated water vapor containing hydrocarbons is supplied to the pre-reformer (48) via a steam supply line (50), and less than 30% of the purified water has a COD of less than 2000 mg / l and is supplied to a municipal wastewater treatment plant.

18. The method according to claim 12 or 13, characterized in that... At least 80% of the water produced in the equipment (12) for separating carbon dioxide and water from ambient air, the syngas production equipment (18), the separation equipment (26), and the optional hydrogen compression equipment (68) is supplied to the desalination equipment (32).

19. The method according to claim 12, characterized in that... The synthetic fuel is aviation turbine fuel, gasoline, and / or diesel.

20. The method according to claim 15, characterized in that... The total concentration of nitrogen and argon in the return gas stream from the Fischer-Tropsch unit (28) to the pre-reformer (48) is set to 1.5 to 10 by mass.

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